The influence of non-ideal vapor-liquid-equilibrium on vaporization of multicomponent hydrocarbon fuels
|
|
- Lucinda Richards
- 6 years ago
- Views:
Transcription
1 ICLASS 202, 2 th Trennal Internatonal Conference on Lqud Atomzaton and Spray Systems, Hedelberg, Germany, September 2-6, 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels A. Bader, P. Keller, C. Hasse, B. Meyer Department of Energy Process Engneerng and Chemcal Engneerng, Techncal Unversty of Freberg, Germany Andre.Bader@ec.tu-freberg.de, Peter.Keller@ec.tu-freberg.de, Chrstan.Hasse@ec.tu-freberg.de, Bernd.Meyer@ec.tu-freberg.de Abstract In ths work the dfferences between deal and non-deal vapor-lqud-equlbrum (VLE) and the effect on vaporzaton for multcomponent hydrocarbon fuels, whch are representatve for engnes or gasfers, are nvestgated. Based on these devatons, a parametrc study of non-deal VLE-behavor for a pressure range of bar and a temperature range tll 600 C, whch are typcal vaporzaton condtons n techncal systems, s performed. The VLE results are then appled for a 0D sngle droplet vaporzaton model, whch can be consdered as a base model for most CFD applcatons. The droplet lfe tme and the vaporzaton rates of the sngle components are compared between deal and non-deal behavor varyng the pressure, the temperature and the partcle Reynolds number. The observed dfferences suggest that non-deal VLE have a sgnfcant mpact on the droplet vaporzaton characterstcs for complex hydrocarbon mxtures. Introducton The vaporzaton of fuels s a relevant process n many practcal devces lke engnes, furnaces and gasfers whch effects mxture formaton and further steps lke burnng, gasfcaton or pollutant formaton. The accuracy of the droplet vaporzaton affects all the further steps sgnfcantly. Snce real fuels consst of a large number of speces, t s mportant to model the fuels wth a multcomponent approach. Fuels are usually depcted wth contnuous thermodynamcs, where all the sngle components are lumped together. The descrpton of the real vapor pressure for mxtures has the man mpact on the vaporzaton. Hence, the vapor-lqud-equlbrum (VLE) wll be determned wth sutable real approaches n contrast to the deal approach of Raoult. The non-deal VLE for mxtures s a classcal topc of the multcomponent thermodynamcs whch s essental n all flud separaton technologes lke n petrol chemstry or n gas treatment processes. In praxs there are sgnfcant dfferences n non-deal behavor compared to the deal assumptons. A very popular example s the mxture of ethanol and water whch form an azeotrope. Several studes n the lterature looked at non-deal mxtures and ther VLE. As an example Neroorkar et al. [] analyzed already non-deal vapor-lqud equlbrum propertes of gasolne-ethanol fuel blends wth an emprcal Gasolne-Ethanol Flash model and Aspen Plus up to hgh temperatures but below ts vapor pressure. Zhang et al. studed n [2] the vaporzaton of 00 µm ol droplets n pure ntrogen wth contnuous thermodynamcs and especally for bo-ol droplets n [3]. Wthn the scope of ths work the fuel vaporzaton s nvestgated wth a sngle droplet of dscrete components whereby deal and non-deal VLE approaches are compared. The hydrocarbon fuel vaporzaton s consdered for sngle component fluds and bnary mxtures. The fuel s assumed to be a mxture of so-octane (2,2,4 trmethylpentane) and ethanol, whch results n a ternary vapor-lqud equlbrum (VLE) wth the surroundng ntrogen atmosphere. Iso-octane was chosen n order to model gasolne and was mxed wth ethanol n all mxture ratos, for nstance to model E0 (0 vol.-% ethanol n gasolne). The droplet vaporzaton s dscussed n a pressure range from 0.5 bar tll 20.0 bar and n a ntrogen atmosphere wth temperatures between 0 C and 600 C. The paper starts wth a descrpton of the chosen non-deal VLE model and follows wth an explanaton of the 0D sngle droplet model for multcomponents. After that, the dependency of the ambent gas temperature, relatve droplet velocty and the pressure mpact on the droplet vaporzaton are dscussed n the followng secton. Thereby, the dfferences between deal and non-deal VLE droplet vaporzaton are compared wth each other. Numercal Model The numercal modelng can be dvded nto two parts. The frst part deals wth the descrpton of the nondeal VLE where the correcton factors to account for the non-deal thermo-chemcal equlbrum of lqud and Correspondng author: Andre.Bader@ec.tu-freberg.de
2 2 th ICLASS 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels gas mxtures are determned. In addton, the teraton process wll be ntroduced to determne the new bolng temperature of the mxture. The second part concerns the zero-dmensonal descrpton of the vaporzaton of a sngle droplet combned wth the frst part. Here, a multcomponent vaporzaton model s presented as gven by Law n [4] and extended by mprovements due to convecton and non-deal behavor. Vapor-lqud equlbrum The Gbbs phase rule says that vapor and lqud are at the equlbrum-state f the pressures of both phases are equal. In order to descrbe the non-deal behavor the pressure of speces or mxtures s replaced n the Gbbs- Duhem equaton by a corrected pressure, the so-called fugacty f. The non-deal VLE s acheved f the fugacty of the vapor f v s equal to the one of the lqud phase f l for all sngle components, see eq. (). f l = f v () In general, the two ways besde the deal approach of Raoult to determne the fugacty are the equatons-ofstates (EoS) models and excess Gbbs energy (G E ) models. A typcal EoS model s the Redlch-Kwong-Soave- Wong-Sandler (RKSWS) model. Commonly used G E models are the non-random-two-lquds-model (NRTL) and the Unversal Quaschemcal Functonal Group Actvty Coeffcents model (UNIFAC). The VLE of the ternary mxture consstng of so-octane, ethanol and ntrogen and t s bnary mxture combnatons s llustrated n Fg.. The VLE determnaton was done usng mass fractons and transformed wth a lnear mxng rule nto volume Fgure. VLE of the ternary mxture consstng of so-octane, ethanol and ntrogen and t s bnary mxture combnatons at.0 bar. 2
3 2 th ICLASS 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels fractons. The volume fracton s used to descrbe common lqud mxng ratos n the droplet on volume base, lke 0 vol.-% ethanol n gasolne, called E0. The VLE models are determned wth Aspen Plus for Raoult s law and for the non-deal methods NRTL, RKSWS and UNIFAC. Furthermore the results of an own mplemented NRTLmodel and the expermental data from Wen [5] for the bnary mxture of so-octane and ethanol are gven n Fg.. The bnary mxture of so-octane and ethanol shows an azeotrope pont at around 0.40 kg/kg ethanol and lower bolng and condensaton temperatures for the non-deal approaches as n Raoult s law, whch s typcally used n CFD calculatons. The bnary mxture of so-octane wth ntrogen and the mxture of ethanol wth ntrogen are almost equal for the condensaton temperatures of all of the four methods for both mxtures. In contrast to that the bolng temperature devates. As a consequence the solublty for ntrogen n so-octane and ethanol s set to zero n the sngle drop model, whch wll be dscussed n the next secton. The reason to use the NRTL-model n ths work for the so-octane/ethanol/ntrogen mxture s that the results from the NRTL-model match the measurement data from Wen [5] n good agreement. Furthermore, t s much easer mplementable than the other models, RKSWS and UNIFAC. The fugacty of the vapor phase s defned by eq. (2), where ỹ s the molar fracton of the vapor of component, ϕ v are the fugacty coeffcents of the vapor speces and p the system pressure. f v = ϕ v p = ỹ ϕ v p (2) The fugacty of the lqud phase s formed by the actvaton a and a standard fugacty f + whch has a freely selectable reference state, eq. (3). The actvaton of the lqud phase s determned by the molar fractons x of the lqud components and the actvaton coeffcents γ. Usually, the fugacty of the pure component at saturaton state s selected. Therefore, the vapor pressures p 0 can be used together wth the Poyntng correctons κ whch descrbes the pressure dependency of the fugacty. f l = a f + = γ x f + = γ x f 0 = γ x ϕ 0 p 0 exp p p 0 V 0 RT dp } {{ } κ 0 (3) In order to determne the vapor fracton n the vapor lqud equlbrum, equatons (2) and (3) are nserted n eq. () and result n (4). ỹ = γ x f 0 ϕ v p = ( p γ x p 0 ϕ0 exp p 0 ϕ v p V 0 RT dp ) = γ x p 0 p ϕ 0 exp ( p p 0 ϕ v V 0 RT dp ) = γ x p 0 p ϕ0 ϕ v κ 0 (T, p) (4) The Poyntng correcton can be determned by eq. (5), where ṽ l 0, are the molar volumes of the lqud components, T the temperature and R the unversal gas constant. {ṽl κ 0 0, (T ) ( (T, p) = exp p p 0 RT (T ) )} (5) The fugacty coeffcents of the vapor at system pressure and saturaton state are calculated usng eq. (6) and (7), respectvely. { } B ϕ v (T ) = exp RT p ϕ 0 = exp { } B (T ) RT p 0,(T ) (6) (7) 3
4 2 th ICLASS 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels The second Vral coeffcents B are determned by the method of Tsonopoulos [6], and are n the form of eq. (8) whch use the crtcal pressure p c, the crtcal temperature T c, the current drop temperature T and the reduced temperature T r = T/T c. Ths method s based on the correspondence prncple of Ptzer and Curl [7]. B p c RT c = f (0) (T r ) + ωf () (T r ) + f (2) (T r ) (8) The actvaton coeffcents γ are determned applyng the NRTL (non random two lquds) model, whch was developed by Renon et. al [8], and can be calculated usng equaton (9). The NRTL model base on mass fracton x and on the temperature dependent NRTL parameters τ j and G j, whch can be determned wth eq. (0) tll (2). The coeffcents A j, B j, C j, D j come from the Aspen database. K x j G j τ j j= K ln γ = + K x k G j= k k= k= K x j G x l G l τ l j K τ l= j K x k G kj x k G kj k= (9) τ j = A j + B j T (0) G j = exp { α j τ j } () α j = C j + D j (2) In contrast to the non-deal VLE, n deal approaches the actvaton and fugacty coeffcents are equal to one n eq. (4) whch s well known as Raoult s law. The results from the NRTL-model correspond wth the measurement data from Wen [5] and are equal to the results obtaned from the software ASPEN Plus. The VLE of the ternary mxture consstng of so-octane, ethanol and ntrogen and ts bnary mxture combnatons s calculated wth eq. (4). The non-deal vapor-lqud-equlbrum s calculated teratvely wth eq. (4) by adjustng the temperature at a gven system pressure, as γ = f(x, T ), s temperature dependent. Hgher pressures lead to hgher bolng and condensaton temperatures. The azeotrope ponts change from 0.37 kg/kg at atm at hgher pressures to hgher ethanol concentratons (0.57 kg/kg at 0 bar and 0.63 kg/kg at 20 bar). The dfferences between the non-deal NRTL model compared wth Raoult s law ncrease wth pressure, especally at so-octane contents lower than the azeotrope. Fnally, t s demonstrated that the NRTL-model gves the same results as the ASPEN-NRTL-model even at hgh pressures and hence can be used n the sngle droplet model up to 20 bar. Sngle Droplet Vaporzaton The vaporzaton rate and change of composton, radus and temperature are calculated usng the method of Law [4]. Assumng a unbounded atmosphere, the quas-steady, sobarc and sphercally symmetrc vaporzaton of a sngle multcomponent droplet s descrbed. The equatons to calculate the mole fractons of the lqud components, the radus and the surface temperature of the droplet are wrtten for a zero-dmensonal droplet (dscretzed n tme) and read x (n ) x (n) (r (n ) ) 3 3 Ω ṁ F δt 4πM = (r (n ) ) 3 ex (n ) M ρ (n ),l ex (n ) M Ω 3 ṁ ρ (n ) F δt,l 4πM (3) ( r (n) = 3 (r (n ) ) 3 3 4π δt Ω ṁ F ρ (n ),l ) ex (n) M ρ (n),l ex (n) M ρ (n ),l 4 (4)
5 2 th ICLASS 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels T (n) s = T (n ) s + ṁ F δth 4 c p,g 3 π(r(n ) ) 3 ρ (n ) m,l (5) wth total vaporzaton rate ṁ F, fractonal vaporzaton rates Ω, heat nput functon H, molar masses M, denstes of lqud components ρ,l and lqud mxture ρ m,l, tme step sze δt, heat capacty of gas mxture c p,g, radus r and surface temperature T s. The superscrpts (n ) and (n) denote the old and new state, respectvely. All of the spece propertes are calculated temperature dependent wth the equatons and coeffcents from Yaws [9]. The orgnal equaton was formulated by Law [4] for stagnant envronments only. As the drop has a moton relatve to the ambent atmosphere, the heat and mass transfer across the drop surface are ncreased. Hence, the Nusselt number requres a convecton correcton as proposed by Turns [0]. The total vaporzaton rate then reads wth ṁ F = 2Nu πλ gr c p,g ln ( + y ) F,s y F,s Nu = Re/2 P r /3 ( ReP r 4/3 ) /2, (7) thermal conductvty of the gas mxture λ g and total surface mass fracton of vapor y F,s. Ths surface mass fracton s determned usng the VLE-model mentoned prevously and hence ncludes non-deal behavor of lquds and gases, too. The Reynolds number Re represents the relatve moton between droplet and the ambent medum. The sngle droplet model s solved by ntegratng the eq. (3) tll (5) wth fxed tme steps of order δt 0 5 s. Results and Dscusson In ths secton the temperature, relatve droplet velocty and the pressure dependency applyng the sngle droplet model s dscussed. The mpacts are descrbed for dfferent ntal compostons, frst for the sngle components so-octane and ethanol and second for the mxtures. For nstance, E90 represents a mxture of 90 vol.-% ethanol and 0 vol.-% so-octane. For all cases, the sngle droplet model s ntalzed wth a dameter of D d = 00 µm and at lqud temperature of T lqud = 25 C. The soluton of sngle droplet model s obtaned by ntegratng the equatons of the prevous secton and ended because of numercal reasons at a fnal droplet sze wth r = 5 µm. Temperature dependency The temperature dependency s dscussed at a system pressure of 0 bar. The results are llustrated n Fg. 2 whereas an ambent gas temperature of 25 C s represented n the left column and 600 C at the rght column. Varous ntal compostons are used for both ambent gas temperatures. All these cases are calculated wth Raoult s law as well as the NRTL-model. Fgure 2 shows the transent normalzed squared dameter n the frst row. The tme scale s normalzed wth the droplet lfe tme (DLT). Ths tme scale s appled for all the pctures n Fg. 2. For pure so-octane (E00) at 25 C gas temperature the DLT s.0444 s n the deal case and s n the NRTL-model case, whch results n an error of 5.7%. The error decreases wth a hgher ethanol content. For nstance to 34.7% at 0.60 mol/mol ethanol, whereas the DLT ncrease to.6448 s n the deal case and.224 s n the NRTL-model case. The mnmal error s at 0.92 mol/mol ethanol wth 9.5% and ncreases at.00 mol/mol ethanol to 20.4%. At 600 C gas temperature the droplet vaporze 40 tll 60 tmes faster than at 25 C gas temperature both wth the NRTL as well wth the Raoult approach. In the case of 600 C gas temperature the DLT s longer n the NRTL-model case compared to the deal DLTs at 25 C gas temperature. The error s always lower then 2.0%. The transent surface temperatures of the droplet are llustrated n the second row of Fg. 2. Fgure 3 gves the transent equlbrum molar fractons n the gas phase of so-octane and ethanol for the ntal compostons E0 and E90. The reman to 00 % s ntrogen. In Fgure 2 at 25 C gas temperature, both pure ethanol and pure so-octane show a lnear D 2 -law behavor for the Raoult approach as well as for the NRTL-model. Even for mxtures wth less ethanol lke E0, the droplet dameter decreases wth an almost lnear D 2 -law behavor, as the vapor pressures are close to each other. Only for hgher ethanol contents wth a non-deal NRTL approach, the droplet shrnkng velocty shows a characterstc turnng pont after ethanol left the droplet completely. At the same tme the droplet surface temperature ncreases because the enthalpy of vaporzaton of so-octane s lower than the one of ethanol. For the deal approach the droplet 5 (6)
6 2 th ICLASS 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels D 2 /D p = 0.0 bar; T Gas = 25 C; T lqud = 25 C Raoult; E00 NRTL; E00 Raoult; E0 NRTL; E0 Raoult; E60 NRTL; E60 Raoult; E90 NRTL; E90 Raoult; E00 NRTL; E00 D 2 /D p = 0.0 bar; T Gas = 600 C; T lqud = 25 C tme/tme end [s/s] 0 tme/tme end [s/s] Temperature [ C] Temperature [ C] tme/tme end [s/s] 20 tme/tme end [s/s] Fgure 2. Normalzed droplet square dameter and surface temperature at T gas = 25 C (left) and T gas = 600 C (rght) at 0 bar, T lqud = 25 C, Re = 0 Vapor mole fracton at droplet surface [mol/mol] Iso Octane Raoult; E0 Iso Octane NRTL; E0 Ethanol Raoult; E0 Ethanol NRTL; E0 Iso Octane Raoult; E90 Iso Octane NRTL; E90 Ethanol Raoult; E90 Ethanol NRTL; E expands at the begnnng of the vaporzaton because of thermal expanson and has a hgher vaporzaton rate the densty reduces 0.00at hgher temperatures by the equatons of 0.00 Yaws [9], whereby no correcton for the property Vapor mole fracton at droplet surface [mol/mol] Iso Octane Raoult; E0 Iso Octane NRTL; E0 Ethanol Raoult; E0 Ethanol NRTL; E0 Iso Octane Raoult; E90 Iso Octane NRTL; E90 Ethanol Raoult; E90 Ethanol NRTL; E90 vaporzaton rate and the temperature are constant for the most of the tme as the dfferences between condensaton and the bolng curve are almost equal, see Fg.. The conclusons derved from the 25 C gas temperature case can be adapted to the 600 C case. But the droplet n the case of gas temperature 600 C compared to 25 C n the ambent atmosphere. The droplet expands, as mxng s mplemented as the error s assumed to be small. The error occurs as well n the deal and n the nondeal case. Consequently, the assumpton has no mpact on0.000 the dfference between deal and non-deal droplet vaporzaton, whch s the focus n tme/tme ths end work. [s/s] The transent droplet surface temperature tme/tme end [s/s] converges to so-octane bolng temperature (T bol = C at 0 bar) when ethanol left the droplet completely. Fgure 3 shows the ethanol and the so-octane content n the vapor phase at the droplet surface. If the vapor phase content of a spece s zero, the spece does not exst n the droplet anymore, too. Ethanol leaves the droplet completely n the deal and the NRTL approach f only less ethanol, lke E0, s n the ntal composton of the droplet. At hgher ntal ethanol content, lke E90, ethanol leaves the droplet completely only for the deal approach. For the NRTL approach the droplet surface temperature s close to the mxture bolng pont temperature at 0 bar, and the droplet conssts of both ethanol and so-octane tll the end of the droplet lfe tme, see Fg. 3. Fnally, t can be concluded that the vaporzaton takes longer the hgher the ntal content of ethanol s and that at hgher temperatures, the dfference n the DLT between the deal and the non-deal behavor s reduced. But for ntal compostons wth a hgh ethanol content the error ncreases agan after a decrease, see Fg. 4. At 25 C gas temperature, the maxmum error s at +82% related to an ntal composton of 40 vol.-% ethanol. Whereas at 600 C gas temperature the maxmum error s at 2% related to an ntal composton of 70 vol.-% ethanol. The regons of error maxma can be better derved from Fg. 4 whch wll be dscussed n a later secton. 6
7 Tempe 6 Tempe tme/tme end [s/s] 2 th tme/tme ICLASS 202 The nfluence end [s/s] of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels Iso Octane Raoult; E0 Iso Octane NRTL; E0 Ethanol Raoult; E0 Ethanol NRTL; E0 Iso Octane Raoult; E90 Iso Octane NRTL; E90 Ethanol Raoult; E90 Ethanol NRTL; E90 Iso Octane Raoult; E0 Iso Octane NRTL; E0 Ethanol Raoult; E0 Ethanol NRTL; E0 Iso Octane Raoult; E90 Iso Octane NRTL; E90 Ethanol Raoult; E90 Ethanol NRTL; E90 Vapor mole fracton at droplet surface [mol/mol] p = 0.0 bar; T Gas = 25 C; T lqud = 25 C tme/tme end [s/s] Vapor mole fracton at droplet surface [mol/mol] p = 0.0 bar; T Gas = 600 C; T lqud = 25 C tme/tme end [s/s] Fgure 3. Equlbrum vapor mole fracton for E0 and E90 at T gas = 25 C (left) and T gas = 600 C (rght) at 0 bar, T lqud = 25 C, Re = 0 Relatve droplet velocty dependency The vaporzaton rate of the droplet s affected by the gas flow around the droplet. Increasng relatve veloctes between gas and droplet are represented by an ncreasng Reynolds number Re. The Reynolds number can only be ncreased to a maxmum value of Re = 00 n order to avod droplet break-up. Because of ntegraton nto the vaporzaton rate, the DLT of course decreases wth ncreasng Re. The relatve error of the vaporzaton rate between the deal and the non-deal approach can be calculated wth the help of eq. (6) n eq. (8). As eq. (8) can be reduced by the Nu(Re, P r), the relatve moton has no mpact on the error. The error has the maxmum at ntal composton around the azeotrope concentraton. ṁ F,deal ṁ F,non-deal ṁ F,non-deal = 2Nu(Re, P r) πλ g c p,gr +yf,s,deal ln y F,s,deal 2Nu(Re, P r) πλg +yf,s,non-deal c p,gr ln y F,s,non-deal (8) 2Nu(Re, P r) πλg +yf,s,non-deal c p,gr ln y F,s,non-deal Pressure dependency The vaporzaton of the fuel droplet s analyzed wth the sngle droplet model wth pressures at 0.5 bar, 5 bar, 0 bar and 20 bar. Furthermore, the ambent gas temperature s varated n a range from T = 0 C to T = 600 C and the ntal mxture s changed from 0 vol.-% to 00 vol.-% ethanol for a parameter study. The dfference n the DLT between the deal and the non-deal approach f rel s calculated wt eq. (9) and s represented n Fg. 4. f rel = DLT deal DLT real DLT real (9) The DLT wth the Raoult approach s longer than wth the NRTL approach at low temperatures. Ths s because the vapor pressure s ncreased usng the NRTL approach for the ethanol/so-octane mxture. Thereby, the dfferences ncrease wth hgher pressures. Whereas hgh temperatures reduce the dfferences between the vapor pressure. Hence, the DLT error between deal and non-deal decreases. Except for hgh ethanol contents n the ntal composton at hgh temperatures the DLT s longer wth the NRTL approach than wth deal approach as the vaporzaton of so-octane s preferred at the begnnng n the non-deal approach n contrast to the deal approach. Ths behavor can be derved from Fg.. In general, the DLT ncreases wth the pressure ncrease. The postve maxmum of the DLT error s always at 0 C. Only the ntal ethanol content vares whch results n a maxmum shft from 37 vol.-% to 23 vol.-% at a pressure change from 0.5 bar to 20 bar. The maxmum of the negatve error s at the lmt of the dscussed regon at 600 C and at 74 vol.-% ethanol for 5, 0 and 20 bar. Only at 0.5 bar, the maxmum of the negatve error s at a gas temperature of 270 C and at 68 vol.-%. 7
8 2 th ICLASS 202 The nfluence of non-deal vapor-lqud-equlbrum on vaporzaton of multcomponent hydrocarbon fuels Fgure 4. Error of droplet-lfe-tme between Raoult and NRTL approach at 0.5,.0, 0 and 20 bar for ntal mxtures of ethanol an so-octane between 0% - 00% ( + / red non-deal s faster than deal) and ( - / blue deal s faster than non-deal) by T lqud = 25 C and ndependent of Re. Colorbar s scaled to +20% and -20%. Summary and Conclusons The use of Raoult s law nstead of a non-deal approach lke NRTL can lead to an error n the droplet lfe tme up to more than 400%. Crtcal regons are at ambent gas temperatures lower than around 00 C especally at ntal compostons wth lower ethanol content than at the azeotrope pont. The error ncreases wth hgher pressures and lower temperatures. For the current formulaton, the Reynolds number has no mpact n a 0D sngle droplet model on the error between deal and non-deal approaches. Fnally, t can be concluded that non-deal descrptons of vapor-lqud-equlbrums should be ncluded n CFD solvers, as sgnfcant dfferences between deal and non-deal approaches can be notced even n smple sngle droplet models. Acknowledgements The authors acknowledge the funded research by the Federal Mnstry of Educaton and Research of Germany n the framework of Vrtuhcon (project number 03Z2FN), the Bavaran Scence Foundaton n the project WDKO(project number AZ-932-0) and by Ar Lqude S.A. References [] Neroorkar, K. and Schmdt, D., Fuel Vol. 90, p (200). [2] Zhang, L. and Kong, Song-Charng, Combuston and Flame Vol. 58, p (20). [3] Zhang, L. and Kong, Song-Charng, Fuel Vol. 95, p (202). [4] Law, C.K., Combuston and Flame Vol. 26, p (976). [5] Wen, C.C. and Tu. C. H., Flud Phase Equlbrum Vol. 258, p (2007). [6] Tsonopoulos, C., AIChEJ Vol. 2 p (975). [7] Ptzer, K. S. and Curl, R. F., J. Am. Chem. Soc. Vol. 79 p (957). [8] Renon, H. and Prausntz, J.M., AIChEJ Vol. 4 p (968). [9] Yaws, C. L., Chemcal propertes handbook ISBN (999). [0] Turns, S.R., McGraw-Hll, 3 rd Internatonal Edton ISBN (2000). 8
Energy, Entropy, and Availability Balances Phase Equilibria. Nonideal Thermodynamic Property Models. Selecting an Appropriate Model
Lecture 4. Thermodynamcs [Ch. 2] Energy, Entropy, and Avalablty Balances Phase Equlbra - Fugactes and actvty coeffcents -K-values Nondeal Thermodynamc Property Models - P-v-T equaton-of-state models -
More informationSupplementary Notes for Chapter 9 Mixture Thermodynamics
Supplementary Notes for Chapter 9 Mxture Thermodynamcs Key ponts Nne major topcs of Chapter 9 are revewed below: 1. Notaton and operatonal equatons for mxtures 2. PVTN EOSs for mxtures 3. General effects
More informationIntroduction to Vapor/Liquid Equilibrium, part 2. Raoult s Law:
CE304, Sprng 2004 Lecture 4 Introducton to Vapor/Lqud Equlbrum, part 2 Raoult s Law: The smplest model that allows us do VLE calculatons s obtaned when we assume that the vapor phase s an deal gas, and
More informationIf two volatile and miscible liquids are combined to form a solution, Raoult s law is not obeyed. Use the experimental data in Table 9.
9.9 Real Solutons Exhbt Devatons from Raoult s Law If two volatle and mscble lquds are combned to form a soluton, Raoult s law s not obeyed. Use the expermental data n Table 9.3: Physcal Chemstry 00 Pearson
More informationThe ChemSep Book. Harry A. Kooijman Consultant. Ross Taylor Clarkson University, Potsdam, New York University of Twente, Enschede, The Netherlands
The ChemSep Book Harry A. Koojman Consultant Ross Taylor Clarkson Unversty, Potsdam, New York Unversty of Twente, Enschede, The Netherlands Lbr Books on Demand www.bod.de Copyrght c 2000 by H.A. Koojman
More informationI wish to publish my paper on The International Journal of Thermophysics. A Practical Method to Calculate Partial Properties from Equation of State
I wsh to publsh my paper on The Internatonal Journal of Thermophyscs. Ttle: A Practcal Method to Calculate Partal Propertes from Equaton of State Authors: Ryo Akasaka (correspondng author) 1 and Takehro
More informationOpen Systems: Chemical Potential and Partial Molar Quantities Chemical Potential
Open Systems: Chemcal Potental and Partal Molar Quanttes Chemcal Potental For closed systems, we have derved the followng relatonshps: du = TdS pdv dh = TdS + Vdp da = SdT pdv dg = VdP SdT For open systems,
More information( ) 1/ 2. ( P SO2 )( P O2 ) 1/ 2.
Chemstry 360 Dr. Jean M. Standard Problem Set 9 Solutons. The followng chemcal reacton converts sulfur doxde to sulfur troxde. SO ( g) + O ( g) SO 3 ( l). (a.) Wrte the expresson for K eq for ths reacton.
More informationMulticomponent Vaporization Modeling of Petroleum-Biofuel Mixture at High-Pressure Conditions
ILASS Amercas, 3 rd Annual Conference on Lqud Atomzaton and Spray Systems, Ventura, CA, May 011 Multcomponent Vaporzaton Modelng of Petroleum-Bofuel Mxture at Hgh-Pressure Condtons L. Zhang and Song-Charng
More informationAdiabatic Sorption of Ammonia-Water System and Depicting in p-t-x Diagram
Adabatc Sorpton of Ammona-Water System and Depctng n p-t-x Dagram J. POSPISIL, Z. SKALA Faculty of Mechancal Engneerng Brno Unversty of Technology Techncka 2, Brno 61669 CZECH REPUBLIC Abstract: - Absorpton
More informationA Self-Consistent Gibbs Excess Mixing Rule for Cubic Equations of State: derivation and fugacity coefficients
A Self-Consstent Gbbs Excess Mxng Rule for Cubc Equatons of State: dervaton and fugacty coeffcents Paula B. Staudt, Rafael de P. Soares Departamento de Engenhara Químca, Escola de Engenhara, Unversdade
More informationINTRODUCTION TO CHEMICAL PROCESS SIMULATORS
INTRODUCTION TO CHEMICAL PROCESS SIMULATORS DWSIM Chemcal Process Smulator A. Carrero, N. Qurante, J. Javaloyes October 2016 Introducton to Chemcal Process Smulators Contents Monday, October 3 rd 2016
More information(1) The saturation vapor pressure as a function of temperature, often given by the Antoine equation:
CE304, Sprng 2004 Lecture 22 Lecture 22: Topcs n Phase Equlbra, part : For the remander of the course, we wll return to the subject of vapor/lqud equlbrum and ntroduce other phase equlbrum calculatons
More information3. Be able to derive the chemical equilibrium constants from statistical mechanics.
Lecture #17 1 Lecture 17 Objectves: 1. Notaton of chemcal reactons 2. General equlbrum 3. Be able to derve the chemcal equlbrum constants from statstcal mechancs. 4. Identfy how nondeal behavor can be
More informationmodeling of equilibrium and dynamic multi-component adsorption in a two-layered fixed bed for purification of hydrogen from methane reforming products
modelng of equlbrum and dynamc mult-component adsorpton n a two-layered fxed bed for purfcaton of hydrogen from methane reformng products Mohammad A. Ebrahm, Mahmood R. G. Arsalan, Shohreh Fatem * Laboratory
More informationTransfer Functions. Convenient representation of a linear, dynamic model. A transfer function (TF) relates one input and one output: ( ) system
Transfer Functons Convenent representaton of a lnear, dynamc model. A transfer functon (TF) relates one nput and one output: x t X s y t system Y s The followng termnology s used: x y nput output forcng
More informationSolution Thermodynamics
Soluton hermodynamcs usng Wagner Notaton by Stanley. Howard Department of aterals and etallurgcal Engneerng South Dakota School of nes and echnology Rapd Cty, SD 57701 January 7, 001 Soluton hermodynamcs
More information10.34 Numerical Methods Applied to Chemical Engineering Fall Homework #3: Systems of Nonlinear Equations and Optimization
10.34 Numercal Methods Appled to Chemcal Engneerng Fall 2015 Homework #3: Systems of Nonlnear Equatons and Optmzaton Problem 1 (30 ponts). A (homogeneous) azeotrope s a composton of a multcomponent mxture
More informationGeneral Thermodynamics for Process Simulation. Dr. Jungho Cho, Professor Department of Chemical Engineering Dong Yang University
General Thermodynamcs for Process Smulaton Dr. Jungho Cho, Professor Department of Chemcal Engneerng Dong Yang Unversty Four Crtera for Equlbra μ = μ v Stuaton α T = T β α β P = P l μ = μ l1 l 2 Thermal
More informationUniversity of Washington Department of Chemistry Chemistry 452/456 Summer Quarter 2014
Lecture 16 8/4/14 Unversty o Washngton Department o Chemstry Chemstry 452/456 Summer Quarter 214. Real Vapors and Fugacty Henry s Law accounts or the propertes o extremely dlute soluton. s shown n Fgure
More informationAppendix II Summary of Important Equations
W. M. Whte Geochemstry Equatons of State: Ideal GasLaw: Coeffcent of Thermal Expanson: Compressblty: Van der Waals Equaton: The Laws of Thermdynamcs: Frst Law: Appendx II Summary of Important Equatons
More informationAssignment 4. Adsorption Isotherms
Insttute of Process Engneerng Assgnment 4. Adsorpton Isotherms Part A: Compettve adsorpton of methane and ethane In large scale adsorpton processes, more than one compound from a mxture of gases get adsorbed,
More informationLNG CARGO TRANSFER CALCULATION METHODS AND ROUNDING-OFFS
CARGO TRANSFER CALCULATION METHODS AND ROUNDING-OFFS CONTENTS 1. Method for determnng transferred energy durng cargo transfer. Calculatng the transferred energy.1 Calculatng the gross transferred energy.1.1
More informationELASTIC WAVE PROPAGATION IN A CONTINUOUS MEDIUM
ELASTIC WAVE PROPAGATION IN A CONTINUOUS MEDIUM An elastc wave s a deformaton of the body that travels throughout the body n all drectons. We can examne the deformaton over a perod of tme by fxng our look
More informationCHEMICAL ENGINEERING
Postal Correspondence GATE & PSUs -MT To Buy Postal Correspondence Packages call at 0-9990657855 1 TABLE OF CONTENT S. No. Ttle Page no. 1. Introducton 3 2. Dffuson 10 3. Dryng and Humdfcaton 24 4. Absorpton
More informationNon-Ideality Through Fugacity and Activity
Non-Idealty Through Fugacty and Actvty S. Patel Deartment of Chemstry and Bochemstry, Unversty of Delaware, Newark, Delaware 19716, USA Corresondng author. E-mal: saatel@udel.edu 1 I. FUGACITY In ths dscusson,
More informationPhase equilibria for the oxygen-water system up to elevated temperatures and pressures
Phase equlbra for the oxygen-water system up to elevated temperatures and pressures Xaoyan J 1, 2, Xaohua Lu 2, Jnyue Yan 1,3* 1 Department of Chemcal Engneerng and Technology / Energy Processes, Royal
More informationThermodynamics General
Thermodynamcs General Lecture 1 Lecture 1 s devoted to establshng buldng blocks for dscussng thermodynamcs. In addton, the equaton of state wll be establshed. I. Buldng blocks for thermodynamcs A. Dmensons,
More informationWeek3, Chapter 4. Position and Displacement. Motion in Two Dimensions. Instantaneous Velocity. Average Velocity
Week3, Chapter 4 Moton n Two Dmensons Lecture Quz A partcle confned to moton along the x axs moves wth constant acceleraton from x =.0 m to x = 8.0 m durng a 1-s tme nterval. The velocty of the partcle
More informationNumerical Heat and Mass Transfer
Master degree n Mechancal Engneerng Numercal Heat and Mass Transfer 06-Fnte-Dfference Method (One-dmensonal, steady state heat conducton) Fausto Arpno f.arpno@uncas.t Introducton Why we use models and
More informationName: SID: Discussion Session:
Name: SID: Dscusson Sesson: Chemcal Engneerng Thermodynamcs 141 -- Fall 007 Thursday, November 15, 007 Mdterm II SOLUTIONS - 70 mnutes 110 Ponts Total Closed Book and Notes (0 ponts) 1. Evaluate whether
More informationGasometric Determination of NaHCO 3 in a Mixture
60 50 40 0 0 5 15 25 35 40 Temperature ( o C) 9/28/16 Gasometrc Determnaton of NaHCO 3 n a Mxture apor Pressure (mm Hg) apor Pressure of Water 1 NaHCO 3 (s) + H + (aq) Na + (aq) + H 2 O (l) + CO 2 (g)
More informationMass Transfer Processes
Mass Transfer Processes S. Majd Hassanzadeh Department of Earth Scences Faculty of Geoscences Utrecht Unversty Outlne: 1. Measures of Concentraton 2. Volatlzaton and Dssoluton 3. Adsorpton Processes 4.
More informationModule 3: The Whole-Process Perspective for Thermochemical Hydrogen
"Thermodynamc Analyss of Processes for Hydrogen Generaton by Decomposton of Water" by John P. O'Connell Department of Chemcal Engneerng Unversty of Vrgna Charlottesvlle, VA 2294-4741 A Set of Energy Educaton
More informationProblem Set #6 solution, Chem 340, Fall 2013 Due Friday, Oct 11, 2013 Please show all work for credit
Problem Set #6 soluton, Chem 340, Fall 2013 Due Frday, Oct 11, 2013 Please show all work for credt To hand n: Atkns Chap 3 Exercses: 3.3(b), 3.8(b), 3.13(b), 3.15(b) Problems: 3.1, 3.12, 3.36, 3.43 Engel
More informationExercises of Fundamentals of Chemical Processes
Department of Energ Poltecnco d Mlano a Lambruschn 4 2056 MILANO Exercses of undamentals of Chemcal Processes Prof. Ganpero Gropp Exercse 7 ) Estmaton of the composton of the streams at the ext of an sothermal
More informationDETERMINATION OF CO 2 MINIMUM MISCIBILITY PRESSURE USING SOLUBILITY PARAMETER
DETERMINATION OF CO 2 MINIMUM MISCIBILITY PRESSURE USING SOLUBILITY PARAMETER Rocha, P. S. 1, Rbero, A. L. C. 2, Menezes, P. R. F. 2, Costa, P. U. O. 2, Rodrgues, E. A. 2, Costa, G. M. N. 2 *, glora.costa@unfacs.br,
More informationLecture. Polymer Thermodynamics 0331 L Chemical Potential
Prof. Dr. rer. nat. habl. S. Enders Faculty III for Process Scence Insttute of Chemcal Engneerng Department of Thermodynamcs Lecture Polymer Thermodynamcs 033 L 337 3. Chemcal Potental Polymer Thermodynamcs
More informationCHAPTER 5 NUMERICAL EVALUATION OF DYNAMIC RESPONSE
CHAPTER 5 NUMERICAL EVALUATION OF DYNAMIC RESPONSE Analytcal soluton s usually not possble when exctaton vares arbtrarly wth tme or f the system s nonlnear. Such problems can be solved by numercal tmesteppng
More informationChemical Equilibrium. Chapter 6 Spontaneity of Reactive Mixtures (gases) Taking into account there are many types of work that a sysem can perform
Ths chapter deals wth chemcal reactons (system) wth lttle or no consderaton on the surroundngs. Chemcal Equlbrum Chapter 6 Spontanety of eactve Mxtures (gases) eactants generatng products would proceed
More informationElectrical double layer: revisit based on boundary conditions
Electrcal double layer: revst based on boundary condtons Jong U. Km Department of Electrcal and Computer Engneerng, Texas A&M Unversty College Staton, TX 77843-318, USA Abstract The electrcal double layer
More informationModule 3 LOSSY IMAGE COMPRESSION SYSTEMS. Version 2 ECE IIT, Kharagpur
Module 3 LOSSY IMAGE COMPRESSION SYSTEMS Verson ECE IIT, Kharagpur Lesson 6 Theory of Quantzaton Verson ECE IIT, Kharagpur Instructonal Objectves At the end of ths lesson, the students should be able to:
More information(Online First)A Lattice Boltzmann Scheme for Diffusion Equation in Spherical Coordinate
Internatonal Journal of Mathematcs and Systems Scence (018) Volume 1 do:10.494/jmss.v1.815 (Onlne Frst)A Lattce Boltzmann Scheme for Dffuson Equaton n Sphercal Coordnate Debabrata Datta 1 *, T K Pal 1
More informationStructure and Drive Paul A. Jensen Copyright July 20, 2003
Structure and Drve Paul A. Jensen Copyrght July 20, 2003 A system s made up of several operatons wth flow passng between them. The structure of the system descrbes the flow paths from nputs to outputs.
More informationDETERMINATION OF TEMPERATURE DISTRIBUTION FOR ANNULAR FINS WITH TEMPERATURE DEPENDENT THERMAL CONDUCTIVITY BY HPM
Ganj, Z. Z., et al.: Determnaton of Temperature Dstrbuton for S111 DETERMINATION OF TEMPERATURE DISTRIBUTION FOR ANNULAR FINS WITH TEMPERATURE DEPENDENT THERMAL CONDUCTIVITY BY HPM by Davood Domr GANJI
More informationEquation of State Modeling of Phase Equilibrium in the Low-Density Polyethylene Process
Equaton of State Modelng of Phase Equlbrum n the Low-Densty Polyethylene Process H. Orbey, C. P. Boks, and C. C. Chen Ind. Eng. Chem. Res. 1998, 37, 4481-4491 Yong Soo Km Thermodynamcs & Propertes Lab.
More informationLecture 8. Chapter 7. - Thermodynamic Web - Departure Functions - Review Equations of state (chapter 4, briefly)
Lecture 8 Chapter 5 - Thermodynamc Web - Departure Functons - Revew Equatons of state (chapter 4, brefly) Chapter 6 - Equlbrum (chemcal potental) * Pure Component * Mxtures Chapter 7 - Fugacty (chemcal
More informationy i x P vap 10 A T SOLUTION TO HOMEWORK #7 #Problem
SOLUTION TO HOMEWORK #7 #roblem 1 10.1-1 a. In order to solve ths problem, we need to know what happens at the bubble pont; at ths pont, the frst bubble s formed, so we can assume that all of the number
More informationPhysics 607 Exam 1. ( ) = 1, Γ( z +1) = zγ( z) x n e x2 dx = 1. e x2
Physcs 607 Exam 1 Please be well-organzed, and show all sgnfcant steps clearly n all problems. You are graded on your wor, so please do not just wrte down answers wth no explanaton! Do all your wor on
More information4.2 Chemical Driving Force
4.2. CHEMICL DRIVING FORCE 103 4.2 Chemcal Drvng Force second effect of a chemcal concentraton gradent on dffuson s to change the nature of the drvng force. Ths s because dffuson changes the bondng n a
More informationSolution Thermodynamics
CH2351 Chemcal Engneerng Thermodynamcs II Unt I, II www.msubbu.n Soluton Thermodynamcs www.msubbu.n Dr. M. Subramanan Assocate Professor Department of Chemcal Engneerng Sr Svasubramanya Nadar College of
More informationGlobal Sensitivity. Tuesday 20 th February, 2018
Global Senstvty Tuesday 2 th February, 28 ) Local Senstvty Most senstvty analyses [] are based on local estmates of senstvty, typcally by expandng the response n a Taylor seres about some specfc values
More informationUncertainty in measurements of power and energy on power networks
Uncertanty n measurements of power and energy on power networks E. Manov, N. Kolev Department of Measurement and Instrumentaton, Techncal Unversty Sofa, bul. Klment Ohrdsk No8, bl., 000 Sofa, Bulgara Tel./fax:
More informationThermodynamics II. Department of Chemical Engineering. Prof. Kim, Jong Hak
Thermodynamcs II Department of Chemcal Engneerng Prof. Km, Jong Hak Soluton Thermodynamcs : theory Obectve : lay the theoretcal foundaton for applcatons of thermodynamcs to gas mxture and lqud soluton
More informationDepartment of Physical Chemistry, Faculty of Chemistry, University of Bucharest, Bd. Regina Elisabeta 4-12, , Bucharest, Romania
ISOTHERMAL LIQUID-VAOR EQUILIBRIUM IN ACETONITRILE-WATER SYSTEM Rodca Vlcu, Zoca Cenuse abstact: The study of ths system started from the mportance that acetontrle has as the component of some mxtures
More informationPrediction of steady state input multiplicities for the reactive flash separation using reactioninvariant composition variables
Insttuto Tecnologco de Aguascalentes From the SelectedWorks of Adran Bonlla-Petrcolet 2 Predcton of steady state nput multplctes for the reactve flash separaton usng reactonnvarant composton varables Jose
More informationProcess Modeling. Improving or understanding chemical process operation is a major objective for developing a dynamic process model
Process Modelng Improvng or understandng chemcal process operaton s a major objectve for developng a dynamc process model Balance equatons Steady-state balance equatons mass or energy mass or energy enterng
More informationBasic concept of reactive flows. Basic concept of reactive flows Combustion Mixing and reaction in high viscous fluid Application of Chaos
Introducton to Toshhsa Ueda School of Scence for Open and Envronmental Systems Keo Unversty, Japan Combuston Mxng and reacton n hgh vscous flud Applcaton of Chaos Keo Unversty 1 Keo Unversty 2 What s reactve
More informationUncertainty and auto-correlation in. Measurement
Uncertanty and auto-correlaton n arxv:1707.03276v2 [physcs.data-an] 30 Dec 2017 Measurement Markus Schebl Federal Offce of Metrology and Surveyng (BEV), 1160 Venna, Austra E-mal: markus.schebl@bev.gv.at
More informationMODELING THE HIGH-PRESSURE BEHAVIOR OF BINARY MIXTURES OF CARBON DIOXIDE+ALKANOLS USING AN EXCESS FREE ENERGY MIXING RULE
Brazlan Journal of Chemcal Engneerng ISSN 0104-6632 Prnted n Brazl Vol. 21, No. 04, pp. 659-666, October - December 04 MODELING THE HIGH-PRESSURE BEHAVIOR OF BINARY MIXTURES OF CARBON DIOXIDE+ALKANOLS
More informationA PROCEDURE FOR SIMULATING THE NONLINEAR CONDUCTION HEAT TRANSFER IN A BODY WITH TEMPERATURE DEPENDENT THERMAL CONDUCTIVITY.
Proceedngs of the th Brazlan Congress of Thermal Scences and Engneerng -- ENCIT 006 Braz. Soc. of Mechancal Scences and Engneerng -- ABCM, Curtba, Brazl,- Dec. 5-8, 006 A PROCEDURE FOR SIMULATING THE NONLINEAR
More information#64. ΔS for Isothermal Mixing of Ideal Gases
#64 Carnot Heat Engne ΔS for Isothermal Mxng of Ideal Gases ds = S dt + S T V V S = P V T T V PV = nrt, P T ds = v T = nr V dv V nr V V = nrln V V = - nrln V V ΔS ΔS ΔS for Isothermal Mxng for Ideal Gases
More informationCOMPARISON OF SOME RELIABILITY CHARACTERISTICS BETWEEN REDUNDANT SYSTEMS REQUIRING SUPPORTING UNITS FOR THEIR OPERATIONS
Avalable onlne at http://sck.org J. Math. Comput. Sc. 3 (3), No., 6-3 ISSN: 97-537 COMPARISON OF SOME RELIABILITY CHARACTERISTICS BETWEEN REDUNDANT SYSTEMS REQUIRING SUPPORTING UNITS FOR THEIR OPERATIONS
More informationPhysics 5153 Classical Mechanics. D Alembert s Principle and The Lagrangian-1
P. Guterrez Physcs 5153 Classcal Mechancs D Alembert s Prncple and The Lagrangan 1 Introducton The prncple of vrtual work provdes a method of solvng problems of statc equlbrum wthout havng to consder the
More informationVapor-Liquid Equilibria for Water+Hydrochloric Acid+Magnesium Chloride and Water+Hydrochloric Acid+Calcium Chloride Systems at Atmospheric Pressure
Chnese J. Chem. Eng., 4() 76 80 (006) RESEARCH OES Vapor-Lqud Equlbra for Water+Hydrochlorc Acd+Magnesum Chlorde and Water+Hydrochlorc Acd+Calcum Chlorde Systems at Atmospherc Pressure ZHAG Yng( 张颖 ) and
More informationCHEMICAL REACTIONS AND DIFFUSION
CHEMICAL REACTIONS AND DIFFUSION A.K.A. NETWORK THERMODYNAMICS BACKGROUND Classcal thermodynamcs descrbes equlbrum states. Non-equlbrum thermodynamcs descrbes steady states. Network thermodynamcs descrbes
More informationCombustion and Flame
Combuston and Flame 159 (2012) 1693 1707 Contents lsts avalable at ScVerse ScenceDrect Combuston and Flame journal homepage: www.elsever.com/locate/combustflame Multphyscs modelng of carbon gasfcaton processes
More informationTHE IGNITION PARAMETER - A quantification of the probability of ignition
THE IGNITION PARAMETER - A quantfcaton of the probablty of ton INFUB9-2011 Topc: Modellng of fundamental processes Man author Nels Bjarne K. Rasmussen Dansh Gas Technology Centre (DGC) NBR@dgc.dk Co-author
More informationOutline. Unit Eight Calculations with Entropy. The Second Law. Second Law Notes. Uses of Entropy. Entropy is a Property.
Unt Eght Calculatons wth Entropy Mechancal Engneerng 370 Thermodynamcs Larry Caretto October 6, 010 Outlne Quz Seven Solutons Second law revew Goals for unt eght Usng entropy to calculate the maxmum work
More informationClassical binary nucleation theory applied to the real mixture n-nonane/methane at high pressures
Classcal bnary nucleaton theory appled to the real mxture n-nonane/methane at hgh pressures K. N. H. Loojmans, a) C. C. M. Lujten, G. C. J. Hofmans, and M. E. H. van Dongen Department of Appled Physcs,
More informationComputation of Phase Equilibrium and Phase Envelopes
Downloaded from orbt.dtu.dk on: Sep 24, 2018 Computaton of Phase Equlbrum and Phase Envelopes Rtschel, Tobas Kasper Skovborg; Jørgensen, John Bagterp Publcaton date: 2017 Document Verson Publsher's PDF,
More informationTHE EFFECT OF TORSIONAL RIGIDITY BETWEEN ELEMENTS ON FREE VIBRATIONS OF A TELESCOPIC HYDRAULIC CYLINDER SUBJECTED TO EULER S LOAD
Journal of Appled Mathematcs and Computatonal Mechancs 7, 6(3), 7- www.amcm.pcz.pl p-issn 99-9965 DOI:.75/jamcm.7.3. e-issn 353-588 THE EFFECT OF TORSIONAL RIGIDITY BETWEEN ELEMENTS ON FREE VIBRATIONS
More informationEstimation of the composition of the liquid and vapor streams exiting a flash unit with a supercritical component
Department of Energ oltecnco d Mlano Va Lambruschn - 05 MILANO Eercses of Fundamentals of Chemcal rocesses rof. Ganpero Gropp Eercse 8 Estmaton of the composton of the lqud and vapor streams etng a unt
More informationPART I: MULTIPLE CHOICE (32 questions, each multiple choice question has a 2-point value, 64 points total).
CHEMISTRY 123-07 Mdterm #2 answer key November 04, 2010 Statstcs: Average: 68 p (68%); Hghest: 91 p (91%); Lowest: 37 p (37%) Number of students performng at or above average: 58 (53%) Number of students
More informationand Statistical Mechanics Material Properties
Statstcal Mechancs and Materal Propertes By Kuno TAKAHASHI Tokyo Insttute of Technology, Tokyo 15-855, JAPA Phone/Fax +81-3-5734-3915 takahak@de.ttech.ac.jp http://www.de.ttech.ac.jp/~kt-lab/ Only for
More informationNormally, in one phase reservoir simulation we would deal with one of the following fluid systems:
TPG4160 Reservor Smulaton 2017 page 1 of 9 ONE-DIMENSIONAL, ONE-PHASE RESERVOIR SIMULATION Flud systems The term sngle phase apples to any system wth only one phase present n the reservor In some cases
More informationNON-CENTRAL 7-POINT FORMULA IN THE METHOD OF LINES FOR PARABOLIC AND BURGERS' EQUATIONS
IJRRAS 8 (3 September 011 www.arpapress.com/volumes/vol8issue3/ijrras_8_3_08.pdf NON-CENTRAL 7-POINT FORMULA IN THE METHOD OF LINES FOR PARABOLIC AND BURGERS' EQUATIONS H.O. Bakodah Dept. of Mathematc
More informationGrand canonical Monte Carlo simulations of bulk electrolytes and calcium channels
Grand canoncal Monte Carlo smulatons of bulk electrolytes and calcum channels Thess of Ph.D. dssertaton Prepared by: Attla Malascs M.Sc. n Chemstry Supervsor: Dr. Dezső Boda Unversty of Pannona Insttute
More informationPrinciples of Food and Bioprocess Engineering (FS 231) Solutions to Example Problems on Heat Transfer
Prncples of Food and Boprocess Engneerng (FS 31) Solutons to Example Problems on Heat Transfer 1. We start wth Fourer s law of heat conducton: Q = k A ( T/ x) Rearrangng, we get: Q/A = k ( T/ x) Here,
More informationLecture 5. Stoichiometry Dimensionless Parameters. Moshe Matalon N X. 00 i. i M i. i=1. i=1
Summer 23 Lecture 5 Stochometry Dmensonless Parameters Stochometry Gven the reacton M dn or n terms of the partal masses dm ( )W N X dn j j M we have seen that there s a relaton between the change n the
More informationCalculating the Quasi-static Pressures of Confined Explosions Considering Chemical Reactions under the Constant Entropy Assumption
Appled Mechancs and Materals Onlne: 202-04-20 ISS: 662-7482, ol. 64, pp 396-400 do:0.4028/www.scentfc.net/amm.64.396 202 Trans Tech Publcatons, Swtzerland Calculatng the Quas-statc Pressures of Confned
More information9 Derivation of Rate Equations from Single-Cell Conductance (Hodgkin-Huxley-like) Equations
Physcs 171/271 - Chapter 9R -Davd Klenfeld - Fall 2005 9 Dervaton of Rate Equatons from Sngle-Cell Conductance (Hodgkn-Huxley-lke) Equatons We consder a network of many neurons, each of whch obeys a set
More informationUniversity of Washington Department of Chemistry Chemistry 452/456 Summer Quarter 2014
Lecture 12 7/25/14 ERD: 7.1-7.5 Devoe: 8.1.1-8.1.2, 8.2.1-8.2.3, 8.4.1-8.4.3 Unversty o Washngton Department o Chemstry Chemstry 452/456 Summer Quarter 2014 A. Free Energy and Changes n Composton: The
More informationTensor Smooth Length for SPH Modelling of High Speed Impact
Tensor Smooth Length for SPH Modellng of Hgh Speed Impact Roman Cherepanov and Alexander Gerasmov Insttute of Appled mathematcs and mechancs, Tomsk State Unversty 634050, Lenna av. 36, Tomsk, Russa RCherepanov82@gmal.com,Ger@npmm.tsu.ru
More informationMass transfer in multi-component mixtures
Chapters -0 ex. 7, of 5 of boo See also Krshna & Wesselngh Chem. Eng. Sc. 5(6) 997 86-9 Mass transfer n mult-component mxtures Ron Zevenhoven Åbo Aadem Unversty Thermal and Flow Engneerng Laboratory tel.
More informationMathematical Preparations
1 Introducton Mathematcal Preparatons The theory of relatvty was developed to explan experments whch studed the propagaton of electromagnetc radaton n movng coordnate systems. Wthn expermental error the
More informationChapter 5. Solution of System of Linear Equations. Module No. 6. Solution of Inconsistent and Ill Conditioned Systems
Numercal Analyss by Dr. Anta Pal Assstant Professor Department of Mathematcs Natonal Insttute of Technology Durgapur Durgapur-713209 emal: anta.bue@gmal.com 1 . Chapter 5 Soluton of System of Lnear Equatons
More informationSuppose that there s a measured wndow of data fff k () ; :::; ff k g of a sze w, measured dscretely wth varable dscretzaton step. It s convenent to pl
RECURSIVE SPLINE INTERPOLATION METHOD FOR REAL TIME ENGINE CONTROL APPLICATIONS A. Stotsky Volvo Car Corporaton Engne Desgn and Development Dept. 97542, HA1N, SE- 405 31 Gothenburg Sweden. Emal: astotsky@volvocars.com
More informationMore metrics on cartesian products
More metrcs on cartesan products If (X, d ) are metrc spaces for 1 n, then n Secton II4 of the lecture notes we defned three metrcs on X whose underlyng topologes are the product topology The purpose of
More informationChapter Newton s Method
Chapter 9. Newton s Method After readng ths chapter, you should be able to:. Understand how Newton s method s dfferent from the Golden Secton Search method. Understand how Newton s method works 3. Solve
More informationInductance Calculation for Conductors of Arbitrary Shape
CRYO/02/028 Aprl 5, 2002 Inductance Calculaton for Conductors of Arbtrary Shape L. Bottura Dstrbuton: Internal Summary In ths note we descrbe a method for the numercal calculaton of nductances among conductors
More informationSystem in Weibull Distribution
Internatonal Matheatcal Foru 4 9 no. 9 94-95 Relablty Equvalence Factors of a Seres-Parallel Syste n Webull Dstrbuton M. A. El-Dacese Matheatcs Departent Faculty of Scence Tanta Unversty Tanta Egypt eldacese@yahoo.co
More informationAirflow and Contaminant Simulation with CONTAM
Arflow and Contamnant Smulaton wth CONTAM George Walton, NIST CHAMPS Developers Workshop Syracuse Unversty June 19, 2006 Network Analogy Electrc Ppe, Duct & Ar Wre Ppe, Duct, or Openng Juncton Juncton
More informationInvestigation of a New Monte Carlo Method for the Transitional Gas Flow
Investgaton of a New Monte Carlo Method for the Transtonal Gas Flow X. Luo and Chr. Day Karlsruhe Insttute of Technology(KIT) Insttute for Techncal Physcs 7602 Karlsruhe Germany Abstract. The Drect Smulaton
More informationV T for n & P = constant
Pchem 365: hermodynamcs -SUMMARY- Uwe Burghaus, Fargo, 5 9 Mnmum requrements for underneath of your pllow. However, wrte your own summary! You need to know the story behnd the equatons : Pressure : olume
More informationCinChE Problem-Solving Strategy Chapter 4 Development of a Mathematical Model. formulation. procedure
nhe roblem-solvng Strategy hapter 4 Transformaton rocess onceptual Model formulaton procedure Mathematcal Model The mathematcal model s an abstracton that represents the engneerng phenomena occurrng n
More informationLecture 12: Discrete Laplacian
Lecture 12: Dscrete Laplacan Scrbe: Tanye Lu Our goal s to come up wth a dscrete verson of Laplacan operator for trangulated surfaces, so that we can use t n practce to solve related problems We are mostly
More informationConsistency & Convergence
/9/007 CHE 374 Computatonal Methods n Engneerng Ordnary Dfferental Equatons Consstency, Convergence, Stablty, Stffness and Adaptve and Implct Methods ODE s n MATLAB, etc Consstency & Convergence Consstency
More informationRobert Eisberg Second edition CH 09 Multielectron atoms ground states and x-ray excitations
Quantum Physcs 量 理 Robert Esberg Second edton CH 09 Multelectron atoms ground states and x-ray exctatons 9-01 By gong through the procedure ndcated n the text, develop the tme-ndependent Schroednger equaton
More informationElectrochemical Equilibrium Electromotive Force
CHM465/865, 24-3, Lecture 5-7, 2 th Sep., 24 lectrochemcal qulbrum lectromotve Force Relaton between chemcal and electrc drvng forces lectrochemcal system at constant T and p: consder Gbbs free energy
More information