CHME_4040_Exam_2_Solutions_Fall_2011

CHME_4040_Exam_2_Solutions_Fall_2011 - fol/VT The number of...

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Unformatted text preview: fol/VT The number of stages if the M111ph1ee efficiency based on the vap01 11. Problem I) (50 points) We are usin a distillation column with a altia] condenset and diiect steam g E13 M injection into the 1eboile1 to separate ethanol £10111 watei The distillation W column IS used to process two feed stleams at Feed 1:85 kgmole/hi of 21 5 and a binaly equ111b11um dlagtam IS given in Figure 1). The bottoms product is a satugaged liquid and has a mole fraction of XB=0. 04, and the distillate yflfii (both mole fractions ethanol, with ethanol being the more volatile component). The 1eboiie1' direct steam is a saturated yapqr with a flow late of 3£i_ lggmole/hr Constant molal overflow can be assumed. The reflux (R) at the top of the column is set at 2.56 the minimum 1'.eflux The heat of vaporization is 1125 kJ/kgmole for the composiTtiTi'mT—The condenser C6? t111Ct—a flow chalt 111111115 distillation column and determine the . following (assuming constant molal ovetwflow) 9N3 “1)Allexte1nal flow rates and compositions. 9, T5 Li [LN '93, 4‘; 99111. To /7 n59: ----- 2 The minimum and actual1eflux 1n fhe condenser {11; W"? K1111. Q TOT“) 1,110an El T351” T Fdfld (lmhfbi [km 90} ”T 3) All 1nte1nal flow lates 11, V L V 1 L V A '1 T f” " ' N6 1?]: l/ .11..» NoTHT ; . 0&3 3") The heat duty 1n the condense1.FM Lil/l F011- 7 17 In!" £5 1 1‘1 11ng On Figure l const1uct all 111;qu i1911aterype1at1ng lines and Q lines. g“ Lth Q [Jr/to}: F0117 TH 1011,1111??? 2" ‘. . {10111149 The number of stages and optimum location of the two feed streams. (1;, we ital/L. TIP OZ \ 2" haseis65% “A” 1? we % If the steam used in the reboiler had been contaminated with trace ethanoi to make a steam with a mole fraction of 0.02 ethanol where would the bottom operating line end and why (do not1'egwalg11'lateanything here, just give the point coordinates and explain). [l ST 1749:}? A) Ti (C) ’0? 0 02) z. 5" are 1+ Wear/1M7 "5) 2,.) {ROM FIWlflii RMM. SLOW—E; £0323“: FEM "' 623%, "' 8X5 3 D331) “r BX?) laws" + 4,2, .2: me) 4— (’21‘1rb>0.0‘4 E30. z’aS’ :: 0.8km + 3W5. (dab/D W.s’)€§"‘: 0.90 WWW?! M ”£30 101000) L’ w + 0.8(100)HL5 W I h ,..m,..» A U*-%fi a? 9+(pgx;:vl 769 '250 + 0(4) 3255 l: \7 4» 0,4[393 83’19‘7 -Mu-1wwm th{a?3§7 {Etiiiqu 5) 3 6.6. e—12emm (0 a”? m Tmmé, ; 9‘ 9) “’“‘ ’8 S’mgn-mt (Q , r: 5 (33> "190m?" fl“) (amt/l (9,01) TH 313 190 TM Ty ”TS F01?“ “TI-“Hi m) i) TIM 3T“ Eli-W1 FROEMQT 77%,. W5 Q IN 6, EN '7‘" iii? aim/G, g 7% £5 AM. Pam/u 7’" /,,~7777§ R I; fidetifL Lfifidtnkg :ET. Figure 2: Equilibrium Data for Ethanol-Water at 101.43 kPa . EIHIEEIIIIIIIII'IIIIIII'II‘ I.II.IIIIII‘ll-i..-ilmlllllIIIIIII'IRIIIIIIIIIIII II.IIIIIII!!‘:‘Ill-ill W.- .IIIIIII'I'IIIEIIIIIEIE illilil'lllglilll" I‘mlmllillllllllllilIlii'l , "manll‘lill'llllllil'll: I'I'IIII'IIIII‘IIIIII'II I'lllllllll-i—Ililililill AIIIIII'IIIII..IIIII'II .I'lillal‘lllligj'llill “E‘IIHIIIIIII'IIII' I'lllli'lligflilifili'lll-II' Flliglll'lilllllilllI I.Hilligai‘mfimmfllllllllllm IEEFAMIWIIEEWIIIII." cams E noun—Eu. .295 h 0.10 0.20 0.30 0.40 0.50 0.60 0.70 0.80 0.90 1.00 0.00 x (mole fraction in liquid) 1073 j . Problem 2) (40 points) A distillation column' IS used to process a feed stream at 1 atm. (250 kgmole/h1 of 40 mole % propane, 33 % saturated liquid). (note: a binary equilib1ium diagram 18 given in Figure 1). A total condenser and a partial reboilel are employed 111 this system. The distillation towe1 has two exiting streams, a distillate product (11D: 0. 96) and a bottoms p10duct The reflux ratio in the condenser isset equal to 3. 5. The vapm flow rate e11te1ingthe total condenser at the top of the column is 440. 2 kg mole/h1zA cooling coil- is placed 111 the 0011111111 1n such a way that 47% of the vapm ieaving the fast actual tiay from the bettom (not including the pai t1a1 reboiler)‘ 1s condensed. Construct a flow chart foi this distillation column and determine the following (assuming constant molal ove1 flow) / > s ‘111'1—r-itb’egem 1) All exteinal flow 1ates and compositions. 1,: . , 1h €01 their its; Zplscfidfis 2) All internal flow rates L— , L 1" V L, V 3) The minimum number of stages. i‘” (f’ [33‘ _ ' <2 «'3 Fa its; TEL“; 11 i” 11mm 1 icrccii' Jill" $5 ‘ :31 three" 33' i“ 4) On Figuie 1 construct alljp101§11ate opeiating lines and lines fotTh‘“ fie 111 no Mic}... L“ . actuaiieflux condition Li 1,1147; 1ft) $116,125 J at .l 1 11 WT“. T 1 - K 3 P 13f 5) The number of stages and optimum location of the feed stream M517" '1- 6 £111 #3 {31-1 mi eastid'x of: “es at goal» usii V : .' . . . ”Tit get! . ‘ F T 1"” 1 i“ i 11:11 " £1th * ” 1” . _ , . ) f 131 hum—k ‘97“ L, _flf’ gaff} '(yefiéi 7/ t? 5 11-110!“ ' ‘ T” ”’1: ”if” Tim @1111 1111 F: D *- 3 FZF 2‘ DMD +BXB 19’) 9E8?“ " ‘3 286(0-‘0 : 272624022) 2— 1452.!ng @ “TO 2 $3.?! 4» 115212-223 £20343 £332] EM '1 f' “R K‘VL PL 02A: RAJVQJ S: F.) . ' 2 2W WV v: 218. ' a. \/ 2%)?) J, U] 2 (Mai: 322.38 {0.331250% LJ v’ (NJXNJ LIL/0 7: @2522] J V’ J L1 .1- (9,412- \7 = C V v’ : \7 0 212v (/2222; 2621287253) .2 J: 222 2 « 0‘53 V JV 5: 51> 2 ' 5‘5"“ 3': P 'f E: ”7:2:ij 1Q 0, 7‘???“ I7} KQTAQJE (0 (’24) I 0.9(11) OgULNfa «:27 SLOPE, : :22, 2 2% (A “02,93 is! $01 1 U @2255 7742024911: (0,21, and!) A ' f 5’1'J2'F9PLN6, 51;“ VlgVJ I L? 38! l 2: B‘LLM CON'QEJJSI’lg/I’L7 .CjLUfli” V13 «r “3%, in“; I. 1% r V fl’mfis "Wraomm (0.014102%) STfl'fiPPINCQ ’3‘832’0‘08, .53 SLGENZ 2: 1:..— “A LLB/gt?) Cam D 17-2 “’22??fo V l UN Equilibrium Data for Propane-Butane at10‘i.43 kPa Allii‘lllllllillli"I'llllll EIIEIIIV IIHIIIIIIIII'I:IIE.IIIII Illa'lllll'aillglil Ew-llllllilillilll'llllll lllllllllllllfiiflflflflfilli flllllllllllllllllllllllll Illllllllilfifimflllllfiill r Alllilfl1llflfl IIIEIISIIV llllllllllllllllllll Allllllinll A EJ!I5IIH'IIV IEIIIIIIIIIII I‘IIIIIll-III!III.‘IIIIVAIIHMKIWIHI'EEIIIIIII.III I'lllllllllllllilllllllfiy AlIl-fl I'flllm IIIIIII‘II' IIIEIIIIIIIIIIIIIIIIIIHHW ‘IIIHIIHI .‘ll'....lll'llllll..'lll! EOBOE 29.: 0223 Long a 0.10 0.20 0.30 0.40 0.50 0.60 0.70 0.80 0.90 1.00 0.00 x (liquid phase mole fraction) ...
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