a. Prepare a graph showing P vs x1 and P vs y1 for T = 348.15 K (75 C)A B C

Acetonitrile (1) 14.2724 2945.47 -49.15Nitrometana (2) 14.2043 2972.64 -64.15

T= 348.15

4.42132977 83.2068575

3.73725775 41.9827049

x1 P Y183.2068575 41.9827049 0 41.9827049 083.2068575 41.9827049 0.1 46.1051202 0.1804720583.2068575 41.9827049 0.2 50.2275354 0.3313196983.2068575 41.9827049 0.3 54.3499507 0.459283983.2068575 41.9827049 0.4 58.472366 0.5692046683.2068575 41.9827049 0.5 62.5947812 0.6646469283.2068575 41.9827049 0.6 66.7171965 0.7482945583.2068575 41.9827049 0.7 70.8396117 0.8222066683.2068575 41.9827049 0.8 74.962027 0.88798941

ln P1 sat P1

sat

ln P2 sat P2 sat

P1 sat P2

sat

83.2068575 41.9827049 0.9 79.0844422 0.9469140883.2068575 41.9827049 1 83.2068575 1

P(kPa)0.6 450.6 59.740550.6 66.715220.6 80

SAAT TEKANAN KONSTAN 1 DAN Y = 0,659.74055 0.659.74055 0.43404425

SAAT TEKANAN KONSTAN 2 DAN X = 0,666.71522 0.666.71522 0.74829455

SAAT KOMPOSISI KONSTAN

X1=Y1

0 0.2 0.4 0.6 0.8 10

20

40

60

80

100

66.7152266.7152259.7405559.74055

45

80f(x) = 27.5642727987x^2 + 12.3648648575x + 42.5343636333R = 0.9988273488

f(x) = 41.224152519x + 41.9827049461R = 1

BUBBLE LINE Linear (BUBBLE LINE)DEW LINE Polynomial (DEW LINE)CONSTANT COMPOSITION COSTANT PRESSURE 1CONSTANT PRESSURE 2

X1,Y1

P(kPa)

Subcooled Liquid

a. Prepare a graph showing P vs x1 and P vs y1 for T = 348.15 K (75 C)

Keterangan :

y = 41.224x + 41.983dimana x= fraksi (X1 atau y1)

y= tekanan (P)jika, 0.6maka, P= 66.7174sehingga, 0.7482945497

jika, 0.6maka, P= 59.87604sehingga, 0.43404425

menggunakan persamaan bubble line:

X1=

Y1=

menggunakan persamaan dew line: y = 27.564x2 + 12.365x + 42.534

Y1=

X1=

b. Prepare graph showing t vs x1 dan t vs y1 for P=70kPaA B C

Acetonitrile (1) 14.2724 2945.47 -49.15Nitrometana (2) 14.2043 2972.64 -64.15

untuk P= 70 kPa ln 4.248495342.9946362.7336

T(K)362.7336 4.8795 131.5604 4.2485 70.0000 0.0000 0.0000

359.15 4.7709 118.0235 4.1276 62.0260 0.1424 0.2401355.15 4.6467 104.2384 3.9890 54.0031 0.3184 0.4742351.15 4.5192 91.7611 3.8467 46.8368 0.5156 0.6759347.15 4.3883 80.5012 3.7003 40.4583 0.7378 0.8484343.15 4.2538 70.3719 3.5497 34.8021 0.9895 0.9948

342.9946 4.2485 70.0001 3.5437 34.5960 1.0000 1.0000

SAAT KOMPOSISI KONSTAN SAAT TEKANAN KONSTAN 1 DAN Y = 0,6X1=Y1 T(K) 352.728 0.6

0.6 362.7336 352.728 0.43510.6 359.150.6 347.15 SAAT TEKANAN KONSTAN 2 DAN X = 0,60.6 343.15 349.572 0.6

T1 sat =T2 sat=

lnP1 P1sat lnP2 P2sat X1 Y1

0.6 342.9946 349.572 0.7473

dengan persamaan :

dimana

P1sat dan P2sat ditentukan dengan Antoine Equation

Iterasia' P2sat lnP2sat T (K) ln a a a'-a

1.971 44.229 3.789 349.5714 0.678555 1.971027 0.000

dimana

metode iterasi sama dengan di atas, tetapi menggunakan rumus T sebagai berikut

a P1sat lnP1sat T (K) ln a a a'-a1.948 96.534 4.570 352.728 0.66657751 1.948 0.000

Untuk T konstan pada x1 = 0,6 dan P = 70 kPa dievaluasi dari bubble line menggunakan metode iterasi.

Untuk T konstan pada y1 = 0,6 dan P = 70 kPa dievaluasi dari dew line menggunakan metode iterasi.

0 0.2 0.4 0.6 0.8 1 1.2330335340345350355360365

349.572349.572

352.728352.728

362.7336

343.15

f(x) = - 7.4256658694x^2 - 12.1465566483x + 362.6441485907R = 0.9997755086f(x) = 5.6348573683x^2 - 25.304189808x + 362.6850213964R = 0.9999664776

DEW LINE Polynomial (DEW LINE)BUBBLE LINE Polynomial (BUBBLE LINE)CONSTANT COMPOTITION CONSTANT TEMPERATURE 1CONSTANT TEMPERATURE 2

X1Y1

T(K)

0 0.2 0.4 0.6 0.8 1 1.2330335340345350355360365

349.572349.572

352.728352.728

362.7336

343.15

f(x) = - 7.4256658694x^2 - 12.1465566483x + 362.6441485907R = 0.9997755086f(x) = 5.6348573683x^2 - 25.304189808x + 362.6850213964R = 0.9999664776

DEW LINE Polynomial (DEW LINE)BUBBLE LINE Polynomial (BUBBLE LINE)CONSTANT COMPOTITION CONSTANT TEMPERATURE 1CONSTANT TEMPERATURE 2

X1Y1

T(K)

SAAT TEKANAN KONSTAN 1 DAN Y = 0,6

SAAT TEKANAN KONSTAN 2 DAN X = 0,6

jika:P= 70

X1= 0.6X2= 0.4

Jika :

87.18056

Y1= 0.747262

P= 70Y1= 0.6Y2= 0.4

X1= 0.435081

menggunakan metode iterasi.

P1 sat=

menggunakan metode iterasi.

1= a 2

1=(1 1 )/

1 = (1 )/1

0 0.2 0.4 0.6 0.8 1 1.2330335340345350355360365

349.572349.572

352.728352.728

362.7336

343.15

f(x) = - 7.4256658694x^2 - 12.1465566483x + 362.6441485907R = 0.9997755086f(x) = 5.6348573683x^2 - 25.304189808x + 362.6850213964R = 0.9999664776

DEW LINE Polynomial (DEW LINE)BUBBLE LINE Polynomial (BUBBLE LINE)CONSTANT COMPOTITION CONSTANT TEMPERATURE 1CONSTANT TEMPERATURE 2

X1Y1

T(K)

menggunakan persamaan bubble line:

dimana x= fraksi (X1 atau y1)y=suhu(T)

jika, 0.6maka, T= 352.678548sehingga, 0.74829455

menggunakan persamaan dew line:

jika, 0.6maka, T= 59.87604sehingga, 0.43404425

y= -7.4257x2 - 12.147x + 362.64

X1=

Y1=

y = 27.564x2 + 12.365x + 42.534Y1=

X1=0 0.2 0.4 0.6 0.8 1 1.2

330335340345350355360365

349.572349.572

352.728352.728

362.7336

343.15

f(x) = - 7.4256658694x^2 - 12.1465566483x + 362.6441485907R = 0.9997755086f(x) = 5.6348573683x^2 - 25.304189808x + 362.6850213964R = 0.9999664776

DEW LINE Polynomial (DEW LINE)BUBBLE LINE Polynomial (BUBBLE LINE)CONSTANT COMPOTITION CONSTANT TEMPERATURE 1CONSTANT TEMPERATURE 2

X1Y1

T(K)

species 1 Henry's Law x = fraksi liquid

species 2 water Raoult's Law y = fraksi vapour

sehingga,

diasumsikan bahwa fraksi CO2 dalam air adalah 0.010.010.99990 bar

0.01227 bar (steam table)

Antoine Equation T(K) = 283.15CO2 H2O P(bar)

A 6.81228 16.262 P(kPa)B 1301.679 3799.89C -3.494 -46.8

x1 x2= 2.1577079543 0.01 0.99= 8.6512857745 kPa= 0.0865128577 bar maka fraksi vapor CO2 hampir murni yaitu 0.9988= 0.1846147662= 1.202755009 kPa= 0.0120275501 bar

P1 0 0 990 1.000 0.000

0.6 0.4 0.4 594.00481 0.600 0.400

CO2

x1y1H1P2sat

H1H1

ln P 1satP 1sat

ln P 2sat

x1 y1 x2 x1 x2

0.5 0.5 0.5 495.00601 0.500 0.5000.4 0.6 0.6 396.00722 0.400 0.6000.3 0.7 0.7 297.00842 0.300 0.7000.2 0.8 0.8 198.00962 0.200 0.8000.1 0.9 0.9 99.010825 0.100 0.9000 1 1 0.0120276 0.000 1.000

0 0.2 0.4 0.6 0.8 1 1.20

200400600800

10001200

f(x) = 0.0120241122 exp( 10.2851802063 x )R = 0.9641783691

f(x) = 989.9879724499x + 0.0120275501R = 1

Chart Title

bubble lineLinear (bubble line)dew lineExponential (dew line)

Axis Title

Axis Title

99099000

P y1 x1 y2 y19.9121473 1 0.01 0.0012 0.9988

maka fraksi vapor CO2 hampir murni yaitu 0.9988

0.000 1.0000.000 1.000

y2 y1

0.000 1.0000.000 1.0000.000 1.0000.000 1.0000.000 1.0001.000 0.000

0 0.2 0.4 0.6 0.8 1 1.20

200400600800

10001200

f(x) = 0.0120241122 exp( 10.2851802063 x )R = 0.9641783691

f(x) = 989.9879724499x + 0.0120275501R = 1

Chart Title

bubble lineLinear (bubble line)dew lineExponential (dew line)

Axis Title

Axis Title

0 0.2 0.4 0.6 0.8 1 1.20

200400600800

10001200

f(x) = 352.2492122925 exp( -10.2851802063 x )R = 0.9641783691

f(x) = - 989.9879724499x + 990R = 1

Chart Title

bubble lineLinear (bubble line)dew lineExponential (dew line)

Axis Title

Axis Title

0 0.2 0.4 0.6 0.8 1 1.20

200400600800

10001200

f(x) = 352.2492122925 exp( -10.2851802063 x )R = 0.9641783691

f(x) = - 989.9879724499x + 990R = 1

Chart Title

bubble lineLinear (bubble line)dew lineExponential (dew line)

Axis Title

Axis Title

10.1a10.1b10.210.3a