Therm

odynamics

Mollier plots of tw

o imaginary gas m

ixes created by means of our com

puter programs.

One visualizes gas behavior at extrem

ely high pressures, the other illustrates propertiesof another gas m

ix at very low tem

peratures.

~l 16

i 28 i 32 1 36

~g~ I-

CR

IGG

EN

I C M

IXT

UR

EM

l'LE F

RA

CT

JON

OF

CO

MP

ON

EN

TS

ME

TH

AN

E 0.9000 IS

l'PE

NT

RN

EETHANE 0.0529 N-PENTANE

PRClPANE 0.0200 N-HEXANE

ISDBUTANE 0.0030 NITROGEN

N-BUTANE 0.0030 C DIOXIDE

0.0005O

. OD

DS

O. 0001

0.01000.0100

~ t-

TE

MP

ER

AT

UR

E-D

EG

. FA

HA

PRE

SSUA

E-P5IA

g~~~ggg~~

~~g~o!~rg~~

/"v/

--g

~"

~g'¡.it:J.Z

41.%

3M-BTU/LB OEG. FAHA

i 60 1611 168

-,,~~/C

if.. //0 %: §;

M? ~

-80 AV //Ô ~

~;:/V

1.60 l,t4 J.£û

5M.-BTU/LB DEe. FRHP. -40/

I 721 '"

2 00204

g ~ ;ZV

. ~~

/-20o ~ un~7-

o ~Jk7kn/~~o #/ '£/~7~

0~;7HØ

;0~/'~~ /~Vh

-2 ~ ~b~/ ó-/l?-~

'ih////20~~ /Á/?

~r140~~

_.all

, 08

65 2'"gN'""N~~~~~~g"-~~g~g~~g J,g ~~,'"rgg~g"g~~~~~~~ggg~g

('.1"

~..-'l.ijlJ i.L1a i.S2 i.S6 1.60 1.6L1

~'"

--~grr~fg~

~~~~~g~gg~~g~g~g~g~""'.35

l.66 i.72

i.76 SMi~~JU/LB1.~~G. F~~8~

1.961.92

MO

LE F

RA

CT

i ON

OF

Cl'H

Pl'N

EN

TS

METHANE 0.7600 N-PENTANE

ETHYLENE 0.0020 N-HEXRNE

ETHANE 0.1200 N-HEPTANE

PRljPRNE 0.0600 NlTRljGEN

N-B

UT

AN

E 0.0200 C

DIljX

IDE

0.00500.00200.00100.02000.0100

TE

MP

EA

AT

UR

E-O

EG

. FA

HR

PRE

SSUA

E-PS I R

oo~ ~~I-W-ij) )40

" ~1j~~77/IJ" m

"'0 - . ~ l!HlV

1Z /fP7/271-l ls

" /1/4b0t01ß~~~~ L¡ioo

3S ii j¡1l~12M~~Pí~:27

,,, Ii/I¡ 7iVi¡ø~~ ¿iw

;lsoo/Î I~

~~

~~

~~

00 ~û 00

27ì/~/í:i11~

~ ~

i?qso"L/ / J-I//~h20!/0~ij /12

1/ /77/ 1////1 ,;~/17/?A/7/ /.-o

i/1:7jØ~~~W

trr~" ~j/1~~~0~ ~

"0,;0~~

~W

-,,/~%0~~ ~

1~~0ø¡l( ~

a¡0 00., 0

lE ~

~ '"

1.1111i.IIB

2.12i.611

1.76 L.B

O l.a4 l.aa

5M-BTU/LB DEG. FRHR

2.00

2.~~~~~~~~g~

~~

~:'"or~~

2.242.'~

66

Calculation methods

The calculation procedures on thefollowing pages apply to "straight"compression-the compression of acertain gas from a given suction pres-sure to a desired discharge pressure.The methods outlined are:1. The "N" method (so namedbecause of the extensive use of thepolytropic exponent "n"). It is useda. when the fluid to be compressedclosely approximates a "perfect"gas (air, nitrogen, oxygen, hydrogen).b. when a chart of the properties ofthe gas or gas mixture is not available.2. The "Mollier" method which in-volves use of a Mollier diagram andis used whenever a plot of the prop-erties of the fluid being compressedis available.

Symbols and subscripts

cp Specific heat at con- TR Reduced temperaturestant pressure (T/Te)

cv Specific heat at con- Temperature (OF)stant volume v Specific volume (cu. ft.

H Head (ft. lb. per lb.) per lb.)h Enthalpy (BTU per lb.) w Weight flow (lb. perk Adiabatic exponent (cp/cv) min.)

Mcp Molal specific heat at X Temperature rise factorconstant pressure Z Compressibility factor

MW Molecular weight GHP Gas Horsepowern Polytropic exponent BHP Brake or Shaft Horse-

PR Reduced pressure power(PIPe) r¡ Efficiency

p Pressure (psia)

Pe Critical pressure (psia)Subscripts0 Capacity (cfm)

R Gas constant(1544/MW) ad Adiabatic process (Had)

r Pressure ratio (P2/p1) p Polytropic process (Hp)

s Entropy (BTU per lb. S Standard conditions-per °Rankine) usually 14.7 psia,

T Absolute temperature 60°F, dry (Os)(ORankine=oF+459.6) 1 Inlet conditions (P1) (01) (t1)

Te Critical temperature 2 Discharge conditions(ORankine) (T 2) (P2) (Ì2)

69

,-~-. 7'-' ~- - =

Compressor calculation,by the "N" method

STEP 1:If a pure gas, begin with Step 2, If a mixed gas, calculate mixture properties as follows (see Table 1, Page 71):

~f¡4i ,. ..

(1) (2) (3) (5) (6) (7) (8) (9) (10) (11)Gas Mol % Mols/HR Mol Wi. Tc Pc MCn .. ~Mixture each gas each gas (Table 1) (1) x (3) Weight % (Table 1) (Table 1) (1) x (6) (1) x (7) (Table 1) (1) X(10J

,.. . ... . a a/dX100 . . , . ... . ... . ... .

... . ... . b b/dX100 ... . " . . . .. ... . . . c c/dX100 '" . . . . .- - -- -

d ... .- MeR Mix I

- - - -LCalculate k (Mixture) = Apparent Tc Mix Pc Mix MCn MixM'£n_riIX-1.99, Mol Wi. of

Mixture

-

STEP 2: Calculate Inlet Flow (01)Mols/hrXMol Wt01 = V1 Xw w 60 (Ib/min)

ZlRT1 1544Vl = 144 Pi R = MWZl-assume to be 1, or use Chart 1, Page 72

Pi T1If using Chart 1- PR1 =-p T R1 = l-c cSTEP 3: Select Compressor FrameGiven Inlet Volume (01) use Table 2, Page 71 (approx,Dimensions and Weights are listed on Pages 33 and34).

STEP 4: Calculate Average Compressibility(Zavg. )

Zl+Z2IZavg = -r- ,

Zl from Step 2 Z2 as follows:X

*T2'(approx.) = r¡- (Til+T1ad

From Chart 2, Page 72, find X (temperature rise factor)and r¡ad (using pressure ratio (r) as given, k from Step

1 or Table 1, r¡p from Table 2).Then calculate Z2 (as in Step 2, using Chart 1) usingP2 (given) and T2 as calculated.

STEP 5: Calculate Polytropic Head (Hp)**Using Chart 3, in the foldout, determine Hp/Zavg

Multiply by ZavQ to obtain Head.

Or, for greater accuracy:Zava R T1

H =p

n-1n

n-1nk-1

= k(T))

L p 2.' J- n -1P1

T) from Table 2

70

STEP 6: Find number of Stages requiredFirst, from Chart 4, Page 74, find maximum permis-sible head per stage.

_ Hp (Step 5)Stages - Max. Head per Stage

i- If Max. Head per Stage from Chart 4 JL is over 12,000 ft, use 12,000 ft

STEP 7: Find Speed required

. ~ HpSpeed = Nominal Speed 12,000XNo. of Stages

Nominal Speed from Table 2 (at 10,000 or 12,000 fthead depending on impeller selected).

STEP 8: Find Shaft Horsepower requiredTotal HP = Gas HP+Bearing and Oil Seal Losses

wXHpGas HP = r¡pX33000 '"

Determine losses from Chart 5, Page 74, based ontype of seal selected (see Page 18 for discussionof seals).

STEP 9: Find actual Discharge Temperature(h)

t2 =Hp

R ( k~ 1) r¡p

+t1

Zavg.

STEP 10: Calculate Discharge Flow (02)

Pl T 2 Z202 = 01 X P2 X T1 X Zl 'I

*This approximate T 2 may differ slightly from actual dischargetemperature since the effect of compressibility upon tempera-ture rise has not yet been considered.

**Adiabatic head may be calculated by using 100% efficiency lineon Chart 3.

4t- ~ 7l~ ~P;j - i)

.~

Compressor calculationby the Mollier method

Refer to the simplified Mollier diagram (below).

STEP 1: Find Inlet Flow (Od01 = V1 X w

Locate Inlet State Point (1) at intersection of P1 andt, Read V1 by interpolating between specific volume(v),lines.

STEP 2: Select ComPressor FrameGiven Inlet Flow (01) use Table 2, Page 71, (Dimen-sions & Weights are listed on ,Pages 33 and 34.)

STEP 3: Find Adiabatic Head (Had)Read Inlet Enthalpy (hd directly below (1). From (1),follow line of constant Entropy (s) to discharge pres-sure (P2), locating Adiabatic Discharge State Point(2ad). Read Adiabatic Enthalpy. (h2ad) directly below(2ad).

ßhad = h2ad ~ h1 (Btu per lb.)Conversion factor: 778 ft. Ib./BTUHad = ßhad X 778

STEP 4: Find Polytropic Head (Hp)

H = Had X TJpp TJadFind k from Table 1 ,Page 71

Calculate Pressure Ratio, r = P2/P1

Find TJp from Table 2 and use Chart 6, Page 75, to

find TJad

STEP 5: Find Number of Stages requiredFirst, from Chart 4, Page 74, find maximum permis-sible head per stage.

CRITICAL POINT

_ Hp (Step 4)Stages - Max. Head per Stage

If Max. Head per Stage from Chart 4i? over 12,000 ft., use 12,000 ft.

STEP.6:Find Speed Required. I HpSpeed = Nominal Speed~12,000 X No. of Stages

Nominal Speed from Table 2 (at 12,000 ft. head)

STEP 7: Find Shaft Horsepower RequiredTotal HP = Gas HP + Bearing & Oil Seal Losses

w X HpGas HP = % X 33000

Determine losses from Chart 5, Page 74, based ontype of seal selected. (See Page 18 for discussion ofseals).

STEP 8: Find Actual Discharge Enthalpy (h2)ßhad

h2 = -TJ + h1ad

Had from Step 3; TJad from Step 4

STEP 9: Find Discharge Temperature (t2)and Specific Volume (V2)

On Mollier, plot vertically from h2 (Step 8) to P2. ReadÌ2 and V2.

STEP 10: Find Discharge Flow (02)02 = w X V2

v

0c V

0Z

'" UlD. -li-w zII -l:: v -cUl 0Ulw rII ca. :;

v rrrZrrUl

v

ENTHALPY (BTU per LB) hi

i: Ahad ~r75

Chart 1

Table 1 G

as Properties(M

ost values taken from N

atural Gas Processors Suppliers A

ssociation Engineering D

ata Book-(1972. N

inth Edition)C

ritical Conditions

*Mcp

Hydrocarbon

Chem

icalM

olecularSpecific Heat Ratio

Gas or V

aporR

eference Sym

bolsForm

ulaW

eightk =

cp/cvPressure

Tem

peratureat 60F

Pc (psia)Tc (OR)

at 50Fat 300F

Acetylene

C2=

C2H

226.04

1.24905

55710.22

12.21A

irN

2+02

28.971.40

547239

6.957.04

Am

monia

NH

317.03

1.311657

7318.36

9.45A

rgonA

39.941.66

705272

4.974.97

Benzene

C6H

678.11

1.12714

101318.43

28.17Iso-B

utaneiC

4C

4H,o

58.121.10

529735

22.1031.11

n-Butane

nC4

C4H

,o58.12

1.09551

76622.83

31.09Iso-B

utyleneiC

4=C

4H6

56.101.10

580753

20.4427.61

Butylene

nC4

C4H

B56.10

1.11583

75620.45

27.64C

arbon Dioxide

CO

244.01

1.301073

5488.71

10.05C

arbon Monoxide

CO

28.011.40

510242

6967.03

Carbureted W

ater Gas (1)

-19.48

1.35454

2357.60

8.33

Chlorine

CI2

70.911.36

1119751

8.448.52

Coke O

ven Gas (1)

-10.71

1.35407

1977.69

8.44n-D

ecanenC

ioCioH 22

142.281.03

3201115

53.6774.27

Ethane

C2

C2H

630.07

1.19708

55012.13

16.33E

thyl Alcohol

C2H

5OH

46.071.13

927930

1721

Ethyl C

hlorideC

2H4C

I64.52

1.19764

829.

14.518

Ethylene

C2-

C2H

428.05

1.24742

51010.02

13.41F

lue Gas (1)

30.001.38

563264

7.237.50

Helium

He

4.001.66

339

4.974.97

n-Heptane

nC,

C,H

'6100.20

1.05397

97339.52

53.31n-H

exanenC

6C

6H'4

86.171.06

440915

33.8745.88

Hydrogen

H2

2.021.41

18860

6.866.98

Hydrogen Sulphide

H2S

34.081.32

1306673

8.098.54

Methane

CC

H4

16.041.31

673344

8.3810.25

Methyl Alcohol

CH

30H32.04

1.201157

92410.5

14.7M

ethyl Chloride

CH

3CI

50.491.20

968750

11.012.4

Natural G

as (1)-

18.821.27

675379

8.4010.02

Nitrogen

N2

28.021.40

492228

6.967.03

n-Nonane

nCg

CgH

20128.25

1.04345

107348.44

67.04Iso-Pentane

iC5

C5H

I272.15

1.08483

83027.59

38.70n-Pentane

nC5

C5H

'272.15

1.07489

84728.27

38.4 7

PentyleneC

5-C

5H1O

70.131.08

586854.

25.0834.46

n-Octane

nCB

CB

H'B

114.221.05

3621025

43.359.90

Oxygen

O2

32.001.40

730278

6.997.24

PropaneC

3C

3HB

44.091.13

617666

16.8223.57

Propylene.C

3-C

3H6

42.081.15

668658

14.7519.91

Blast F

urnace Gas (1)

-296

1.39-

-7.18

7.40C

at Cracker G

as (1)-

28.831.20

674515

11.315.00

Sulphur Dioxide

S0264.06

1.241142

7759.14

9.79W

ater Vapor

H2O

18.021.33

32081166

7.988.23

N)0f- 0.80:ïai(f(fwa:a.::au 0.70

Chart 2

(1) Approxim

ate values based on average composition.

'Use straight line interpolation or extrapolation to approxim

ate Mcp at actuai inlet T

. (For greater accuracy, average T should be used.)

Table 2 E

llot Com

pressor SpecificationsS

peed at*Normal Flow

**Nom

inal PolytropicN

ominal Polytropic

+Nominal Max.

Nom

inalR

angeH

ead per StageE

ffciencyN

o. ofPolytropic

Frame

(icfm)

(Hp)

T)p

StagesH

ead/Stage

29M500e

8,00010,000

.7610

11,50038M

6,000- 23,000

10,000/12,000.77

98,100

46M20,000- 35,000

10,000/12,000.77

96,400

60M30,000- 58,000

10,000/12,000.77

85,000

70M50,000- 85,000

10,000/12,000.78

84,100

88M75,000-130,000

10,000/12,000.78

83,300

103M110,000-160,000

10,000.78

72,800

110M140,000-190,000

10,000.78

72,600

25MB

(H) (H

H)

500-5,000

12,000.76

1211,500

32MB

(H) (H

H)

5,000- 10,000

12,000.78

1010,200

38MB

(H)

8,000- 23,000

10,000/12,000.78

98,100

46MB

20,000- 35,000

10,000/12,000.78

96,400

60MB

30,000- 58,000

10,000/12,000.78

85,000

70MB

50,000- 85,000

10,000/12,000.78

84,100

88MB

75,000-130,00010,000/12,000

.788

3,300

*Maxím

um flow

capacity is reduced in direct proportion to speed reduction."U

se either 1 0,000 It or 12,000 It for each impeller w

here this option is mentioned.

+A

t reduced speed, impeliers can be added.

7172

1.05

\~::

\" t:

F: ::--i-

:: -r-

r--I---

--:

r--

-i-

--~

~;. ..

..~t-. -.

:-t:--

::::r-

¡---

-J-

-""0.

:...-

::f: r-

-r-i-

..r-t:

::¡-

--

\.6'S

....

t'-

I--¡-

--..

..-

--.¡ ~

....

....

¡.¡-

i-r-

r,. ;.

I....

.¡ ~(..

.. II..

....

..¡...

......

Ì's1'..

.... ..r-

I-....¡-

..i-

¡-r-

....

....

I~,..

..i'

I-..

¡...

I.~c

"r-

"-..

....Ì"

"-~

i'"-

""l"

..i

"-"

"-,,'"

Ì'..

..I'

~,

i' ,

"""

..I

.~

""Ì'

"i

'l~Ì'

i'"

I

0"

'\

'\Ì\

"-I

'\

~.À

\\

-P"

IC

?\

I\

II\

Ii\

I\

I,

1.00

0.90

0.60

0.50o

0.20 0.30

RE

DU

CE

D P

RE

SS

UR

E (P

R)

0.400.50

0.60 0.70 0.80 0.90

0.10

1.50

PO

LYT

RO

PIC

EF

FIC

IEN

CY

(1\, )66 68 70 72 74 76 78 80 82 84 86 88

1.40o

1.30f.

1.20o

1.10.-l

1.00~'!

0.90~.'+

-\"

o.ii;'r:

,t,t,n

.915\J!

60 65 70 A' 75 80

AD

IAB

AT

IC E

FF

ICIE

NC

Y ('lad)

8555

5.003.00

2.00

1.60

1.40

1.30 ~f-w1.20

a:::f--i1.15

0:Wa.::w1.10

f-awu::awa:1.05

1.00

90

í

Calculate the E

lliott compressor required to handle a process gas at the follow

ing operating conditions:Inlet tem

perature (td = 40F. Inlet pressure (pd =

20 psia / Discharge pressure (P2) =

100 psiaG

as conditions: 2378 mols/hour of m

ixture of Propane (95%), B

utane (3%) and E

thane (2%) (by volum

eor m

ol percentage).

STE

P 1: Calculate G

as Mixture Properties

(2)(5)

(1)M

ols/HR

(3)(4)

Weight %

(6)(7)

(8)(9)

(10)(11)

Gas

Mol %

(Mol %

MoIW

L.

1(4)+44.241

Tc

PcM

e"M

ixtureeaeh gas

X2378)

(Table 1 )

(1) X (3)

X100

(Table 1)

(Table 1)

(1) x (6)

(1) x (7)

(Table 1)

(1)X (10)

Propane95%

22594409

41.994.71%

666617

632.7586.5

16.5515.72

Butane

3%71

58.121.74

393%766

55123.0

16.522.5

0.675E

thane2%

4830.07

0.60136%

550708

11.014.2

11.960.239

--

---

--

---

237844.24

666.7617.2

- 16.634-

---

Apparent

T, M

ixPc M

ixMe" Mix

16.63M

oIWL

. ofk (M

ixture) = 16.63

1.99 = 1.137

Mixture

ST

EP

2: Calculate Inlet F

low (O

d2378 x 44.24

weight flow

(w) =

60 = 1753 Ib./m

in.20 40 + 460

PR

1 = 617.2 =

.0324 T R

i = 666.7 =

.75

From C

hart 1 Zl .971544 (40 +

460)V

l = .97 X

44.24 X 144 X

20 = 5.88

01 = 5.88 X 1753 = 10310 icfm

STE

P 3: Select Com

pressor Frame

From

Table 2, the sm

allest compressor fram

e capableof handling this flow

(10310 icfm) is Fram

e 38M.

Note that this is a horizontally-split m

achine; avail-able up to 9 stages; average polytropic efficiency77%

;8100 rpm at 12000 ft. head per stage.

Approxim

ate Dim

ensions and Weights are show

non Page 33. .

ST

EP

4: Calculate A

verage Com

pressibilityP2 100

r (pressure ratio) p; = 20 =

5k = 1.137 (Step 1) 1Jp = 0.77 (Table 2)

From Chart 2 X = 0.21 1Jad = 0.748

0.21 (40+460)

T2 (approx) =

0.748 +(40+

460) = 640.5 R

T2 640.5 P2 100

TR2=Tc =666.7=0.961 PR2=Pc =617.2=0.162

From

Chart 1, Z

2 = 0.93

Zl + Z2

Zavg = 2

.97 + .93

2 = .95

ST

EP

5: Calculate P

olytropic Head (H

p)From

Chart 3, in foldout-know

ingk (Step 1) = 1.137 1Jp (Table 2) = .77

¡- (p2/pd = 5 Mol wt. mix (Step 1) = 44.24

t1 (OF

) = 40

HY =

32000 Zavg =

.95H

p = 30400 ft.

~i

Or, m

ore accurately, from the equations:

n-1 1.137-1

-i = 1.137 X.77 = 0.1566

1544 (40+460)

Hp=

.95X44.24X

.1566 X(51566-1)=

30350ft.

STEP 6: Find Number of Stages

requiredFrom

Chart 4 (know

ing moL

. wt. of m

ix, k1 and tdM

ax Head per S

tage = 10080 ft.

30400N

o. of stages = 10080 =

3.03 or 4 stages

ST

EP

7: Find S

peed required30400

Speed =

8180 10000 X 4 =

7135 rpm

(10000 ft. impellers have been selected.)

STE

P 8: Find Shaft Horsepow

er required1753 X

30400G

as HP =

.77 X 33000 =

2100 hp

Bearing and O

il Seal Loss (from

Chart 5) and as-

suming Iso-C

arbon Seals, for F

rame 38M

com-

pressor = 56 hp

Shaft HP =

2100 + 56 =

2156 hp

STE

P 9: Find Actual D

ischargeT

emperature (t2)

304001544 I 1.137) +40=183.5 F

.95 X

44.24

\1.137-1 X.77

t2 =

ST

EP

10: Calculate D

ischarge Flow

(02)20 179+

460 .9302 =

1031 OX

100 X 40+

460 X m

=2545 cfm

73

Chart 4o

-i00-i'O

OO

MAXIMUM HEAD PER STAGE

'0000r.00

~00

0,'0~O

O,0,

o1'/0

00r.~

~

I,

,

'*..

,.,.

%,.

!/1/

/,.

97/

:0

/',.

/'/

/'/

/'/'

1//'

.'0 p. /'/'

'0

,.

f-ZwZo0-XWuf-.:ai.:o.:

1.051.10

1.20

1.30

1.402530

4050 60

MO

LEC

ULA

R W

EIG

HT

(MW

)

7080

90

Chart 5

LAB

YR

INT

H O

R D

RY

CA

RB

ON

RIN

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EA

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AR

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R IS

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160

140

120F

or atmos. pressure, add 5%

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100

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MO

LL

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AM

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ET

HO

DE

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PER

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LE

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F)

200°F

150°F

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50°F

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-50°F

-100°F

-150°F

-200° F

100160

140

120

100

80 a:ienWenen

603

40

ample

ST

EP

5: Find N

umber of S

tages requiredF

rom T

able 1, MW

for Ethylene =

28.05. From

Chart

4, using MW = 28.05, k = 1.24, t1 = -140; max.

Head per S

tage = 11200 ft.

68800N

o. Stages = 11200 =

6.15 or 7 stages

r

60800

700°F'

600

500fO

4000°

Calculate the E

lliott compressor required to handle E

thylene at the following operating conditions: 90000

Ib./hr.; Inlet temperature (t,) =

-140F/lnlet pressure (p,) = 15 psia/D

ischarge pressure (P2) = 215 psia.

Refer to E

thylene Mollier diagram

on Page 77:

ST

EP

1: Calculate Inlet F

low (O

d90000

Weight flow (w) = 60 = 1500 Ib./min.

From M

ollier (Page 77): at P1(15 psia) and t1(-140)V1 = 8.0

01 = 8.0 X 1500 = 12000 cfm.

STE

P 2: Select Com

pressor Frame

From

Table 2, the sm

allest compressor fram

e capableof handling the flow

(12000 cfm) is F

rame 38M

.N

ote that this is a horizontally-split machine available

up to 9 stages; average polytropic efficiency 77%;

8100 rpm at 10000 ft. or 12000 ft. head per stage.

Approxim

ate Dim

ensions and Weights are show

n onP

age 33.

ST

EP

3: Find A

diabatic Head (H

ad)F

rom M

ollier, inlet Enthalpy (h,) =

87.5. Follow

lineof constant E

ntropy to P2 (215 psia). Read A

diabaticD

ischarge State P

oint (h2ad) = 169.0

.thad = 169 - 87.5 =

81.5H

ad = 81.5 X

778 = 63400 ft.

ST

EP

4: Find P

olytropic Head (H

p)From

Table 1, k for E

thylene = 1.24. From

Table 2,

215T

Jp = 0.77. Pressure ratio (r) =

15 =.14.33

From Chart 6 (below)-at r = 14.33, k = 1.24, and

TJp =

0.77; TJad =

0.708

H =

63400 X .77 =

68800 ftp .700 .

Chart 6

i'~J. .,

o

':.4I;0

O.

i;

I",

t;

+.

t ~

r.:ts

.05.+ +

761.0 2.0 3.0 4.0 5.0 6.0 7.0 8.0 9.0 10.0 11.0 12.0 13.0 14.0 15.0

PRE

SSUR

E R

AT

IO (r)

ST

EP

6: Find S

peed requiredN

ominal S

peed (Table 2) =

8100 rpm.

688008100 12000 X

7 = 7310 rpm

I,

300--l20P

(lLr

-"?

i

15060°F

STE

P 7: Find Shaft Horsepow

er required1500 X

68800G

as HP =

.77 X 33000 =

4060 hpBearing and Oil Seal Losses (from Chart 5) and

assuming Iso-C

arbon Seals, for F

rame 38M

com-

pressor = 59 hp.

Shaft HP =

4060 + 59 =

4119 hp

ST

EP

8: Find A

ctual Discharge E

nthalpy (h2)81.5

h2 = .708 + 87.5 = 202.5 BTU/lb.

STE

P 9: Find Discharge T

emperature

and Specific V

olume

On M

ollier, plot vertically from h2 to P2 (215 psia).

Read Ì2 =

195F; V2 =

1.14.

100

90

.~I'if

80

c:Ul 70

n.-UJ 60

ci::Ul

Ul

UJ

cin. 50m

¡1

40:; iao

ST

EP

10: Find D

ischarge Flow

o = 1500 X 1.14 = 1710 cfm.

30

POL

YT

RO

PIC E

FFICIE

NC

Y (l\p )

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5560 65 70 75 80

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Section 16

Physical Properties

IntroductionThis section contains a number of charts, correla-

tions, and discussions concerning the physical prop-erties of hydrocarbons and related compounds.

Fig. 16-1 is a table of physical constants ofanumber of hydrocarbon compounds, other commonchemicals, and some common gases. Fig. 16-2 is anabridgement of GPA Publication 2145, an officialindustry standard that is widely referenced in con-tracts for custody transfer and other commercialpurposes.

These two tables are followed by correlations oncompressibilty of gases. Additional correlations fol-low on hydrocarbon fluid densities, boilng points,ASTM distilation, critical properties, acentric factors,vapor pr~ssures, viscosity, thermal conductivity, sur-face tension, and gross heating value of natural gases.

Compressibility of gases

PRESSURE- VOLUME-TEMPERATURE

In dealing with gases at low pressure, the ideal gasrelationship has been, and is, a convenient and gen-erally satisfactory tool. But when faced with measure-ments and calculations for gases under high pressurethe use of the ideal gas relationship may lead toerrors as great as 500 %, as compared with 2 or 3 %at atmospheric pressure.

Many equations of state which have been proposedfor representing the pressure-volume-temperaturerelationship of gases are complicated and inconven.-ient in practical use. The compressibilty factor isreasonably convenient and sufficiently accurate formany engineering requirements. It corresponds to amultiplying correction factor (Z) by which the vol-ume computed from the ideal gas equation is con-verted to the correct actual volume.

PV = ZNRT

P = pressure, psiaV = volume, cu ftZ = compressibility factorN = No. oflb moles, or pqund mols, or

lb/molecular wt.R = gas constant, 10.73 for all gases,

(psia' ft3/(OR.lb mol)T = absolute temperature, (459.67 + OF)

The compressibilty factor Z is a dimensionlessfactor independent of the extent or weight of the gasand determined by the character of the gas, the tem-perature, and pressure. Once Z is known or deter-mined, the calculation of pressure-tern perature-volumerelationships may be made with as much ease at highpressure as at low pressure.

The equation used to calculate gas density is:MP

Pv =10.73 TZ

Where:

Pv = gas density, lb/cu ftM = molecular weight

Other symbols described above

Since molecular weight, pressure, and tempera-ture are set by process considerations, it is necessary

to determine compressibility factor Z to obtain gasdensity.

According to the theorem of corresponding statesthe deviation of any actual gas from the ideal gaslaw is the same for different gases when at the samecorresponding state. The same correspondin.g statesare found at the same fraction of the absolute cr-it-ical temperature and pressure, which are knownas the

Reduced temperature, Tr = T ITe

Reduced pressure, Pr = PIPe

Where:Te = absolute critical temperaturePc = absolute critical pressure

T = absolute temperature at which the gas existsP = absolute pressure at which the gas exists.

Any units of temperature or pressure may be usedprovided only that the same absolute units be used forT as for Te and for P as Pc'

GASEOUS MIXTURES

Fig. 16-3 represents the compressibilty factor asa function of pseudo reduced pressure and pseudo

16 - 1 Rev. 1974

FIG. 16 - 1PHYSICAL CONSTANTS OF HYDROCARBONS(271

See Note No. ~ 1. 2. 3.

Critical conltants

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1 Methane CH4 16.043 -258.74(28) (5000.) -296.45d 667.8 -116.68 0.09B82 Ethane C2H6 30.070 -127.44 (800.) -297.04d 707.8 90.10 0.07883 Propane C3HS 44.097 -43.73 188.0 -305.82d 616.3 206.01 0.07374 n-Butane C4H1O 58.124 31.12 51.54 -217.05 550.7 306.62 0.07035 Isobutane C4H1O 58.124 10.74 72.39 -255.28 529.1 274.96 0.07246 n-Pentane Cs H 1 2 72.151 96.91. 15.575 -201.51 488.6 385.6 0.06747 Isopentane CSH12 72.151 82.11 20.444 -255.82 490.4 369.03 0.06798 Neopentane Cs H 1 2 72.151 49.10 36.66 2.21 464.0 321.08 0.06739 n-Hexane C6HI4 86.178 155.73 4.960 -139.58 436.9 453.6 0.068716 2-Methylpentane C6HI4 86.178 140.47 6.769 -244.59 436.6 435.74 0.0682

11 3-Methylpentane C6HI4 86.178 145.89 6.103 - 453.1 448.2 0.068212 Neohexane C6 H 1 4 86.178 121.51 9.859 -147.77 446.9 420.04 0.066813 2,3-Dimethylbutane C6HI4 86.178 136.36 7.406 -199.37 453.5 440.20 0.066514 n-Heptane C7HI6 100.205 209.16 1.6201 -131.05 396.8 512.7 0.069015 2-Methylhexane C7H 16 100.205 194.09 2.2719 -180.89 396.5 494.89 0.067316 3-Methylhexane C7HI6 i 00.205 197.33 2.1310 - 408.1 503.67 0.064617 3-Ethylpentane C7 H 1 6 1 oe .205 200.26 2.0130 -181.48 419.3 513.36 0.066518 2,2-Dimethylpentane C7HI6 100.205 174.54 3.494 -190.86 402.2 477.12 0.066519 2,4-Dimetlylpentane C7HI6 100.205 176.88 3.293 -182.63 397.0 475.84 0.066820 3,3-Dimethylpentane C7HI6 100.205 186.91 2.774 -210.03 427.1 505.74 0.066221 Triptane C7HI6 100.205 177.58 3.375 -12.84 428.4 496.33 0.0636~ n-Octane CfjH1s 114.232 258.21 0.5370 -70.17 360.6 564.10 0.069023 Diisobutyl CsHls 114.232 228.40 1. 017 -132.16 360.6 530.31 0.067624 Isooctane CsHls 114.232 210.63 1.7089 -161.28 372.5 519.33 0.065725 n-Nonane C9H20 128.259 303.48 0.1796 -64.28 331.8 610.54 0.068426 n-Decane C1oH22 142.286 345.49 0.0609 -21.35 304.4 651.6 0.067927 Cyclopentane CsHlo 70.135 120;65 9.914 -136.96 653.0 461.2 0.059428 Methylcyclopentane C6 H 12 84.162 161.26 4.503 -224.43 549.0 499.24 0.060729 Cyclobexane C6HI2 84.162 177.31 3.266 43.80 590.9 536.6 0.058930 Methylcyclohexane C7HI4 98.189 213.67 1.6093 -195.86 503.6 570.15 0.0601

31 Ethene (Ethylene) C2H4 28.054 -154.79(29) - -272.47d 131. 48.56 0.074832 Propene (Propylene) C3H6 42.081 -53.90 227.6 -301.45d 667.2 197.06 0.068933 l-Butene (Butylene) C4HS 56.108 20.79 62.10 -301.63d 583.5 295.48 0.068634 cis-2-Butene C4Hs 56.108 38.70 45.95 -218.04 612.1 324.37 0.066835 trans-2-Butene C4Hs 56.108 33.58 49.94 -157.99 587.0 311 .86 0.067936 i sobutene C4HS 56.108 19.56 63.64 -220.63 580.0 292.55 0.068237 l-Pentene CsHlo 70.135 85.93 19.117 -265.40 511.8 376.93 0.067638 l,2-Butadiene C4H6 54.092 51.53 36.5 -213.14 (653.0) (340.) (0.0649)39 1,3-Butadiene C4H6 54.092 24.06 59.40(45) -164.04 628.0 305. 0.065540 Isoprene CsHs 68.119 93.33 16.68 -230.71 (558.4) (412.) (0.0650)41 Acetylene C2H2 26.038 -120.78e - -113.4d 890.4 95.32 0.069542 Benzene C6H6 78.114 176.16 3.225 41.96 710.4 552.22 0.052543 Toluene C7Hs 92.141 231.3 1 .0330 -138.98 595.5 605.57 0.054944 Ethylbenzene CsHlo 106.168 277.16 0.3716 -138.96 523.4 651.29 0.056545 a-Xylene CsHlo 106.168 291.97 0.2643 -13.32 541.6 674.92 0.055746 m-Xylene CsHlo 106.168 282.42 0.3265 -54.17 512.9 651.02 0.056747 p-Xylene CsHlo 1 06.168 281.05 0.3424 55.87 509.2 649.54 0.057048 Styrene CsHs 104.152 293.25 0.238 -23.10 580.0 706.0 0.054149 i sopropy Ibenzene C9 H 12 120.195 306.34 0.188 -140.86 465.4 676.3 0.057250 Methyl Alcohol CH40 32.042 148.17 4.631 -143.79 1174. 463.08 0.058951 Ethyl Alcobbl C2H6O 46.069 172.92 2.3125 -173.4 925.8 465.39 0.058052 Carbon Monoxide CO 28.010 -312.68 - -337.0Qd 507.5(33) -220.41 (33) 0.0532(33)53 Carbon Dioxide CO2 44.010 -109.32e - -69.77d 1071.33) 87.87(33) 0.0342(33)54 Hydrogen Sulfide H2S 34.076 -76.56 387.1 (44) -121.58d --ae 30 b 212.6 0.046055 Sulfur Dioxide S02 64.059 13.96 85.46(44) -103.81d 1145. 315.8 0.030456 Ammonia NH3 17.031 -27.99(30) 211.9(44). -107.88d 1636. 270.4 0.068157 Air N2 + 0, 28.964 -317.8(36) - - 546.9(2) -221.4(2) 0.0517(3)58 Hydrogen H2 2.016 -423.17v - -434.81d,v 188.1 -399.9 0.516459 Oxygen O2 31.999 -297.332v -

-361 ß2(),v 736.9 -181.2(33) 0.036760 Nitrogen N, 28.013 -320.44(31 ) - -346.0Qd 493.0 -232.7 0.051661 Chlorine CI2 70.906 -29.25 154.9(44) -149.73d 1118. 291. 0.028062 Water H2O 18.015 212.00v 0.9495 32.00 3207.9 705.5 0.050963 Helium He 4.003 -452.07(32) - - 32.990(32) -450.308(32) 0.2300(32)64 Hydrogen Chloride HCI 36.461 -121.00 906.3(44) -173.52d 1205. 124.8 0.0356

Rev. 198116 - 2

.0~ ,,'.- u.=- 0f! 001 (0U ..~,ou.

~ 15en

(0.3)i0.3563h0.507sh0.5842h0.5630h

0.63110.62440.5966h

0.66400.65790.66890.65400.6664

0.68830.68300.69170.70280.67820.67730.69770.6946

0.70700.69800.69620.72190.73420.75040.75360.78340.7740

0.5217h0.6013h0.6271 h0.6101h0.6005h0.64570.658h0.6272h0.6861

0.615k0.88450.87190.87170.88470.86880.86580.91100.8664

0.79630.79160.7894m0.8176h0.7871h1.397h

0.6175h0.856m(36)0.07107m1.1421 m (25)

0.8094m(26)1 .424h1.0000.1251om0.851h

Density of liquid14.696 psia, 60 of

Ê:i:iu~.=

~ ¡a'¡¡.. :;f! -

(2;il)i2.9701,x4.231h,x4.87CJ4.694h

5.2615.2064.974h

5.5365.4855.5775.4535.556

5.7385.6945.7675.8595.6545.6475.8175.791

5.8945.8195.8046.0196.1216.2566.2836.5316.453

4.348h.x5.01s15.228h5.086h5.006h5.3835.49h5.229h5.720

7.3747.2697.2677.3767.2427.2187.5957.223

6.6396.5996.581m(34)6.817h(35)6.562h,X(36)

11.65h,x (36)

5.14Sh,X(30)7.32m0.5931m(37)9.522m(38)6.748m(31 )

11.87h8.3371.04SOm(32)7.1 CJ,x

4.

PHYSICAL CONSTANTS OF HYDROCARBONS(27)

(2.5)i2.96CJ4.221h4.861h4.684h

5.2525.1964.965h

5.5275.4765.5685.4445.547

5.7295.6855.7585.8505.6455.6385.8085.782

5.8855.8105.7956.0106.1126.2476.2746.5226.444

4.338h5.004h5.219h5.077h4.997h5.3745.48h5.220h5.711

7.3657.2607.2587.3677.2337.2097.5867.214

6.6306.590

6.808h6.553h

11.64h

5.139h

11.86h8.328

7.09h

...cOl

'ai;:..

'! §ia. æ_~ 8: 'æOl 0: c:~-.-

(6.4JÏ10.12h10.42h11.94h12.38h

13.7113.8614.51h

15.5915.7115.4815.8015.51

17.4617.6017.3817.1017.7517.7417.2517.33

19.3819.6319.6821.3123.2611.2113.4012.8915.22

9.678h11.19h10.73h11.03h11.21 h13.039.86h

10.34h11.91

IIÕEl:"iõOl

~ "lII .ë) u.~oo~ (0u ..II '"

~ i:.. .-E ~ u.~ ~o.. .~ b íi-

0.00152h0.00117h0.00119h

0.000870.000900.00104h

0.000750.000780.000750.000780.00075

0.000690.000680.000690.000700.000720.000720.000650.00069

0.000620.000650.000650.000630.000550.000700.000710.000680.00063

0.00189h0.00116h0.00098h0.00107h0.00120h0.000890.00098h0.00113h0.00086

10.59 0.0006612.68 0.0006014.61 0.0005414.39 0.0005514.66 0.0005414.71 0.0005413.71 0.0005716.64 0.00054

4.826 0.000656.981 0.000594.256m -6.456h -5.193h -5.498h -3.308h -4.06m -3.399m -3.360m -4.151m -5.974h -2.160 0.000083Jm -5.14h 0.00335

5.

0.01260.09780.15410.20150.1840

0.25240.2286a. 1967

0.29980.27840.27410.23330.2475

0.34940.33030.32390.31070.28760.30310.26810.2509

0.39810.35640.30410.44520.49040.19450.23080.20980.2364

0.08690.14430.19490.20330.21260.20260.2334

(0.2540)0.1971

(0.1567)

0.18930.20950.26330.30310.31130.32570.32140.19970.3260

0.56480.66080.0440.26670.09200.2548

0.2576

-0.219W0.02000.03720.07370.3434o0.1232

6. 7.

5..u'"..u.¡:..c:IIU'"..IIt!~

..o5.. u.i6 °.. 0;. (0

.':- '";e N .~~iñ(OE ~~c. _ ~E æ -io .. ~()

O.9Y81 0.553909916 1.03820.9808 1.52250.9637 2.00680.9661 2.0068

0.942t 2.49110.948t 2.49110.9534 2.4911

0.910t 2.9753-- 2.9753- 2.9753- 2.9753- 2.97530.852t 3.4596- 3.4596- 3.4596- 3.4596- 3.4596- 3.4596- 3.4596- 3.45960.783t 3.9439- 3.9439- 3.9439- 4.4282- 4.91250.949t 2.4215- 2.9057- 2.9057- 3.39000.9938 0.96860.9844 1.45290.9704 1.93720.9661 1.93720.9662 1.93720.9689 1.93720.948t 2.4215(0.969) 1.8676(0.965) 1.86760.949t 2.3519

0.9925 0.89900.929t 2.69690.903t 3.1812- 3.6655- 3.6655- 3.6655- 3.6655- 3.5959- 4.1498- 1. 063- 1.59060.9995 0.96710.9943 1.51950.9903 1.1765b.9801t 2.2117

0.9899(30) 0.58800.9996 1.00001.0006 0.06960.9993(39) 1.0480.9997 0.9672(0.9875)t(36) 2.4481- 0.62201.0005(40) 0.1382- 1.2588

16 - 3

8.Ideal gas.

14.696 psia, 60 OF

~.:;f!Ol .U ~:¡ /I.~~

en

IIE:i .Õ .0=- "u '"q: ~

'üCtII ..C. ..

en

23.6512.6208.6066.5296.529

5.2605.2605.260

4.4044.4044.4044.4044.404

3.7873.7873.7873.7873.7873.7873.7873.787

3.3223.3223.3222.9592.6675.4114.5094.5093.865

13.5279.0186.7646.7646.7646.7645.4117.0167.0165.571

14.5744.8584.1193.5743.5743.5743.5743.6443.157

11.8438.237

13.558.623

11.365.924

22.2813.102

188.211 .85913.5475.352

21.0694.8010.408

(59.1)i37.48h36.41 h31.80h30.65h

27.6727.3826.16h

24.3824.1624.5624.0224.4 7

21.7321.5621.8422.1921.4121.3922.0321.93

19.5819.3319.2817.8116.3233.8528.3329.4524.92

39.25h33.91h35.36h34.40h33.86h29.1338.4h36.69h31.87

35.8229.9425.9726.3625.8825.8027.6822.80

78.6154.36

58.78h73.07h69.01h

114.71

63.53175.6

73.88

:2:i0-o = ~

.- - E-: ct ::I- ~ ::II '" uE '" '"Ol =-.. (I c:a +- .-..-~

9.Specific heat

capacity14.696 psia, 60 OF

Cp'

Btu/!Ib . OF)

No.

Ideal

gasLiquid

0.5266 - 10.4080 0.9256 20.3887 0.5920 30.3951 0.566(41) 40.3867 0.566(41) 5

0.3880 0.548(41) 60.3829 0.5353 70.3885 0.5540 80.3857 0.5332 90.3833 0.5272 100.3776 0.5187 110.3812 0.5136 120.3748 0.5130 130.3842 0.5280 140.3816 0.5219 150.3790 0.5110 160.3858 0.5140 170.3858 0.5167 180.3951 0.5243 190.3836 0.5018 200.3776 0.4991 210.3831 0.5238 220.3764 0.5112 230.3825 0.4900 240.3822 0.5220 250.3816 0.5207 260.2712 0.4216 270.3010 0.4407 280.2900 0.4392 290.3170 0.4397 300.3622 - 310.3541 0.5835 320.3548 0.5343 330.3269 0.5352(42) 340.3654 0.5345 350.3701 0.5484 360.3635 0.5353(43) 370.3458 0.5403 380.3412 0.5073 390.3570 0.5185 400.3966 - 410.2422 0.4098 420.2598 0.4009 430.2795 0.4113 440.2914 0.4161 450.2782 0.4054 460.2769 0.4083 470.2706 0.4122 480.2917 0.4041 490.3229 0.5933 500.3318 0.5608 610.2484 - 520.1990 - 530.2379 0.4968(36) 540.1448 0.3246(36) 55

0.4967 1.21(30) 560.2400 - 573.401 - 580.2189 - 590.2484 - 600.1137 - 610.4447 1.001 621.240 - 630.1909 - 64

Rev. 1974, 1979

Rev. 1981

PHYSICAL CONSTANTS OF HYDROCARBONS(27)See Note No. -+ 10. 11. 12. 13. Flammability ÄSTM

Heating value 600FP, limi.ts, vol % octane

Net Gross '" U) in number::. c i: .0 air mixturec := c: E(Ê o 0 0''¡ .. " c. -::

.~ lt.ox U)Compound '-) . coNo. :: 0) o U) '"

'8c.

.. co:: "0 'l co_~ C ~~..co co 0._ ::

.ccñ .~

.."ëñ £ Q. B. +-0) i. co:: ..

~(Oco :; .- 0)_ 0).c '8 cxf\+- a~ ~ ii~ .. - * .. 0) .. ''¡ u. ::"O .. E in

.0 "0 .c co "0 0(0 c160 ~.- .¡¡ .. .. .. C' ~.J a

~æ~ -'- '" "'.- c- O) Ql.8 i

g¡ .. ai~æ~ -. ::.- .. :: l- ..-~ æ .. 0'" :: .c

iß ~ ¿:: 0- 0) . :: 0- co "' 0 .!:''¡~ '" 00êi "0 -: .. "0 "' .. .- :: .. .- O)~c. 0-~ co _ ~ co .._ co .. I a: 0: .. I :¡ a:1 Methane 909.1 1009.7 - - 219.20 - 9.54 5.0 15.0 - -2 Ethane 1617.8 1768.7 22178h 65889h 210.39 1.19949h 16.70 2.9 13.0 +0.051 +1.6fj3 Propane 2315.9 2517.2 21499h 90962h 183.03 1 .28624h 23.86 2.1 9.5 97.1 +1.8fj4 n-Butane 3010.5 3262.0 21133h 102918h 165.63 1 .32943h 31.02 1.8 8.4 89.61 93.815 Isobutane 3001.0 3252.6 21084h 98968h 157.52 - 31.02 1.8 8.4 97.6 +0.10fj6 n-Pentane 3706.8 4008.7 20922 110071 153.58 1 .35748 38.18 1.4 8.3 62.61 61.717 Isopentane 3697.9 3999.7 20884 108722 147.12 1.35373 38.18 1.4 (8.3) 90.3 92.38 Neopentane 3682.3 3984.2 20819h 103554h 135.57 1.342 38.18 1.4 (8.3) 80.2 85.5

\9 n-Hexane 4403.9 4756J 20783 115055 143.94 1.37486 45.34 1.2 7.7 26.0 24.810 2-Methylpentane 4395.2 4747.3 20753 113830 138.66 1.37145 45.34 1.2 (7.7) 73.5 73.411 3-Methylpentane 4398.2 4750.3 20764 115801 140.08 1.37652 45.34 (1.2) (7.7) 74.3 74.512 Neohexane 4384.6 4736.8 20718 112975 131.23 1.36876 45.34 1.2 (7.7) 93.4 91.813 2,3-D imethylbutane 4393.8 4746.0 20751 115293 136.07 1.37495 45.34 (1.2) (7.7) 94.3 +0.3114 n-Heptane 5100.3 5502.8 20680 118662 136.00 1.38764 52.50 1.0 7.0 0.0 0.015 2-Methylhexane 5092.3 5494.8 20657 117621 131.58 1.38485 52.50 (1.0) (7.0) 46.4 42.416 3-Methylhexane 5096.1 5498.6 20671 119210 132.10 1 .38864 52.50 (1.0) (7.0) 55.8 52.017 3-Ethylpentane 5098.4 5500.9 20679 121158 132.82 1 .39339 52.50 (1.0) (7.0) 69.3 65.018 2,2-Dimethylpentane 5079.7 5482.2 20620 116585 125.12 1.38215 52.50 (1.0) (7.0) 95.6 92.819 2,4-Dimethylpentane 5084.4 5486.8 20636 116531 126.57 1.38145 52.50 (1.0) (7.0) 83.8 83.120 3,3-Dimethylpentane 5086.5 5489.0 20644 120086 127.20 1.39092 52.50 (1.0) (7.0) 86.6 80.821 Triptane 5081.3 5483.8 20628 119457 124.20 1 .38944 52.50 (1.0) 17.0) +0.11 +1.8122 n-Octane 5796.1 6248.9 20601 121422 129.52 1.39743 59.65 0.96 - - -23 Diisobutyl 5780.7 6233.4 20563 119656 122.82 1.39246 59.65 (0.98) - 55.7 55.224 I soocta ne 5778.9 6231.7 20568 119377 116.70 1.39145 59.65 1.0 - 100. 100.25 n-Nonane 6493.3 6996.3 20542 123642 124.17 1 .40542 66.81 0.878 2.9 - -26 n-Decane 7189.7 1743.1 20494 125444 118.68 1.41189 73.97 0.788 2.6 - -

(27 Cyclopentane 3512.2 3763.7 20186 126284 167.33 1 .40645 35.79 (1.4) - 84.9Í +0.1'28 Methylcyclopentane 4199.1 4501.0 20131 126483 148.54 1.40970 42.95 (1.2) 8.35 80.0 91.329 Cyclohexane 4179.7 4481.6 20036 130855 153.03 1 .42623 42.95 1.3 7.8 77.2 83.030 Methylcyclohexane 4863.7 5215.9 20002 129073 136.30 1.42312 50.11 1.2 - 71. 74.831 Ethene (Ethylene) 1498.5 1599.2 - - 207.55 - 14.32 2.7 34.0 75.6 +0.03132 Propene (Propylene) 2182.7 2333.6 - - 188.17 - 21.48 2.0 10.0 84.9 +0.2133 I-Butene (Butylene) 2879.0 3080.2 20670h 103619h 167.93 - 28.63 1.6 9.3 80.G; 97.434 cis-2-Butene 2871.4 3072.6 20604h 107718h 178.89 - 28.63 (1.6) - 83.5 100.35 t'Bns-2-Butene 2865.1 3066.3 20568h 104609h 174.36 - 28.63 (1.6) - - -36 Isobutene 2859.7 3060.9 20536h 1 02803h 169.47 - 28.63 (1.6) - - -37 l-Pentene 3575.2 3826.7 20545 110594 154.45 1.37148 35.79 1.4 8.7 77.1 90.938 l,2-Butadiene 2789.1 2940.0 20423h 112041h (193.3) - 26.25 (2.0) (12,) - -39 l,3-Butadiene 2730.1 2881.0 20037h 104773h (180.0) - 26.25

(~~)11.5 - -

40 Isoprene 3410.9 3612.1 19951 114120 (165.6) 1.42194 33.41 - 81.0 99.141 Acetylene 1422.4 1472.7 - - - - 11.93 2.5 80. - -42 Benzene 3591.0 3741.9 17989 132651 169.10 1.50112 35.79 1.38 7.9g +2.81 -43 Toluene 4273.5 4474.8 18250 132659 154.83' 1.49693 42.95 1.2g 7.1g +0.31 +5.8144 Ethylbenzene 4970.6 5222.1 18492 134381 144.02 1.49588 50.11 0.99g 6.7g 97.9 +0.8145 a-Xylene 4958.1 5209.7 18443 136036 149.10 1.50545 50.11 1.g 6.4R 100. -46 m-Xylene 4956.2 5207.8 18440 133542 147.24 1.49722 50.11 1.1g 6.4R +2.81 +4.0147 p-Xylene 4957.0 5208.6 18444 133129 145.71 1.49582 50.11 1.g 6.f3 +1.21 +3.4148 Styrene 4829.5 5030.8 18148 137834 (151.00) 1.54682 47.72 1.1 6.1 +0.21 )o3/49 Isopropylbenzene 5661.0 5962.8 18663 134803 134.24 ' 1.49145 57.27 0.88g 6.5R 99.3 +2.1150 Methyl Alcohol 766.2 866.8 9752 64744 462.58 1 .32840 7.16 6.72(5) 36.50 - -51 Ethyl Alcohol 1448.2 1599.1 12771 84276 361.37 1.36143 14.32 3.28(5) 18.95 - -52 Carbon Monoxide 319.79 319.79 - - 92.7 1 .00034 2.39 12.50(5) 74.20 - -53 Carbon Dioxide 0 0 - - 246.5n 1 .00045 - - - - -54 Hydrogen Sulfide 586.71 637.02 - - 236.2 1 .00059 7.16 4.30(5) 45.50 - -55 Sulfur Dioxide - - - - 167. 1.00061 - - - - -56 Ammonia 358.94 432.59 - - 589.4 1.00035 3.58 15.50(5) 27.00 - -57 Air - - - - 88.22 - - - - - -58 Hydrogen 273.85 . 324.15 - - 193. 1.00013 2.39 4.00(5) 74.20 - -59 Oxygen - - - - 91.62 1 .00027 - - - - -60 Nitrogen - - - - 85.60 1 .00028 - - - - -61 Chlorine - - - - 123.7 1 .3832h - - - - -62 Water 0 49.4 0 0 970.3 1 .33299 - - - - -63 Helium - - - - - 1 .00003 - - - - -64 Hydrogen Chloride - - - - 185.5 1 .00042 - - - - -

Rev, 1974, 1979

Rev. 198116 - 4