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
G S
EA
LIS
O-C
AR
BO
N O
R IS
O-S
LEE
VE
SE
AL
160
140
120F
or atmos. pressure, add 5%
foreach additional 100 psi suctionpressure.
100
ã: 80
ienweneno.- 60
MO
LL
IER
EX
AM
PLE
"N" M
ET
HO
DE
XA
MPL
E
40
206000 8000 10,000
2010002000 4000
OPE
RA
TIN
G SPE
ED
6000 8000 10,000 1000 2000 4000O
PER
AT
ING
SPEE
D
74
000,'/'IN
LE
TT
EM
P(O
F)
200°F
150°F
100°F
50°F
OaF
-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 )
66 68 70 72 74 76 78 80 82 84 86 88
f,"
20
( I..~
- 6F~f:
10 i It9_
"f865.4
60
5560 65 70 75 80
AD
IA8A
TIC
EF
FIC
IEN
CY
(l)ad)90
85
80°!'
I °F
I 0
Ethylene Chart
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c 116.5 F P
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Adapted from
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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
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