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Phase Behavior in Binary
And Multicomponent Systems
At Elevated Pressures:
n-Pentane and
Methane-n-Pentane
NATIONAL BUREAU OF STANDARDS
The National Bureau of Standards ' was established by an act of Congress March 3, 1901. Today,
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UNITED STATES DEPARTMENT OF COMMERCE
Maurice H. Stans, Secretary
NATIONAL BUREAU OF STANDARDS • Lewis M. Branscomb, Director
Phase Behavior in Binary and Multicomponent SystemsAt Elevated Pressures: n-Pentane and Methane-n -Pentane
Virginia M. Berry and B. H. Sage
Chemical Engineering Laboratory
California Institute of Technology
Pasadena, California 91109
NSRDS-NBS 32
Nat. Stand. Ref. Data Ser., Nat Bur. Stand. (U.S.), 32, 73 pages (June 1970)
CODEN: NSRDA
Issued June 1970
For sale by the Superintendent of Documents, U.S. Government Printing Office
Washington, D.C. 20402 (Order by SD Catalog No. C 13.48:32), Price 70 cent9
NATIONAL BUREAU Of STANDARDS
JUL 2 3 1970
no. /fln
/ 70Cop
.
© 1970 by the Secretary of Commerce on behalf of the United States Government.
Library of Congress Catalog Card Number: 78-603442
Foreword
The National Standard Reference Data System provides effective access to the quantitative
data of physical science, critically evaluated and compiled for convenience, and readily accessible
through a variety of distribution channels. The System was established in 1963 by action of the
President’s Office of Science and Technology and the Federal Council for Science and Technology,
with responsibility to administer it assigned to the National Bureau of Standards.
The System now comprises a complex of data centers and other activities, carried on in
academic institutions and other laboratories both in and out of government. The independent
operational status of existing critical data projects is maintained and encouraged. Data centers
that are components of the NSRDS produce compilations of critically evaluated data, critical
reviews of the state of quantitative knowledge in specialized areas, and computations of useful
functions derived from standard reference data. In addition, the centers and projects establish
criteria for evaluation and compilation of data and make recommendations on needed improvements
in experimental techniques. They are normally closely associated with active research in the
relevant field.
The technical scope of the NSRDS is indicated by the principal categories of data compilation
projects now active or being planned: nuclear properties, atomic and molecular properties, solid
state properties, thermodynamic and transport properties, chemical kinetics, and colloid and
surface properties.
The NSRDS receives advice and planning assistance from the National Research Council of
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The NSRDS-NBS series of publications is intended primarily to include evaluated reference
data and critical reviews of long-term interest to the scientific and technical community.
Lewis M. Branscomb, Director
ill
Preface
In 1966 support was received from the Office of Standard Reference Data of the National
Bureau of Standards for a program of data review undertaken in the Chemical Engineering Labora-
tory of the California Institute of Technology. Emphasis was directed to the volumetric and phase
behavior of the coexisting phases of pure paraffin hydrocarbons and their binary mixtures. Aneffort was made to provide conservative estimates of the accuracy in contradistinction to the
precision of the tabulations presented. As a result of the withdrawal of B. H. Sage from active
research on July 1, 1969, the program has been limited to work completed at that time. The current
presentation covers a review of the methods employed, the volumetric and phase behavior of
n-pentane, and the volumetric and phase behavior in the methane-n-pentane system.
A number of the members of the staff of the Chemical Engineering Laboratory contributed
to the work and among these should be mentioned Donna Johnson, who aided in the tabulation of
the results and the preparation of the manuscript, and June Gray, who assisted the authors in the
preparation of the numerous diagrams associated with this activity.
IV
Contents
Page
Foreword Ill
Preface IV
List of figures VList of tables VNomenclature and conversion factors., VII, VIII
1. Introduction 1
1.1. Measures of uncertainty 1
1.2. Residual methods 2
1.3. Dimensions and units 3
2. The n-pentane system 13
3. The methane-n-pentane system 22
4. References 66
List of Figures
Figure page
1.1. Variation in dew point volume of propane with temperature 4
1.2. Residual dew point volume of propane 5
1.3. Vapor pressure of propane 6
1.4. Vapor pressure-temperature diagram 7
2.1. Residual vapor pressure of re-pentane 15
2.2. Bubble point volume of n-pentane 16
2.3. Residual volume at dew point for re-pentane 17
3.1. Pressure-temperature diagram for methane-n-pentane system 24
3.2. Effect of pressure upon equilibrium ratio for methane-n-pentane system 25
3.3. Pressure-composition diagram for methane-n-pentane system 26
3.4. Pressure-temperature diagram for methane-n-pentane system, engineering units 27
3.5. Effect of pressure upon equilibirum ratio for methane-n-pentane system, engineering units 28
3.6. Pressure-composition diagram for methane-n-pentane system, engineering units 29
List of Tables
Table
1.1. Experimental values of dew point volume for propane
1.2. Residual specific volume of dew point gas for propane
1.3. Deviations of several sets of experimental data for specific volume of dew point gas for propane
1.4. Experimental values of vapor pressure for propane
1.5. Deviations in experimental values of vapor pressure for propane
2.1. Critical properties of n-pentane
2.2. Properties of the coexisting phases for re-pentane
2.3. Agreement of interpolated and experimental data for re-pentane
2.4. Critical properties of the n-pentane system, engineering units
2.5. Properties of the coexisting phases for re-pentane, engineering units
2.6. Agreement of interpolated and experimental data for re-pentane, engineering units
2.7. Accuracy of experimental background for re-pentane
2.8. Reviews of properties of the paraffin hydrocarbons
3.1. Properties of the coexisting phases in the methane-re-pentane system
3.2. Agreement of interpolated and experimental data for the methane-re-pentane system
3.3. Unique states for the methane-re-pentane system
3.4. Properties of the coexisting phases in the methane-n-pentane system, engineering units
3.5. Unique states for the methane-n-pentane system, engineering units
3.6. Agreement of interpolated and experimental data for the methane-re-pentane system, engineering units
3.7. Accuracy of experimental background for the methane-n-pentane system
Page
8
9
10
11
12
17
18
19
19
20
21
21
22
30
46
46
47
65
65
6t>
V
,
CO,
C«
Nomenclature
B, C, D Coefficients
Variable
Molal equilibrium ratio, K— y\x
Number of points
Pressure, atm or psia
Residual pressure, atm or psia
Average deviation defined by
2 (Cm-Cm )IN1
Absolute deviation defined by
^ (GeXp— Gsm )IN
1
Absolute temperature, K or °RTemperature, °C or °F
Specific volume, liters/kg or ft 3/lb
Molal volume, liters/kg-mol or ft3/lb-mol
V Residual volume, liters/kg
X Mole fraction liquid
y. Mole fraction gas
a Degrees of freedomcr Standard error of estimate
{ X (^exp— Csm )
2
1
/(/v-
Subscripts
exp Experimentalgr Graphical
k Component k
j Component jr Referencesm Smooth or predicted
Constants and Conversion Factors
Molecular Weight3
Methane 16.04303
Propane 44.09721n-Pentane 72.15139
Physical Constants 15
Force
1 pound (lb) avoirdupois
Length1 U.S. inch (in)
Volume1 liter (1)
Acceleration Due to Gravity— Standard
gc
Pressure1 standard atmosphere (atm)
Temperature1 degree centigrade (° C)
TICTo F
= 453.59237 grams (g)
= 2.54 centimeters (cm)
= 1000 cm 3
= 980.665 cm/sec2
= 32.1740 ft/sec 2
= 1,013,250 dyne/cm2 = 101,325 N/m 2
= 1.8 degrees Fahrenheit (°F)= 273.16 degrees Kelvin (°K)= 459.688 degrees Rankine (° R)
a Based on a Report of the International Commission on Atomic Weights, J. Am Chem. Soc. 84, 4175-97 (1962).b Wilhoit, Randolph C. and Hathaway, Wayne, Tables of Conversion Factors Based on Accepted Constants as of 1965. Am Petroleum Inst., Project 44, Chemical Thermodynamic
Properties Center, Texas A & M Univ., College Station, Texas, Nov. 1965.
VII
Conversion Factors 3
Length
Units cm m in ft
1 cm 1 0.01 0.3937008 0.03280401 m 100 1 39.37008 3.2808401 in 2.540000 0.02540000 1 0.083333331 ft 30.48000 0.3048000 12.0000 1
Area
Units cm 2 m2 in 2ft
2
1 cm21 io-4 0.1550003 1.076391 x 10-3
1 m 2 104 1 1550.0003 10.76391
1 in2 6.451600 6.451600 X 10-41 6.944444 X IO*3
1 ft 2 929.0304 0.09290304 144.0000 1
Volume
Units cm 3 in3 ft 3 liter
1 cm 3 1 0.06102374 3.531467 x 10-5 1.000 x io-3
1 in3 16.38706 1 5.787037 x 10~4 1.638661 X 10-2
1 ft3 28316.85 1728.000 1 28.316851 liter 1000.000 61.02375 0.0351467 1
Weight
Units g lb
1 g 1 2.204623 X IO-3
1 lb 453.5924 1
Specific Weight
Units g/cm 3 g/ml lb/ft 3
1 g/cm31 1 62.42795
1 g/ml 1 1 62.427951 lb/ft 3 0.01601847 0.01601847 1
Pressure
Units atm kg/cm 2 lb/in 2 Newton/m2
1 atm 1 1.033227 14.69595 1.013250 X 105
1 kg/cm 2 0.9678411 1 14.22334 9806.6501 lb/in2 0.06804596 0.07030696 1 6894.757
Newtons/
m
2 9.869233 X 10-6 1.019716 X 10-5 14.50377 X 10-51
a See footnote b on page VII.
VIII
Phase Behavior in Binary and Multicomponent SystemsAt Elevated Pressures: n-Pentane and Methane-n-Pentane
Virginia M. Berry and B. H. Sage
This paper, which is concerned with the critical evaluation of data on the phase behavior of binary
systems, consists of three parts. In the first part the rationale of the evaluation process used is dis-
cussed, in the second the behavior of n-pentane, and in the third the behavior of the system methane-n-pentane.
The properties of n-pentane considered are the critical constants and the vapor pressures anddensities of the saturated coexistent phases as functions of temperature. For the methane-n-pentanesystem the compositions and densities of the coexisting phases are given as functions of temperatureand total pressure. Data for the unique states of the two-component system are also presented.
Discussions are given of the reliability of the selected values and of the differences between the
selected values and various measured values.
Key words: Evaluated data; liquid-vapor equilibria; methane-n-pentane system; n-pentane;
thermodynamics.
1. Introduction
The critical review of experimental data in the
field of volumetric and phase behavior of pure
substances and mixtures involves, at best, certain
elements of judgment, particularly in regard to the
actual in contradistinction to the stated uncer-
tainties of measurement. Probably historical evi-
dence is the best evidence of the difference be-
tween the stated and actual uncertainties associated
with experimental observations. Often precision is
confused with accuracy even though the author
has made a conscientious effort to appraise the
uncertainties in each of the primary experimental
variables involved. In this critical review and com-pilation, an effort was made to apply realistic andconservative uncertainties to the tabulated values
which, to many readers, may seem unusually large
when the claims of the investigators are considered.
In the authors’ experience, the accepted intensive
properties of materials continue to change with the
passage of time by amounts which are many times
the original estimated uncertainties involved in the
experimental work. An example of such a situation
is the thermodynamic properties of water. Accuratevalues of the thermodynamic properties of waterin both the liquid and gas phase are of importancein the design of large steam turbines. Yet, within
the last 10 years, differences in the properties of
water employed in this country and in Russia re-
sulted in significant differences in the prediction
of the efficiency of large steam turbines manu-factured in the two countries. Even with unusualinternational cooperation in this matter [l] 1 in-
dividual nations still prepare their own tabulations
1 Figures in brackets indicate the literature references at the end of this paper.
of the thermodynamic properties of water whichdiffer somewhat in detail.
On the basis of such experience it is hoped that
the reader will understand the conservatism
employed in assigning rather large measures of
uncertainty to the individual experimental data as
compared to that which has often been suggested
by the original experimental investigator. In addi-
tion, the uncertainties assigned to the recorded
values have been set forth on what is hoped to bea realistic basis. It will remain for investigators
of the future to ascertain whether the somewhatsubjective assignment of uncertainty in connection
with the recorded values has been correct.
1.1. Measures of Uncertainty
In the following section a short discussion of the
measures of uncertainty employed is presented.No attempt has been made to justify the choice of
such measures but only to indicate in a specific
manner what was involved. The use of an exampleis perhaps the best method to illustrate the fashion
in which the several measures of uncertainty canbe applied. In figure 1.1 2 is portrayed the variation
in the specific volume with temperature of the dewpoint gas for propane. In addition, the various ex-
perimental values upon which the critically chosenfine was evaluated have been presented. There is
set forth in table 1.1 the several results obtained bydifferent experimental methods. The points shownin figure 1.1 are presented in the table together with
2 Figures and tables will be found at the end of the section to which they pertain.
372-701 0 - 70 -2
1
an estimate of the measure of uncertainty of eachset of experimental data.
In the example, presented in table 1.1, it has beenassumed that all of the uncertainty is in the specific
volume and none in the temperature. The curvewas established by direct graphical inspection of
the data coupled with the application of “least
squares” methods of analysis to a particular
polynomial which will be presented later in the
discussion.
The greatest weight was given to the experimentaldata which was assigned the smallest uncertainty
in table 1.1. Usually there is not as much experi-
mental data as is indicated in figure 1.1 and the
choice of the smooth functional relation becomes,in part, a matter of judgment. The average deviationwith regard and without regard to sign was estab-
lished by use of the following expressions:
s = f(G-Gsm )IN, (1.1)
variable undergoes marked change from a low tem-
perature to temperatures approaching that of the
critical state. In some circumstances it is desirable
to treat only portions of the range of the independentvariables as an independent statistical population.
This is particularly true when the data from different
investigators do not extend over the entire range of
the independent variable as is the case in figure 1.1.
In many ways it would be advantageous to consider
the normal distance of the curve from the experi-
mental points in question. However, this introduces
significant complexities in the evaluation of eachmeasure of uncertainty and for that reason has not
been adopted in the current tabulations.
1.2. Residual Methods
In many situations the combination of analytical
and graphical techniques is useful. For example,it is possible to approximate the smooth curveshown in figure 1.1 by a polynomial of the following
form:
s'=2\G-Gm \IN. (1.2)
1
For the most part, the value of the average deviation
with regard to sign should be small and deviate
from zero primarily as a result of intentional bias
in locating the critically chosen value in order to
favor the more accurate data. This is illustrated bythe values of the average deviation with regard to
sign of the points shown in figure 1.1 which havebeen tabulated in table 1.1 for each of the several
investigators.
As a second measure of uncertainty, the average
deviation without regard to sign was established
from eq (1.2) and is one useful measure of the
variability of the data from the smooth curve shown.The results of applying eq (1.2) to the experimental
information presented in figure 1.1 are also recorded
in a portion of table 1.1. The average difference be-
tween deviations with regard to and without
regard to sign is evident.
For many purposes, the standard error of estimate
is a useful means of indicating the difference be-
tween a chosen continuous function such as the
curve in figure 1.1 and the experimental points
involved. This quantity may be defined by eq (1.3):
a 2<c-csmvi- l
(N-a)}1'2 (1.3)
The quantity a represents the degrees of freedomassociated with the system. In the case of a puresubstance it is one since the temperature fully
establishes all of the intensive properties of the twocoexisting phases. The values of the standard error
of estimate as established from eq (1.3) for eachof the experimental investigations are recordedin a portion of table 1.1.
All of these measures of uncertainty suffer fromthe fact that the magnitude of the dependent
V=AT+BT2 + CT3 + DT4= 24.967T- 0.21184T2
+ 0.60276 X 10-3P - 0.57430 X HU6!74
(1.4)
In this instance, the coefficients have been indicated
in both symbolic and numerical form. There is
shown in figure 1.2 the smooth curve of figure 1.1
and the graphical representation of eq (1.4). Upona markedly enlarged scale the difference betweenthe analytical and graphical representation has beendepicted in a portion of figure 1.2. Such a difference
is called the residual specific volume of the dewpoint which would be defined by:
V=V-Vr (1.5)
The value of the residual specific volume of the
dew-point gas may be evaluated for each of the ex-
perimental points by application of eq (1.5). Thecorresponding values of the analytical reference
values established from eq (1.4) for the temperatureof measurement as well as the values of the residual
specific volume of the dew-point gas are recordedin a part of table 1.2 for each set of experimentaldata. It is apparent from a review of table 1.2 that
the residual specific volumes do not undergo changesin order of magnitude over the entire range of
temperature.
Smooth values of the residual specific volume for
each of the experimental points also are recorded in
table 1.2. It is evident that the graphical precision
realized by use of the residual techniques is muchgreater than that feasible from direct plotting of the
data. Attempts to increase the scale of the graphical
operations invariably results in such wide spacing
of the experimental points as to render any markedimprovement in the precision of the graphical
operation difficult.
In table 1.3 are shown the values obtained for
the average deviation with regard to sign, the
2
average deviation without regard to sign, and the
standard error of estimate as determined from large
plots, one such as is shown in figure 1.1 and a similar
sized plot involving the residual data shown in figure
1.2. It is believed that the comparison presented in
table 1.3 shows what can be gained by the use of
residual methods.Such approaches are also useful in connection
with the smoothing of vapor pressure data. Undersuch circumstances a form of the Antoine equation
[2] may be used as the reference expression for
vapor pressure. The reference vapor pressure maybe approximated by:
logioPr^+y (1.6)
Using propane as an example, the coefficients of
eq (1.6) become:
logic Pr= 4.294323 -990
'p--- (1.7)
There is shown in table 1.4 experimental values of
the vapor pressure of propane based upon the meas-urements of several investigators. The corre-
sponding reference vapor pressure calculated from
eq (1.7) is included along with the residual vaporpressure defined by eq (1.8):
P=P-PT (1.8)
In figure 1.3 is depicted the vapor pressure as a
function of temperature for propane with the ex-
perimental data of table 1.4 included. In the lowerpart of this figure is shown the residual vapor pres-
sure with the same experimental data. The shapeof the residual vapor pressure curve is typical for
most paraffin hydrocarbons when a form of the
Antoine equation is employed as a reference. Theprecision with which the measures of uncertainty
can be established has been increased manyfoldby the use of the residual vapor pressure shown in
the lower part of figure 1.3. The results of the
evaluation by analytic methods of the average devia-
tion with regard to sign, the average deviation
without regard to sign, and the standard error of
estimate are recorded in table 1.5 for each set of
experimental data.
Such residual techniques as have been described
were employed in this review and tabulation when-ever feasible. A certain amount of ingenuity is
required to utilize the most efficacious form of the
analytical expression to approximate the experi-
mental behavior. The use of residual methods pre-
vents a tendency to expand the scale of both the
independent and dependent variable in an attemptto increase the precision of the direct interpolative
process. Often such attempts yield unsatisfactory
results because of the wide spacing of the experi-
mental data. This is illustrated in figure 1.4 wherethe vapor pressure data for propane have beenexpanded on a large scale plot involving only a
portion of the temperature range. Physical separa-
tion of points on the diagram indicates the
uncertainties that are introduced in arriving at the
most probable curve to draw through the data.
1.3. Dimensions and Units 3
The greater part of the scientific literature is
expressed in the mass-length-time system of dimen-sions. This system of dimensions will be usedthroughout this compilation in the primary tabula-
tions. However, in the interest of utility, pressures
will be expressed in atmospheres. A conversionfactor is available to permit the establishment of
the numerical value of the pressure expressed in
newtons per square meter if such should be desired.
Temperatures will be expressed in degrees kelvin
which are related to temperatures in degreesCelsius by the following expression:
T=t+ 273.16 (1.9)
The value of the constant in eq (1.9) is based uponrecent international agreement concerning thetemperature in degrees kelvin of the triple point of
water [3], The nomenclature employed togetherwith the dimensions and units involved are givenbefore the introduction on p. vil. A short table ofconversion factors for the common dimensions andunits used is also presented, p. VIII.
A number of secondary tabulations have beenprepared involving the force-length-time systemof dimensions and engineering units. The appro-priate conversion factors may be found in the above-mentioned conversion table.
3 The NBS Office of Standard Reference Data, as administrator of the NationalStandard Reference Data System, has officially adopted the use of SI units for all
NSRDS publications, in accordance with NBS practice. This publication does not
use SI units because contractual commitments with the author predate establishment
of a firm policy on their use by NBS. However, conversion factors are given. We urgethat specialists and other users of data in this field accustom themselves to SI units
as rapidly as possible.
3
oCOro
Oro
LlI
(T
O 3C\J h-ro <
crLlI
CL
LJ
O HOro
OCOC\J
lOCVJ
OO
by\/ sjid\\\
LOn-
o loLO C\J
3IAimOA
4
FIGURE
1.1.
Variation
in
dew
point
volume
of
propane
with
temperature.
VOLUME
liters
/kg
2.5
0
- 2.5
- 5.0
FIGURE 1.2. Residual dew point volume ofpropane.
5
RESIDUAL
VOLUME
liters
/kg
VAPOR
PRESSURE
atm
0.25
0
-0.25
280 300 320 340 360
TEMPERATURE K
FIGURE 1.3. Vapor pressure of propane.
6
RESIDUAL
VAPOR
PRESSURE
atm
VAPOR
PRESSURE
atm
TEMPERATURE K
Figure 1.4. Vapor pressure-temperature diagram.
7
Table 1.1. Experimental values ofdew point volume a/or propane
Temperature
Reference
Temperature
Reference
Dana[4]
Sage
[5]
Reamer[6]
Helge-
son b[7]
Dana[4]
Sage
[5]
Reamer[6]
Helge-
son b[7]
K K255.4 169.2 343.5 15.4
260.9 141.7 344.3 15.2 15.4
266.5 118.6 346.4 14.3
272.0 99.9 346.9 14.0
277.6 85.5 82.8 349.8 13.2
283.2 73.7 72.7350.1 12.7
288.7 63.1 62.3352.7 12.1
293.9 52.4353.1 11.6
294.3 55.1 53.7355.4 11.3
299.8 48.1 46.4355.9 10.6
301.1 43.3
305 4 42.0 40.2 358.3 10.2
307 5 37.0 358.6 9.6
310 9 3A 9 34. ft 34. Q 360.9 9.8 9.5
313.3 32.2 361.3 8.8
363.6 8.5
313.5 32.6
316.5 32.5 30.4 363 8 8 0
318.6 28.3 366 3 7.3
322.0 28.7 26.5 368 4 6.6
323.4 25.3 368 8 6.5
370.0 4.5324.5 J 25.6
327 6 23.0 23.1
327.9 22.8
332.0 20.6 Estimated uncer-
332.1
333.2
20.5
20.2
tainty c, percent 1.0 0.2 0.2 0.2
336.1 18.6 Deviation
338.7 17.6 absolute d 1.07 0.31 0.28 0.34
339.6 16.8 algebraic e 1.07 -0.27 0.22 0.07
339.9 16.9 standard f1.4* 0.62 0.39 0.58
a Specific volumes expressed in liters/kg.b Specific volume calculated by application of Clapeyron equation to latent heat of
vaporization data.c Estimated uncertainty in experimental measurements.
d Absolute deviation defined by eq (2).e Average deviation defined by eq (1).
' Standard deviation defined by eq (3).
8
Table 1.2. Residual specific volume of dew point gas for propane
Temperature Reference
volume b
Residual volume a, liters/kg
Dana [4] Sage [5] Reamer[6]
Helgeson Smooth c
K
255.4 156.7 12.4 12.4
260.9 137.7 4.0 4.0
266.5 120.3 -1.7 -1.7
272.0 104.5 -4.6 -4.6
277.6 90.1 -5.4 -6.5 -5.4
283.2 77.3 -4.0 -5.3 -4.9
288.7 66.0 -3.4 -3.6 -3.6
293.9 56.7 -2.9 -2.3
294.3 56.1 -1.8 -2.3 -2.3
299.8 47.6 -1.2 -1.2 -1.1
301.1 45.8 -1.5 -0.9
305.4 40.3 -0.1 -0.2 -.1
307.5 37.8 -0.2 .1
310.9 34.2 .7 0.7 .5 .5
313.3 31.9 .5 .8
313.5 31.7 .7 .8
316.5 29.1 1.1 .7 1.0
318.6 27.5 .8 1.2
322.0 25.0 1.6 1.2 1.3
323.4 24.2 1.2 1.3
324.5 23.5 1.9 1.3
327.6 21.7 1.3 1.3 1.3
327.9 21.5 1.5 1.3
332.0 19.6 1.0 1.1
332.1 19.5 1.1 1.1
333.2 19.1 1.0 1.0
336.1 17.9 0.8 0.8
338.7 17.0 0.4 .5
339.6 16.6 0.4 .4
339.9 16.5 .5 .4
343.5 15.4 .1 -.1
344.3 15.1 -.3 -.3 -.2
346.4 14.5 -.4 -.4
346.9 14.3 -.2 -.5
349.8 13.5 -.7 -.8
350.1 13.4 -.6 -.8
352.7 12.6 -.9 -.9
353.1 12.5 -.8 -.9
355.4 11.8 -1.0 -1.0
355.9 11.6 -.9 -1.0
372-701 0 - 70 -39
Table 1.2. Residual specific volume of dew point gas for propane— Continued
Temperature Reference
volume b
Residual volume aliters/kg
Dana [4] Sage [5] Reamer[6]
Helgeson[7]
Smooth c
K
358.3 10.8 -1.0 -1.0
358.6 10.6 — 0.8 -1.0
360.9 9.8 -1.1 -0.9 -0.8
361.3 9.6 -.7 - 8
363.6 8.6 -0.5 -.4
363.8 8.6 -.5 -.4
366.3 7.4 -.1 .0
368.4 6.3 .3 4
368.8 6.0 .6 .6
370.0 5.3 -.8 .8
a Residual specific volume defined by Fg,— Vr.
b Reference volume expressed in liters/kg and defined by eq (4).c Critically chosen values of residual volume.
Table 1.3. Deviations of several sets of experimental data for
specific volume of dew point gas for propane
Deviation
Reference
Dana
[4]
Sage
[5]
Reamer[6]
Helge-
son [7]
Liters/ Liters/ Liters/ Liters/
kg kg kg kg
Absolute a 0.18 0.20 0.11 0.16
Algebraic b -.07 .02 .07 .08
Standard c .31 .27 .20 .32
Number of Points 13 20 14 16
a Absolute deviation defined by eq (2).
b Average deviation defined by eq (1).
c Standard error of estimate defined by eq (3).
10
Table 1.4. Experimental values of vapor pressure for propane
TemperatureK
Referencepressure,
equation
(1.7)
Dana [4] Sage [5] Reamer [6] Helgeson [7]
Vaporpressure
Residualpressure b
Vaporpressure
Residualpressure b
Vaporpressure
Residualpressure b
Vaporpressure
Residualpressure b
255 4 2 604 2.599 -0.005
260 9 3 150 3.130 -.020
266 5 3 779 3.776 -.003
272 0 4 501 4.511 .010
277 6 5 323 5.308 -.015 5.376 0.053
283 2 6 254 6.247 -.007 6.314 .061
288 7 7.302 7.288 -.014 7.335 .033
293 9 8 403 8.506 0.103
294 3 8.477 8.438 -.039 8.506 .029
299 8 9 786 9.717 -.069 9.805 .019
301 1 10.107 10.207 .100
305 4 11.239 11.160 -.079 11.248 .009
307 5 11.830 11.908 .078
310.9 12.843 12.724 -.119 12.840 -0.003 12.840 -.003
313.3 13.582 13.609 .027
313 5 13.634 13.609 -.025
316.5 14.608 14.426 -.182 14.596 -.012
318.6 15.322 15.310 -.012
322.0 16.542 16.331 -.211 16.515 -.026
323.4 17.032 17.011 -.022
324.5 17.448 17.011 -.047
327.6 18.652 18.610 -.042 18.610 -.042
327.9 18.785 18.713 -.072
332.0 20.474 20.414 -.060
332.1 20.498 20.414 -.084
333.2 20.949 20.910 -.039
336.1 22.243 22.115 -.128
338.7 23.438 23.408 -.030
339.6 23.854 23.816 -.038
339.9 23.986 23.816 -.170
343.5 25.739 25.517 -.222
344.3 26.128 26.116 -.012 26.116 -.012
346.4 27.234 27.218 -.016
346.9 27.493 27.218 -.275
349.8 29.027 29.049 .021
350.1 29.178 28.919 -.259
352.7 30.619 30.621 .002
353.1 30.838 30.621 -.217
355.4 32.142 32.226 .084
355.9 32.433 32.322 -.111
358.3 33.849 34.023 .174
358.6 34.050 34.023 -.027
11
Table 1.4. Experimental values of vapor pressure for propane a— Continued
TemperatureK
Referencepressure,
equation
(1.7)
Dana [4] Sage [5] Reamer [6] Helgeson [7]
Vaporpressure
Residualpressure b
Vaporpressure
Residualpressure b
Vaporpressure
Residualpressure b
Vaporpressure
Residualpressure b
360.9
361.3
363.6
363.8
366.3
368.4
368.8
370.0
35.479
35.686
37.162
37.269
38.898
40.311
40.576
41.413
35.710 .231 35.710 .231
35.724 .038
37.425 .263
37.425
39.126
.156
.228
40.827 .516
40.827 .251
42.011 .598
Estimated uncertainty,
percent 1.0 0.2 0.2 0.2
3 Pressures expressed in atmospheres.b Residual pressure calculated from eq (8).
Table 1.5. Deviations in experimental values of vapor pressure
for propane
Deviation a
Reference
Dana[4]
Sage
[5]
Reamer[6]
Helge-
son [7 ]
atm atm atm atm
Absolute b 0.059 0.129 0.173 0.044
Algebraic c -0.058 -0.031 0.082 0.024
Standard d 0.094 0.173 0.166 0.071
Number of Points 13 20 14 16
3 Deviations between experimental and predicted values.b Absolute deviation defined by eq (2).c Average deviation defined by eq (1).d Standard error of estimate defined by eq (3).
12
2. The fi-Pentane System
The vapor pressure of re-pentane has been studied
by numerous investigators [8-13] and the critical
properties have been measured many times [8, 9,
12, 14, 15]. The older data suffer from limitations
as to the purity of the samples of re-pentane em-ployed. For this reason, primary emphasis has beengiven to the latter measurements which have em-ployed markedly purer materials than those avail-
able prior to 1945. Table 1 reports critical properties
of re-pentane as measured by several investigators.
The critically chosen values are recorded in the
lower part of the table along with estimated meas-ures of uncertainty.
For the most part, the critically chosen values
follow closely those selected by the AmericanPetroleum Institute Project 44 [16]. It was thought
that Project 44 had an opportunity to review the
critical properties in somewhat greater detail than
was done in the present instance. The rather large
estimated uncertainty in the critical temperatureresulted from the significant variation in the critical
temperature reported by Beattie [12] and Ambrose[14]. Likewise, the critical pressure selected bythe American Petroleum Institute Project 44 wassignificantly different from that established fromthe experimental work of Beattie. For this reasonan uncertainty of 0.2 atm was selected. Ratherclose agreement in the critical volume as established
by Beattie [12] from direct volumetric measurementand that selected by the American PetroleumInstitute Project 44 [16] resulted in a somewhatsmaller estimate of uncertainty than otherwisewould haive been the case.
Following the graphical techniques that havebeen described in the introduction to this com-pilation, the vapor pressure interpolated from the
experimental measurements [11-13, 16] is reported
in a portion of table 2.2 at 10 degree K. intervals.
The residual vapor pressure of re-pentane is shownin figure 2.1. In this instance the reference vaporpressure was established from:
log„P r= 5.587347-
24^3 '45
(2.1)
The marked difference in the measurements of
Young [9] from those of the other investigators are
clearly indicated. Other measurements of Sage
[10, 11], Li [13], and Beattie [12] are in rather
good agreement. The average fractional deviation
and the standard deviation of each set of the ex-
perimental data from the critically chosen values
are set forth for the vapor pressure of re-pentane in
the upper part of table 2.3. It is most likely that the
measurements of Beattie [12] and Li [13] represent
the most accurate measurements. However, the
paucity of experimental points made it necessaryto place some reliance upon the measurements of
Sage [11]. Young’s measurements were not given
much credence because of their large deviations
from the significant body of more recent experi-
mental data which has accumulated. Again, the
current critically chosen data follow closely those
recommended by American Petroleum Institute
Project 44 [16]
.
Values of the specific volume of the saturated or
bubble-point liquid and the saturated or dewpointgas also have been recorded in a part of table 2.2.
These latter data were interpolated from selected
measurements [11-13],
Figure 2.2 depicts the bubble-point volume as a
function of temperature and presents the data of
Li [13], Sage [10, 11], and Young [9]. The data
shown in figure 2.2 were based upon direct measure-ments of the volume in the condensed liquid extra-
polated to the vapor pressure. In this instance, it
was not necessary to utilize the residual techniquesas the variation in the specific or molal volume with
pressure was sufficiently small that direct graphical
operations were satisfactory. The agreement of the
several sets of data for the volume of the bubble-
point liquid in comparison with the critically chosenvalues are set forth in the lower part of table 2.3.
Values of the vapor pressure and the specific
volume of the saturated liquid, together with applica-
tion of the Clapeyron equation to calorimetric meas-urements of the latent heat of vaporization of re-
pentane [17], were used to establish the volumeof the saturated gas at temperatures below 350 °K.
Figure 2.3 depicts the residual volume at dewpoint for re-pentane as established by several
methods. The volume of the gas was smoothed in
terms of the compressibility factor which is defined
by eq (2.2):
Z^— PVJbkT (2.2)
In this instance, residual graphical methods weredeemed sufficient to permit critically chosen valuesto be established without the need of analytical
techniques. The reference volume at dew point wasestablished from:
Vr= bkT/P (2.3)
It is apparent that the calorimetric measurements of
Kozicki, et al. [17] and the volumemetric data of
Li and Canjar [13] are in good agreement whilesome of the earlier measurements by Sage andLacey [10, 11] yielded larger values of the residual
volume.After a review of the information presented in
figure 2.3, primary emphasis was placed upon themeasurements of Kozicki [17] and Li [13] althoughthe data by Young [9] and Sage [10, 11] at the
higher temperatures, for the most part, were in goodagreement with the critically chosen values. Theagreement of the results obtained from the calori-
metric measurements of Kozicki [17] with the
13
directly measured values of Li [13] Young [9]
and Sage [10, 11] yields credence to the critically
chosen values.
The standard error of estimate of the smooth data
from the experimental values is recorded in table
2.3. This includes a comparison of the agreementof the directly-measured specific volume of the
dew-point gas with values calculated from the appli-
cation of the Clapeyron equation to the available
enthalpy changes upon vaporization established
from calorimetric measurements [17].
The same information presented in tables 2.1
and 2.2 is also depicted in tables 2.4 and 2.5 in the
force-length-time system of dimensions, and the
results tabulated in engineering units. The standard
errors of estimate are equal tor the data presentedin tables 2.1 and 2.2, and 2.4 and 2.5, respectively,
but they have been repeated in the different sets
of dimensions and engineering units in table 2.6
for the convenience of the user. The graphical
methods employed in interpolating these data havebeen applied with different levels of agreement at
various ranges of temperature, thus requiring
separate measures of uncertainty for each range.
Accuracy— There is recorded in table 2.7 the esti-
mated uncertainty for the vapor pressure, tempera-ture, and volume of the saturated gas and saturated
liquid as measured by each of the several investi-
gators. These have been evaluated by the current
authors for each of the several investigators, while
the over-all summary of the probable uncertainty
in the results reported in tables 2.1 and 2.2 is set
forth in the lower part of table 2.7. It should berecognized that a certain element of subjective
judgment is required in arriving at values of uncer-
tainty which have been ascribed to the several
variables. For the most part, uncertainties several
times those assigned by the original investigators
have been reported in table 2.7.
The measurements of Young resulted from tech-
niques involving confinement of the hydrocarbon in
glass over mercury. Likewise, the methods of
measurement of pressure were considered to besomewhat less accurate than had been stated byYoung. The sample purity was relatively poor by
present day standards but Young’s [9] measure-ments on the whole represented an outstanding
contribution to the knowledge of hydrocarbons at
the time the work was completed. Somewhat later
measurements by Sage [10, 11], in the light of
this review, probably suffered in the gas phase fromadsorption on the walls of the steel pressure vessel
within which the hydrocarbon was confined.
The purity of the sample was inadequate to permit
the vapor pressure to be established within the un-
certainty of the pressure measurements whichaccounted for the somewhat larger measure of
uncertainty indicated in table 2.7 for the vapor
pressure than was originally reported by the authors
[4]. These measurements of vapor pressure by Li
[13] and Beattie [12] are probably as good as anyreported and the sample purities were adequate to
permit the estimated accuracy of vapor pressure
measurements to be of the same order as that esti-
mated by the author [12]. Some difficulties fromadsorption undoubtedly influenced the volumetric
measurements by Li [13] and Beattie [12] but
these were less serious than those found by Sage
[11]. The measurements of vapor pressure byBeattie [12] with a sample of relatively high
purity are considered of good accuracy. Thevolumetric studies by Li [13] were not considered
as satisfactory as Beattie’s [12] techniques andfor that reason a larger measure of uncertainty than
that indicated by the author has been assigned.
Kozicki’s [17] calorimetric measurements offered
an interesting insight into the overall reliability of
the volumetric measurements of the dew-point
gas. However, since the first derivative of the vaporpressure with respect to temperature was required
to establish the volume of the dew-point gas, a higher
uncertainty was assigned to the derived volumetric
behavior than existed in the original calorimetric
measurements.There are a number of correlations and reviews
of the properties of the paraffin hydrocarbons that
include n-pentane which were not utilized in the
preparation of the tabular information submitted. In
table 2.8, however, the more useful reviews are
described briefly [18-27].
14
300TEMPERATURE K
350 400 450
(/)
CL
LUCC3COCOLUa:CL
ocoCL
2
<3QCOLUcr
5
4
3
2
0
2
-3
•4
1
—
6
1
—API 44
1 ~T~ ~T~ n T~
rfo-
?-o •
BEATTLI
SAGE
E
j
YOUNG&
00
J \-O 0
r
^ -
-u
T
j _
CRITICALk
0.35
030
0.25
0.20
0.15
0.10
0.05
0
- 0.05
- 0.10
- 0.15
-0.25
-0.30
00 200TEMPERATURE
300
Figure 2.1. Residual vapor pressure of n-pentane.
15
RESIDUAL
VAPOR
PRESSURE
atm
BUBBLE
POINT
VOLUME
ft3/lb
300TEMPERATURE
350K
400 450
4.25
4.00
3.75
3.50
3.25
3.00
2.75
2.50
2.25
2.00
1.75
1.50
FIGURE 2.2. Bubble point volume of n -pentane.
16
BUBBLE
POINT
VOLUME
liter/
kg
RESIDUAL
DEW
POINT
VOLUME
ft3/lb
TEMPERATURE K
300 350 400 450
FIGURE 2.3. Residual volume at dew point for n-pentane.
TABLE 2.1. Critical properties of n-pentane
Source Temperature Pressure Volume
K Atm Liters/kg Liters/kg-mol
Young [9] 470.4 33.0 4.31 310.9
Sage [11] 470.4 33.6 4.36 314.6
Beattie [12] 469.8 33.31 4.09 295
Ambrose [14] 469.5
Partington [15] 469.6
API 44 [16] 469.49 33.16 4.08 295
Critically chosen value 469.49 33.16 4.08 294.6
Estimated uncertainty 0.7 0.2 0.04 2.9
Estimated uncertainty, percent 0.1 0.5 1.0
17
372-701 0 - 70 -4
RESIDUAL
DEW
POINT
VOLUME
liter/kg
Table 2.2 Properties of the coexisting phases for n-pentane
Temperature
Vapor
pressure a
Volume
Dew point Bubble point
K Atm Liters/kg Liters/kg-mol Liters/kg Liters/kg-mol
280 0.32 970.9 70.06 X 10* 1.561 112.7
290 0.49 656.1 47.34 1.586 114.4
300 0.72 421.0 30.38 1.616 116.6
310 1.03 328.4 23.70 1.641 118.4
320 1.42 241.8 17.45 1.672 120.7
330 1.93 181.1 13.07 1.706 123.0
340 2.57 138.2 9.970 1.739 125.5
350 3.38 107.1 7.728 1.774 128.0
360 4.31 83.4 6.017 1.813 130.8
370 5.45 65.92 4.756 1.855 133.8
380 6.81 52.67 3.800 1.902 137.2
390 8.41 42.31 3.053 1.952 140.8
400 10.3 33.07 2.476 2.010 145.0
410 12.4 27.74 2.001 2.073 149.6
420 14.9 22.50 1.623 2.146 154.9
430 17.7 18.19 1.312 2.232 161.1
440 20.9 14.60 1.054 2.358 170.1
450 24.5 11.57 0.8347 2.525 1&2.2
460 28.6 7.791 .5621 2.792 201.4
469.49 b 33.16 4.08 .295 4.08 295
a (Atm) (1.013250 X 105)= A'/m 2
"Critical state [16]
18
TABLE 2.3. Agreement of interpolated and experimental data for n-pentane
Source Number of Average a Deviation Standard c
of points Fraction b
Vapor pressure, atm
Young [9] 24 -0.164 0.0102 0.248
Sage [11] 22 -.010 .0044 .019
Beattie [12] 4 .005 .0003 .010
Li [13] 2 .001 .0008
API 44 [16] 10 -.001 .0018 .003
Overall d 38 -.005 .0031 .015
Dew-point volume, liters/kg
Young e[9] .. 21 -0.27 0.0050 0.62
Sage [11] 23 .23 .0077 1.21
Li [13] 2 .08 .0056
Kozicki f[17]— |
11 -.42 .0024 0.97
Overall 57 -.08 .0056 .93
Bubble-point volume, liters/kg
Young e[9] 21 -0.0303 0.0124 0.002
Sage [11] 23 .00071 .0008 .062
Li [13] 2 -.0687 .0030
Overall 46 .0164 .0062 .041
“Average deviation defined by^
(Gexp— Csm) J/A
“Average fractional deviation defined byj ^ [ (CexD— Ggm )/Gexp]}/^V^
I
c Standard deviation defined byjj ^ (Gexp— C,m )
2
J/(A— 1)J
1 '2 where G = pressure or volume
d Excluding Young’s vapor pressure datae Values of deviations for Young not comparable since data employed had been smoothed.'Calorimetric data for temperatures between 311 and 350 K.
Table 2.4. Critical properties of the n-pentane system, engineering units
Source Temperature Pressure Volume
° F psia cu ft/lb cu ft/lb-mol
Young [9] 386.96 485.4 0.0690 4.98
Sage [11] 387 494 .0699 5.04
Beattie [12] 385.95 489.5 .0655 4.73
Ambrose [14] 385 41
Partington [15] 385 5
API 44 [16] ..." 385.41 487.3 .0654 4.72
Critically chosen value 385.41 487.3 0.0654 4.72
Estimated uncertainty 0.4 3.0 0.0007 0.05
Estimated uncertainty, percent 0.1 0.5 1.0
19
Table 2.5. Properties of the coexisting phases for n-pentane, engineering units
Temperature
Vapor
pressure a
Volume
Dew point Bubble point
°F psia cu ft!lb cu ft/lb-mol cu ft/lb cu ft/lb-mol
40 4.30 17.2 1240 0.02491 1.797
50 5.48 13.7 986 .02510 1.811
60 6.89 11.0 795 .02532 1.827
70 8.56 8.95 646 .02556 1.846
80 10.6 6.74 487 .02580 1.862
90 12.9 6.12 441 .02612 1.885
100 15.6 5.108 378.7 .02634 1.900
110 18.6 4.325 312.1 .02662 1.921
120 22.3 3.643 262.8 .02691 1.942
130 26.4 3.104 224.0 .02719 1.962
140 31.1 2.660 191.9 .02750 1.984
150 36.4 2.280 164.5 .02779 2.005
160 42.4 1.978 142.8 .02810 2.027
170 49.0 1.716 123.8 .02842 2.051
180 56.5 1.494 107.8 .02876 2.075
190 64.8 1.306 94.23 .02912 2.101
200 73.9 1.145 82.61 .02948 2.127
210 84.0 1.008 72.73 .02987 2.155
220 95.1 0.8886 64.11 .03028 2.185
230 107.2 .7877 56.83 .03072 2.216
240 120.4 .6966 50.26 .03143 2.268
250 134.7 .6184 44.62 .03166 2.284
260 150.3 .5498 39.67 .03219 2.323
270 167.3 .4892 35.30 .03273 2.362
280 185.6 .4353 31.41 .03333 2.405
290 205.4 .3875 27.96 .03396 2.450
300 226.7 .3452 24.91 .03467 2.501
310 249.7 .3067 22.13 .03548 2.560
320 274.3 .2718 19.61 .03641 2.627
330 300.8 .2405 17.35 .03752 2.707
340 329.1 .2118 15.28 .03884 2.802
350 359.4 .1853 13.37 .04043 2.917
360 392.0 .1600 11.54 .04246 3.064
370 426.8 .1348 9.726 .04548 3.281
380 461.3 .1106 2.980 .05109 3.686
385.41 b 487.3 .0654 4.73 .0654 4.72
‘ (Psia) (6.89475 x 103)= /V/m 2
.
b Critical state [16].
20
Table 2.6. Agreement of interpolated and experimental data for n-pentane, engineering units
Source
1 !Number Average a Deviation Standard c
of points fraction b
Vapor pressure, psia
Young [9] 24 -2.41 0.0102 3.65
Sage [11] 22 -0.15 .0044 0.28
Beattie [12] 4 .07 .0003 .14
Li [13] 2 .02 .0008
API 44 [16]... 10 -.02 .0018 .04
Overall d 38 -.08 .0031 .22
Dew-point volume, cu ft/lb
Young e[9] 21 -0.0043 0.0050 0.0099
Sage [11] 23 .0037 .0077 .0194
Li [13] 2 .0014 .0056
Kozicki f[17] 11 -.0067 .0024 .0156
Overall 57 -.0014 .0056 .0149
Bubble-point volume, cu ft/lb
Young e[9] 21 -0.00048 0.0124 0.00003
Sage [11] 23 .00011 .0008 .00100
Li [13] 2 -.0011 .0030
Overall 46 .00026 .0062 .00065
a Average deviation defined by (Gexp-Gsm )j/A.
b Average fractional deviation defined byj ^ j\cexp — Gsm )/GexpjJ/A'.
c Standard deviation defined by| j
^ (Gexp— Gsm )zj/(1V— 1 ) where G = pressure or volume.
“Excluding Young’s vapor pressure data.
“Values of deviations for Young not comparable since data employed had been smoothed.'Calorimetric data for temperatures between 100 and 170 °F.
Table 2.7. Accuracy of experimental background for n-pentane
Quantity Units Young [9] Sage [11] Beattie [12] Li [13] Kozicki [17]a
Sample purity mole fr 0 95 0 9970 0.9985 0.9988 0.9998b
Vapor pressure percent 5 3 .2 .2
Volumetric behavior percent .5 .5 .3 .4 .5
a Includes uncertainty in dew-point volume calculated from Clapeyron equation.b Reported by vendor. The specific weight of the liquid and the index of refraction agree closely with critically chosen values. The reported purity seems higher than would be
expected.
21
Table 2.8. Reviews of properties of the paraffin hydrocarbons
Subject Treatment Reference
Vapor pressure
Vapor pressure
Vapor pressure
Critical constants
Critical constants
Vapor pressure
Thermodynamic properties
Critical constants
Vapor pressure
Physical constants
Correlation. Equation of state
Review and re-evaluation of experimental data
Correlation. Empirical constants
Correlation. Van der Waals constants
Review of experimental data
Correlation. Semi-empirical equation
Re-evaluation of experimental data
Correlation. Van der Waals constants
Correlation. Semi-empirical equation of state..
Correlation. Statistical theory of liquids
[18]
[ 19 ]
[20 ]
[21 ]
[22 ]
[23 ]
[24 ]
[25 ]
[26 ]
[27 ]
3. The Methane-n-Pentane System
The methane-n-pentane system has been subject
to significant experimental study at temperaturesabove ambient. However, only a limited investiga-
tion is available for temperatures below 37.7 °C
[28],
The vapor pressure of methane has been studied
extensively [16, 29-32], and the critical state of
the hydrocarbon measured [16, 29, 33, 34]. Like-
wise, the vapor pressure of n-pentane was studied
by Young and others [8, 9, 12, 13], and the critical
properties determined [9, 12, 14, 16].
The phase behavior and the volumetric charac-
teristics of the coexisting phases in the methane-n-pentane system have been established [35-38].
A comparison of the phase behavior of several
hydrocarbon systems containing methane, withparticular emphasis on the critical states, also hasbeen presented [39]. In addition, a review wasmade of the phase equilibria data for the methane-n-pentane system, and of similar data for other
binary systems [40]. No new experimental datawere included in either of the above reviews.
Utilizing the graphical techniques which havebeen described in the introduction to this compila-
tion, the aforementioned experimental data weresmoothed with respect to pressure and temperature.The composition and the specific volume of the co-
existing phases also were interpolated as a function
of pressure and temperature. In table 3.1 are re-
corded the composition, molal volumes, specific
volumes, and molal equilibrium ratios of the
coexisting phases for mixtures of methane andn-pentane. The data are reported at temperaturesfrom 280 to 470 K. for pressures from the vaporpressure of n-pentane to a maximum of 170 atmos-pheres. The data have been recorded for even values
of pressure expressed in atmospheres for each 10 K.
temperature interval. The standard error of estimate
of the smooth curves employed for interpolating
these data from the experimental results are set
forth in table 3.2. The characteristics of the uniquestates, including the critical state, the point of maxi-mum temperature, and the maximum pressure for
mixtures of constant composition, aie listed in
table 3.3. These values of pressure and temperaturefor each of the three unique states, as well as a
rough estimate of the specific volume for the
critical state, are reported as a function of weightfraction methane. The data recorded in table 3.3
were obtained by suitable graphical operationsbased upon experimental volumetric and phaseequilibrium data. The estimated uncertainties for
each property have been included in the tabulation.
Since many persons having an occasion to utilize
this information are concerned with the force-
length-time system of dimensions, the above de-
scribed data expressed in these dimensions are
reported in conventional engineering units in tables
3.4 and 3.5. The composition and the specific
volume of the coexisting phases in the methane-n-pentane system are reported in table 3.4, and the
properties of the unique states in table 3.5.
The standard error of estimate of the smoothcurves used in the evaluation of these quantities
is identical with that reported in table 3.2. How-ever, for the sake of completeness, it has beenpresented in table 3.6 and expressed in the units
used in tables 3.4 and 3.5. In preparing the tabula-
tions shown in tables 3.1 to 3.2, an effort has beenmade to present the data in sufficient detail to permitthe use of four-point linear interpolation in order
to evaluate properties at any chosen temperature,and pressure or composition with a precision at
least equal to the accuracy of the data.
In order to illustrate the nature of the phasebehavior of this system, a pressure-temperaturediagram showing dew points and bubble points
for three mixtures of constant composition and the
vapor pressure of n-pentane is shown in figure 3.1.
In figure 3.1 the effect of temperature upon the
critical state of the methane-n-pentane systemhas also been shown. Since it was, from necessity,
estimated from the observed volumetric behaviorat states near the critical state, the data have beenindicated as an estimated quantity. The critical state
for a binary mixture can be considered to be that
22
state at which the properties of the coexisting phases
become continuously identical. For example, the
critical state can be approached by an increase in
temperature under isobaric conditions or by an
increase in pressure under isothermal conditions
or by any chosen polytropic path. In addition, the
estimated maximum pressure at which two phases
exist for a given temperature has been indicated.
This state often differs materially from the critical
state for a mixture of the same composition, as is
indicated for a mixture containing 0.50 mole frac-
tion methane. However, this state has been called
“maxcondenbar” as being the maximum condensa-
tion pressure for a given mixture. It should be
recognized that the maxcondenbar becomes equato the critical pressure at the maximum two-phase
pressure for the system as a whole. The maximumtwo-phase temperature for a mixture of a given
composition also has been shown and has been en-
titled the “maxcondentherm.” It is again em-phasized that the loci of the maxcondenbar and the
maxcondentherm as well as the critical represent
estimated quantities established from measuredvolumetric and phase behavior and not from direct
observation of these quantities.
In figure 3.2 is depicted the equilibrium ratio as a
function of pressure for each of several tempera-tures. The product of the pressure and the equilib-
rium ratio was employed in figure 3.2 to permit the
data to be presented with greater precision.
The molal equilibrium ratio, K, is detined in the
nomenclature and represents the ratio of the molefraction of a given component in the gas phase to
that in the coexisting liquid phase at the sametemperature and pressure. This quantity is often
employed to represent the phase behavior of the
system since the ratio can often be effectively
employed in phase equilibrium calculations to
greater advantage than values of the compositionsof the coexisting phases.
It should be recognized that the equilibrium ratio
always is unity at the critical state, Thus in the caseof figure 3.2 the critical locus is identified by a line
crossing the diagram in such a fashion that the
product of the pressure and the equilibrium ratio
and the pressure are everywhere equal. It also
should be recognized that the equilibrium ratio
for the less volatile component becomes equal to
unity when the pressure is equal to the vapor pres-
sure of that component. The lower pressureboundary of the heterogeneous region is thus
established by the vapor pressure of the less volatile
component.The effect of pressure upon the composition of the
coexisting phases and upon the critical state hasbeen shown in figure 3.3. The curves shown in this
figure represent the phase behavior for a particular
temperature as the pressure is changed. The critical
state in this instance represents the highest pressureat which two phases may coexist for a given tem-perature. Such behavior can also be seen in figure
3.1. However, it must be recognized that in casesof mixtures of a given composition the critical state
is neither the highest pressure nor the highesttemperature at which two phases can coexistthroughout most of the pressures and temperatureswhere heterogeneous equilibrium exists. The esti-
mated locus of maxcondenbar and maxcondenthermhave also been indicated in figure 3.3, and for a giventemperature represents the dew point gas, in this
instance, containing the largest mole fraction of
methane. Figures 3.4, 3.5, and 3.6 show the sameinformation in terms of the force-length-time systemof dimensions expressed in engineering units.
Accuracy— For those interested in the critical
evaluation of the experimental accuracy underlyingthe information presented in tables 3.1 to 3.5, acritical review of the uncertainties associated withthe measurements of the several investigators hasbeen made and is set forth in table 3.7. In any suchevaluation it is difficult to maintain objectivity. How-ever, it is believed that the values of uncertaintypresented in table 3.7 have been arrived at byconservative judgment and formal statistical
procedures, such as described in the introduction.
The uncertainties assigned to each of the variables
by the current authors are from two to four timesthat reported by the original investigators.
It should be recognized that the majority of the
values reported in table 3.7 do not apply to the
behavior in the vicinity of the critical state wherethe uncertainties may be many times as great, since
these states were not established by direct experi-
mental observation. There is need for additional
experimental work involving the determination of
the critical state by visual observation and byindirect measurements of the intensive properties
of the coexisting phases, in order to permit anobjective appraisal of the accuracy with which the
properties of the system near the critical state have
been established.
23
PRESSURE
atm
275 300 325 350 375 400 425 450 475TEMPERATURE K
Figure 3.1. Pressure-temperature diagram for methane-n-pentane system.
24
PRESSURE
•
EQU
ILI
BR
IUM
RATIO
PRODUCT
atm
FIGURE 3.2. Effect of pressure upon equilibrium ratio for methane-n-pentane system.
372-701 0 - 70-5
25
PRESSURE
atm
0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9
MOLE FRACTION METHANE
FIGURE 3.3. Pressure-composition diagram for methane-n-pentane system.
26
PRESSURE
psiQ
Figure 3.4. Pressure-temperature diagram for methane-n-pentane system, engineering units.
27
PRESSURE-EQUILIBRIUM
RATIO
PRODUCT
FIGURE 3.5. Effect of pressure upon equilibirum ratio for methane-n-pentane system, engineering units.
28
PRESSURE
psia
0.1 0.2 03 0.4 0.5 0.6 0-7 0-8 0.9
MOLE FRACTION METHANE
FIGURE 3 .6 . Pressure composition diagram for methane-n-pentane system, engineering units.
372-701 0 - 70 -6
29
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-<= CL.
2 1
t- z«soc
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LU • o 6 OOOOOOOOOOOO O O O O 0 0000 OOO O O O O O O n O OOO O OOO O 0 O 6 6 OOOz oc UJ
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n cn 4- r- (Mcom^o^co^H O' n n >0 O ao O' 4- n mo® r- n m CM «H 0 0 cn n- cm NO pH n- CM X 0 >0 CM X05
ao >0 n U14444IM— O' 00 r*- >0 "0 m <n CM CM CM CM H F^ pH pH pH #H H •H H O' X X n- >0 >0 n n n 4 >* Xo 0 0 0 OOOOOOOOO 0 d d 0 0 0 OOO 0 600 O O O O O 0 O O 0 000 0 0 0 d 0 0 OOO
n n n n nnnnn-^'t^^ 4- 4- >1* 4- m m m m cn m CO m cn cn CO cn cn m cn cn m cn cn x m CM CM CM CM
o o o o OOOOOOOOO O O O OOO 0 0 0 0 OOO 0 0 0 0 0 0 0 0 0 OOO O 0 O OOO OOOLU LU UJ LU 111 111 UJ in ui ui 111 1 U 111 UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ LU UJ UJ UJ LU UJ UJ UJ UJ UJ UJc cn >0 ®NH>ofCi>tinofn n h- pH O' ao >o r*- 0 m m h N X cn CM m >0 CM X >0 nO n- O' pH 4 pH n n 0 n>0 GO CM S.D 4, M-lOh®fsj ao n m CM 0 n O O' F^ n O ® (M O' n m —a 0 x r*F v0 n cn cn CM H pH 0 0 4 X CM
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30
See
footnotes
at
the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
H H H H H H H pH pH H rgrgrgrgrgpgrgrgrgnjrgrgrgrgrgrgpgrgpg rg rg rg cm rg rg rg rg ph pH pH pH pH pH pH pH pH Oz ooooooooooooooooooooooooo O 000000 9 9 OOOOOOOOOOOOOh- III 111 111 L1J UJ LU UJ LU UJ LU LU UJ UJ ijj UJ UJ LU LU ill UJ UJ UJ LU UJ UJ UJ UJ UJ UJ UJ LU UJ UJ UJ UJ LU UJ UJ LU UJ LU UJ UJ UJ LU LU UJz or\jooop> 4 oinp-p- NOMf*3 «OmoOOH 0 0 4- m in 0 45 rg O' m C30N 4 ro X pg •p in pi in rg O' OO PPI 4 Oa! O^^O’tO'Ul^iAO'ON^ 4- O ©inosinggg in 45 00 O' -- <M m X rg X rg O' f- x HN 4 43 S' CM m 0 0
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orCD
rg eg cm cm rg N »H H H H »h fj pH pH pH 0 0 0 O O O O O O O O O 0 0 0 0 O O 0 0 0 0 O 0 O 0 0 O O O 0 O— LU= z o o oo o 00000 0 0 O 0 0 0 0 0 O O O O O O O O O 0 0 0 0 O O 0 0 0 0 O O O 0 0 O 0 O 0 OO' 11,1 111 liJ ill LU LU UJ UJ UJ LU UJ LU UJ UJ LU UJ UJ UJ UJ LU LU UJ UJ LU UJ LU LU LU UJ UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UJ UJ UJ UJ UJ LU LU UJUJ ^ pH pH ^ ^ pH 45 7* in in m m co in in 0 r- r- 00 r- 4) h- O CM H in m in 00 4- pH O' O' 0 0 CM in h- 0 4 r- 0 4 0 CO 4 0
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rg <NJ •—
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r-t h O' ® g oj rg p-4 H H pH d 00 r- 0 m 4- d ro m ro m CM pg rg rg rg CM CM rg pH pH pH H pH ^H pH pH pH pH pH ^H
H H rH H H H H pH ^4 H pH H pH pH pH p-4 pH •H pH pH ^H *H pH pH H pH pH H H pH pH pH pH pH ^H pH pH pH pH *H pH pH pH
T3 o o o o o 0 0 0 0 0 0 0 O O O O O 0 O O O O O O O O 0 0 0 O O 0 O O O O O 0 O O O O O O O OO
LU LU LU LU LU III 111 ill 111 HI UJ UJ UJ LU LU UJ UJ UJ LU UJ UJ UJ LU UJ UJ UJ UJ LU LU UJ LU UJ UJ LU UJ LU UJ LU LU LU UJ UJ UJ LU LU UJ(jh ^ o O' S' O O O 0 O p-H rg rg co ro m >0 GO O' ph rg 4- in r- O' *H m in r- O' H 4 O CO ^H CO pg 0 O' rg X 4o in in m in in in in in in x -0 43 4) 4) >
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h-o—1 111 HI 111 UJ 111 111 111 III LU III UJ UJ UJ LU UJ UJ LU Ui UJ LU LU UJ UJ UJ UJ LU LU UJ LU LU UJ UJ UJ UJ UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UJ UJ44444444 fr'<n rg -1 -- O O' O' oo >o in 4* CM pH CO in ro -4 O O' 00 r- >0 4) X r— X O' *H 4 X 0 X H ^ cm m XO o ^ H H H H H H ^ H H —
1
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s H »H <H pH c=) ^4 -J «=J H H ^4 pH o=3 pH pH pH H pH pH pH O' O' O' O' O' O' O' O' O' X X X X X X X X X X X X X X X_JCDCDO
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*: o o o o o OOOOOOOOOO 0000 O O 00000---- »H H pH pH H pH pH rg pg pg pg rg rg CO ro ro 4 in in
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o z o o o o o 00000000 O O OOO O O O OOO O O 0 0 O 0 C O 0 0 O O O O O O OOO O 0 Oi— UJ UJ UJ UJ LU Uj UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ uj UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UJ LU LU LU UJ UJ UJ UJ UJ LU UJ LU UJ UJ UJ UJ LU UJ UJ
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§ in in in m in m m in 4 4 4- 4 4 4 4- 4- m cn m ro m CO rT) m rr\ ro m m m m to CO ro <0 <0 CO CO ro CO CO 10 CO rg CMo o o o o 0000000 OOO O O 0 0 0 0 0 0 0 O 0 0 0 0 0 0 0 0 0 O 0 0 O 0 OOOO O O O
_l UJ UJ UJ LU UJ LU UJ LU UJ LU LU UJ UJ UJ LU UJ LU UJ UJ UJ UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UJ UJ LU UJ UJ UJ LU UJ LU UJ UJ LU UJ UJ UJ UJ<c co h n g so m O' 0 cm p- O' O pH co rg in rg O' m pH r- pg 0 pH pH 4) 4- 4- CM X X n n X r* O' rg in 33 rg r- pH in pH—
1
co O' m o no g p*g co 00 00 cO O' 43 4- rg *»h 00 cn PM m f- rg N» 4- pH GO 4D 4- CM pH O' X h- X in 4 ro <0 rg pH pH O O in O'
Q. s <0 rg rg —« -4 f4 H-4 incO rg rg p4 eH rH »-H rH oo r- >0 m 4- 4- ro ro m pg rg rg CM <M <H pH pH pH *H pH ^H pH pH pH pH pH pH O' X
LUOodooddoodd 0 0 O O O OOO O 0 0 O O 0 O odd O O O 0 0 0 d O O O O O O O 0 d 0 0
4 f«34 C0 Or^ 4 S'^S' rg O' m O' p-« O p-4 pH 4- m 0 4- 4) J0 GO 00 CO 00 CO r- 4 pH X 0^4 4 PS) O X ^ in X ro 4 O' h- O'
Li_ pm oo co r- pg in O' rg 4* in -1 m X r- o o -h m 4- m 45 43 0 43 45 45 45 4) 0 4) X 45 in in 4 CO rg pH O X r- in CO pH X CO 4 01—
OOhhN rg rg <0 in x t>- p- r- GO 00 00 oo 00 oo 00 00 00 00 GO ao X CO X X X X X X X X X X r- r- h- X X in X^ LUZc
o o o o o d 0 d 0 0 0 0 0 0 0 0 d O 0 0 d d 0 0 O 0 0 O 0 0 O O 0 0 0 0 0 0 0 odd O O 0 0 0 0
h-UJ
Ll. S o ® -- rp\ O' 00 CM 00 D N r- r- in ph in ^-4 r- 0 CT) m -O N h- r- h- r- r- r- O m 4- <M 0 X in r- (O x to X X X 4 Xo ® h i
n
0 in go 4“ 0s h rg fn 4 4 4 m in >0 4) 4) 45 O 43 45 45 4) 4) 45 45 >0 X X 43 x m m in 4 4 ro co rg pH 0 X 4 X_J
-- cm 4 4 m 4} 4) X CO GO O' O' 0 O' O' O' O' O' O' O' O' O' O' O' O' O' O' O' O' O' O' O' O' S' O' O' O' O' O' O' O' O' O' O' O' X X O'
o2 6600006600 0 0 d d 0 0 0 0 0 0 0 0 d d 0 6 6 0 0 060 OOO 0 d 0 0 d 0 0 0 0 OOO 0
CT5 c V noLUZ >0 oo O rg g- 0 00 0 0 0 000 0 0 0 0 0 0 0 0 0000 O O O O 0 0 0 0 O 0 0 O 0 0 0 OOOO 0 0 co CO
aP O O H H H <h .h eg 4 X OOOMtO 00 0 in 0 in 0 m 0 in 0 in 0 n 0 in 0 m 0 in 0 in 0 in 0 in 0 m 0 in 0 in X X Xto <r pH >-4 H »—h rg rg m 4- 4- m in 4) >0 p- r- co X O' O' 0 O pH pH rg rg to CO 4 4 in m X X X X mCdQ_
pH pH pH pH pH pH pH •H pH pH pH pH pH •H pH
31
See
footnotes
at
the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEW
POINT
BUBBLE
POINT
PRESSURE
3
MOLE
F
WTF
VOLUME
MOLE
F
WTF
VOLUME
EQUILIBRIUM
RATIO
b
ATM
METHANE
MOLAL
c
SPECIFIC
11
METHANE
MOLAL
c
SPECIFIC
11
METHANE
N-PENTANE
^,4.4p4*Hp4,4,4*4r4p4<MCM<M<MCM<M<MiMCMiMiMiM<M<M<M<MCMCMiMiMiM<MCMp4rHr4p4p4p4p4.4*4p4P40ooooooooooooooooooooooooooooooooooooooooooooooI I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I
mmLlJmmLi^yjijjmujiiJtjjijjijj'jjijjyj^ixiLUlUUJIiJIJJLUUJlJJliJUMUU^UUJ^lULJJlUUJUJUJUJUJUJUJUJUJ^o®'Oinaoi/M/iNO(Mfn 4, NMin>oo^N'ONmto>0 'O^Mn^©otf> 0'irun®'tfMio«tinfOOff>oCDNOfONN^O«tNOcO^OiN(3'r^OMiMfl>ONOOO<NJ't'00'M'ON©l/>OH(M^'OflOHi/>^ 0®0xr^xin-$->t, x<M^-4p4 00,00 h-o-xxxminintnininxxxxx^r,fc XXO'^*-<~*»4*4^cMCMX>frin*4
CM <M CM CM CM e4 H H *4 H H H H p4 0 O 0 O 0 0 0 O O 0 0 O 0 O O O 0 0 0 0 0 0 O O 0 0 O O 0 O 0O O O 0 O O O O O O 0 0 O O O 0 O 0 O 0 0 0 O O 0 O O O O O 0 O O 0 0 O 0 O O 0 0 O O 0 O OLU LU LU LU LU LU LU UJ LU LU LU LU LU LU UJ UJ UJ UJ LU LU LU UJ LU LU LU LU UJ LU LU UJ LU LU LU UJ LU LU LU UJ UJ UJ UJ LU LU UJ LU LUCM 00 00 p4 O' r- O >
0
H CM in X 00 0 CM h- -* in CM m CM x >0 H in h- <* in X 00 O cc\ -0 O' CM in r- O CM CM OCM CM H 00 O' h- 0 CM 00 in X *h 0 CM in x * oo x O' 0 x O' <0 >» CCS CM p4 0 O' 00 00 0 m in h- ccs x CM H 0CM H ^4 -4 rH 9.
00 4- x CM -1 ^4 p4 H rH 9.
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CM2.
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pH •4 *4 iH p4 p4 H 4 .4 4 H
1=1 r4 iH <=4 p4 H H H H *4 rH »4 pH *4 r4 *4 p-H 4 p4 4 4 4 4 p-4 p-4 t-4 4 ^4 4 p-4 ^4 r4 4 4 p-4 4 4 *4 rH 4 ^4 *4 *4 4O O O O O 0 O O 0 O O O O 0 0 O O O 0 0 O 0 O 0 O O 0 0 O O O 0 O O O O 0 0 0 O O 0 0 O 0UJ LU UJ of LU UJ UJ LU UJ LU LU LU LU UJ UJ UJ UJ LU UJ UJ UJ LU LU UJ UJ LU LU LU LU LU UJ UJ LU UJ LU LU UJ UJ UJ LU UJ UJ UJ LU UJP=H p4 H H p4 •4 CM CM CO CO CO H- H- in <0 >0 r- O' 0 CM CO in <o co 0 CM CO in r- O CM 0 co >0 p4 O' ^4 r- 0 >0 0 X *4
>0 >0 >0 X >0 O >0 -0 <0 X >0 >0 >
0
x sO .0 >0 0- h- 00 00 00 co 00 O' O' O' O' 0 0 0 4 0 CM CM X H- >0 0- 4«4 c=] ^4 p4 eJ i=3 *4 H ^4 ^4 «“4 pH *4 p-4 p^ ^4 •4 *4 *4 4 4 ^4 *4 4 *4 »-4 4 4 ^
4
^4 CM CM CM CM CM CM CM CM CM CM CM X0 0 660 6 6 6 0 0 0 O O 0 0 0 0 0 O 6 6 6 6 0 6 6 0 006 0 0 0 O 0 0 O O 0 6 0 O 6 0 0
cc\ x x x CO CO CO co CO CO CO CO CO co co CO <r\ r*i CO CO CO CO CO CM CM CM CM <M CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM0 O 000000 0 0 C O O 0 0 000 0 OOO 0 O 0 0 O 0 0 O 0 0 O O OOO O O O 0 0 0 0 0UJ UJ UJ UJ LU LU LU LU UJ LU LU LU LU UJ LU UU UJ UJ LU LU LU LU UJ LU LU UJ UJ UJ LU UJ UJ UJ LU UJ UJ UJ LU LU UJ UJ LU UJ LU LU UJ•0 >0 0 -0 X <3 x in in >* CO CO CM CM *4 O O' 00 0 in CM O 0 O >0 n in -0 O- 00 O <M 'O H- 0 ^ H- h- in X*
4
H H H H rH p-H p“H r4 ^4 H pH *4 —1 -H O O O 0 0 0 0 O GO 0- >0 in >t co CM 4 O O' O' 00 o- •i- -O O in in in 0 Xp4 rH *4 *4 pH c=H pH p4 pH ^4 *4 H 4 p“4 p-4 *4 p-4 p-4 -1 O' O' 0 O' 0 O' O' O' O' <* CO 00 CO ao ao ao X X X X X X
OO
6 0 OOO 000 O 0 0 6 660066 0 0 0 6 0 0 0 6 0 6 0 OOOO 0 006 O OOOO 0 0 0
x0 0 -• -• H H -c >4* nO O' H- O' CM >fr h # in CM O' >0 >t CM O' 00 c CO CM CM cm CM CO in n 0 in 0 4 X 0 X X — 000000 0 0 0 O O *4 H i*4 ^4 (M CM CO co >* in in -a r- 00 ao O' O -* rsl rr\ in >0 GO O' p4 CM 00 0 H- X CM X
* 00000000 O O 0 0 O O 000000 0 0 OOOO *4 p-4 ^4 4 -4 p-4 4 *4 p-4 CM <M CM CM CM X X X in H-
•
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0600 O O 0 0 O 0 0 O 0 6 O O 6 0 O O 0 O 0 0 0 6 O O O O O O O 0 0 0 O 0 OOO d 0 0 0 0 O
O•» ONKt’t in vO o- CD O* O' O O p4 f-4 r4 -i« 0 4- r- 0 CO ^ nO O- 1*- f- r- >0 >0 in n in in in >
0
X CM X N- X CM X 0 o-LU OOOO O 0 0 — CM CO in >0 X O' 0 <m in 0- O' (M -t 0 00 O <M H- >0 00 0 CM <0 oo O fNJ H- >0 X 4 X O O' X r- X O'at O O O O 0 O O O O 0 0 0 0 O 0 r“4 m4 4 p4 CM CM CM CM CO CO CO co CO >** H- >a- in in in in in nO sO O vO 0- X 0-
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O 000 0 600 O 0 6 0 0 O 0 0 OOOO O O O O 0 0 0 O 0 O O 0 O 0 0 0 0 0 odd O 0 O 0 0 0
LUCL X x x x co CO co co CO CO CO CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM 4 p-4 4 -4 p4 f4 p4 *4 *4 4 p4T.UJ4-
O 0000 O 0 0 0 O O O O O O O 000 O O O O O O O 0 0 O O O O O O 0 O O O O O O O 0 O OUJ UJ UJ UJ UJ LU LU UJ LU UJ LU UJ UJ UJ UJ LU LU UJ UJ UJ UJ UJ UJ UJ JJ LU UJ LU UJ LU LU LU UJ UJ UJ UJ LU LU LU LU UJ UJ LU UJ LU
>* 00 CM CM co in O' >0 CM »4 j- O in 00 in ^4 (M in 0 in CO CO r* CM 0 O' O' O CM in in CO in *4 0 rO X >0 in in X 0 inin CM O' h- in CO H H >0 CO *4 in CO co in O' 00 O -t 0 O cO P-4 O' r- >0 in CO <M CM *4 0 GO CM >0 4 O p4 >0 CM X 0 X 0-i- h- x co CO CO CO CM pH p4 •-4 O' 00 0- vO in H- H- CO CO CM CM CM H 4 4 4 *-4 ^4 ^4 p-4 p-4 O' X ao O 0 in in in >* >*
0 O 6 0 O 0 O O O O O 0 0 0 0060 0 0 0 O 0 O 0 O 0 O 0 d O O 0 O 0 O 0 O O 0 0 0 0 0 0
in in m in in in in >t -t H- H- 4- H- H- >$ CO CO CO CO CO CO CO CO CO CO CO CO CO co CO CO CO CO CO co CO CO CC\ X X X X X CM0 0 0 0 0 0 0 0 O O O 0 000 0 OOO 0 0 0 O 0 0 0 0 0 0 O 0 0 0 0 0 O 0 O O 0 0 OOO OUJ UJ UJ UJ UJ LU LU LU UJ JJ LU UJ UJ LU UJ UJ LU UJ LU LU UJ UJ LU LU UJ UJ UJ LU UJ UJ UJ LU LU UJ LU UJ UJ LU UJ UJ UJ UJ UJ LU •JJ
O' O' O' 0 CO O O O' CO CO 0- 00 r- 0 0 -4 O' t h- 0 vO CM O in X) 0 NO co OJ ^0 >0 >fr H- n O' CM >0 O' X r*- *4 inO' x O' o- in O CM O O' O' CO O' >0 H- rO p-4 oj in n O' CO O in (M O' h- in CO CM 0 O' CO 0- >0 in <0 rO CM •4 *4 0 O H-CM CM H H H rH —4 >0 CO CM CM -4 f4 p-4 *4 O' 0- >0 in >fr rO ccs rO <M CM CM IM CM <M p-4 4 p-4 -• p4 4 <4 t4 -4 *4 4 4 p-4 O'
O O 606 O 0 6 O O _> O 0 O c OOO 0 0 0 O O 0 O O O 0 O O O O O O 0 O 0 0 O O O O 0 O 0
O- O X CO O' H s0 O' (M O >fr *-« p-4 0- O O' *-4 m 00 >0 CO in in n in in H- CO p-4 00 H- r- O CM co CM O 0 CM in in O' O' ^4CM OO CM >0 O' CO in vO n CO 0- 1—
H
CO H- >0 >0 O' 0 4 CM CO CO CO CO CO CO co CO CO CO CM CM •-4 4 O O' ao r- in 'T f\J 0 X >* O' CMO O H H cm 'm >* in >0 >0 C'- 0- r- oo 00 00 00 00 CO 00 ao 00 co CO 00 CO 00 00 00 OO ao X X in in
O O O O 0 0 0 d 0600 0 006 600 OOO 0 0 0 0 0 0 O 0 dod O 0 0 0 0 0 O 0 0 0 0 0 0
inx00
o
f0 H!Yjv0 Mf\Q0 a'NinfnN 41 O'tN>ta'ffnANNC0 C0 C0 ®C0 C0 NN>0 >tfn^C0 in 0yJaDm»Min 0 ^OO COr4 XO'xcMr*-oO'inxo^cMcoxx>t, >$* lxininininininininininininininin>fr--$, 4'xx<MrM^OO'^x ^rHCMX-^ininXO-XXO'O'O'O'O'O'O'O'O'O'O'O'O'O'O'CJ'O'O'O'O'O'O'O'O'O'O'O'O'O'O'C^O'O'XXX O'
0000000000000000000000000000000000000000000000 o
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QHHHHH(\|»t>OcOOfM't'OcOOIf'OinO^O^O^OinOino^Ol/'Olf'OiroiAOl/'O^O^NO^*4 .4 .4 r4 .4 <M<MXx>$*-4*ininxx^r'-xxO' 0' 00 *H~«cMCMXx>$, >rininxxxxx
32
See
footnotes
at
the
end
of
this
table,
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
“ a-© i
O' «C
<4 H *4 ^4 e4 ^4 H *4 H H H *4 H »4 e4 »4 4 <=a H •4 4 »4 H •4 r-4 •4 ^4 4 ^4 >4 *4 *4 •H 4 ^4 4 4o O o o <n o o O o o o o o o o o o O o o o o o o O o o o o o o o o o o O o o o o o o o oO
UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ UJ UJ UJ Ul UJ Ul UJ UJ4 4 4 4 4 in in >0 C** h- QO r- O' o <N co 4 <0 O' H co 4 <o 00 o OJ in h- o m <0 o 4 O' m Csl ^4 co o co m
O >0 o •o 'O <o •o <0 o 'O >0 vO >0 >o O r- r- r«- f~ GO GO 00 CO co O' O' O' O' o O o 4 H H eg co 4 in e- O' coUJ H c=4 •4 H •4 H H 5=3 H r4 *4 -* <4 r4 4 4 H 4 4 H »4 *4 H 4 CM eg eg <NJ fVJ eg eg IM eg eg eg eg co
a.UJocQ-
Oe4CO
oUJo
QC
CLXUJ
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOI I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I
III III III 111 III Ml ’ll III III III III 111 I . I III III 111 111 III 111 111 III III III Hi III 111 III III 111 111 III III II 111 III 1 1 I 111 I 111 III III III III
fn<\iroh-M®0'04r'i-*040'Oin<'>joO'0-*{»)inr-0'<\i'004oo-*<\ir^4'0®04®inir>.oo
eg eg eg eg ^4 H 4 *4 4 r4 *4 H 4 o o o o o o o o o o o o O o o o o O o o o o o o o o o o o o oo O O O o o o o o o o o o o o o o o o o o o o o o O o O O o O o o o o o o o O o o o o oUl UJ Ul Ul UJ UJ UJ Ul UJ Ul UJ UJ UJ UJ UJ UJ Ul UJ Ul UJ UJ UJ Ul UJ UJ UJ UJ Ul UJ UJ Ul UJ UJ UJ Ul Ul Ul UJ UJ UJ UJ Ul UJ UJh* »n GO in eg CO >0 GO *4 o e- o o eg <0 f*- o GO o eg 'i- o O' eg o eg o GO GO GO O' .4 CO in r- o CO x\ e- O' o O' oin co ^4 o 4 4 CO O' o ro eg o >0 oo •XI <0 o 4- o 't eg O' GO >0 in 4- eg 4 o O' O' GO h- x> -o in 4 CO eg eg o oi. *4 <4 «4 O' 4 co eg H »4 4 4 4 9.
f**6. XI in 4 <0
3. CO CO eg eg eg eg eg eg eg 2. 4 ^4 ^4 •4 ^4 4 r=0 4 ^4 *4 4 ^4 <4
ooooooooooooooooooooooooocooooooooooooooooo
oooooooooooooooooooooooooooooooooooooooooooIII III 111 III III 111 III III III III III III III III III III 111 ill III III III III III III III III III 111 III III 111 HI III III III III III ill III III III III II
H^rfH-HH-HH^Hrt-HrfOOOOOOOO(MtNi^+flNN-lOO(f»(M>0-l^H H «4 H ^ H ^ H H ««4 ^4 H ^ H H H H H H *4 ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ GO ® CO CO O O' O'
000000 3 OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO
OOHrfH(<10®OMIfH»0«^'0(M9''OmO®^mrtO'®^iOKM(MflMJ'Nie(MO-4IJ'C\|lftONi*>00000000"*<-»-*-<<''Jf''l<\lc*>4't- m'0^r“®0'00-«<\(fr>4lf\Of*-®0-*f'>mh.O'frir'-400000000000000000000000000>H-^---4—OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO
oooooooooooooo-*-**--<<M<\i<\i<\jr'j<nro<t>«nro44444minir»mifi.o.O'Or-r''-®f'-ooooooooooooooooooooooooooooooooooooooooooooo
ooooooooooooooooooooooooooooooooooooooooooo1 1
1
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1
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ill m m in ijj ill in m iii in iii m m m m in m m m m m in m i|p ^ iji m m nf
m in nf ifi up m
40'-0<,''»''l<'r>-*rr>4m'0-<P'J4m04'-, '0«4ir'®4<-*00<''44'0®ir>«4m^(''JO'r-ir>P'J®f\JNOO'BMMnoiOOO'-.feNO^O'Om-O'N'Oin^OlN^OO'fONNNNSflO'iO-iO-ih-h—»-H^^H 0'O'®®h-f^'0'0inir\i/\'t't
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOul ill 111 III ul 111 ill 111 ill III ill in ill m ill ill ill ill ul ill ill ill ill m ill iii iii iii nf ill ill ip m nf yi up i|f i/i
in Ul Hf mrOif*f>>o<Nir\Of“iftrrt'#, »*'*orN>OP»®<7'rr>®O»-*^h-O'r'J®i«n'i<\ir\jiriior-0'c^.oo<*lf,-Oosifi(<>N-irf04, OM<M*i(Mio®'ONOiftONn^aiO+(OrtOO'fflN^in^<*iffwMN-400(MrtrtHw0^mM(M-IH-l-l5'N^IOK\^^(»l(flffl(M(MMPgNN-lrf»4rii-lrf»l-l^F4rt-iHOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO o
*0'tO(<if'^ffi'0'Of'*4’0'0'irio®if\'ONr'Nf'NN^io^('>rfOi'^0'0<M'OOHrth.mo' r-®®>0<*'®^04'0®0'0.-|—i<''j'r'444-J’444444'r4444r'i''ri(*'o<'i(\jr''j—<-*oo'r-u'\—* -r—l(\lf«^44f“®®®®®0'0'0'0'0'0'0'0'0'0'0'0'0'0'0'00'0'0'0'00'0'0'0'0'0'00'®®®® O'• •••••••«••••••••••••••••••••••••••••••••••• •OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO o
• ¥ *0f\l4'0®OQOQOOQOOOOOOOOOOOOOQOOOOOOOOOOOOOOOOOO^-«inHHrf-HM't'0#ON*'0®OlftOH'OlflOiflOiflOiflOiflOiflOiflOK'Oi<'Ol/'OlflOlf'Otf''flN'f
33
See
footnotes
at
the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEW
POINT
BUBBLE
POINT
PRESSURE
3
MOLEF
WTF
VOLUME
MOLE
F
Ff
VOLUME
EQUILIBRIUM
RATIO
b
ATM
METHANE
MOLAL
c
SPECIFIC*
METHANE
MOLAL
c
SPECIFIC"
METHANE
N-PENTANE
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOI I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I
111 111 til in ii* m m ill m hi in m m ill m ii* ill m in ill ill m ill ill ill 111 ill 111 in in ill 111 ill 111 iii m iif ^ iflp
CM eg H H pH pH pH H o o o o o o O o o o o O o o o o o O o o o o o o o o o o o oo o o o o o o o o o o o o o o o o o O o o o o O o o O o o o o o o o o o o o o o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJCO 0- CO O' in O' in O' 4 'I- co in in 4- CO eg CO e- 4- 4- r- CO <6 o x 4 co 4 f- m m O' 5 ® oCNJ CO CO o 4> h- m 4 o o •c 4> co co O' o H H <0 h- 4- CM pH CM ro 4 o 00 O eg 4 o f- CO <o oCM o O' fM 4 0" o 4 eg o o f*p CO •h in 00 in CM o CO h* in 4- CO CM ^H O O' 00 r- 4> 4> in 4 co eg pH o o
1. 9. 4 (O CM pH H pH H pH CO >0 in in 4- 4- 3.co co m CM CM eg CM CM CM CM CM H pH H H -4 ^H
o o o o o o o o o o o o o O o o o o o O o o o o o o o o o o O o o o o O o o O o o pHo o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o O o o o o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ4 4 m GO eg r~ H 43 -o CM p^ pH in o m o m CM p» 4 CM o o CO m o >0 m >0 H CO CM •o o eg eg h- o m o 4f* h- e- e* CD CO O' o o o H fO 4 o h- o o eg co in h- o pH co m t- o m >o o CO 00 CO o co ao pH o o CO>0 >0 <o o X <0 <o 43 h- e- P*» h- f» p^ CO co ® co co 00 o O o o o o o H •M eg co ro 4 43 CO o >0 <o
1. 1. 1. l. H H pH H H H pH c=4 pH pH H H 1. H eg eg 2, 2. 2. 2. 2. eg CM eg eg (\j <n3. 0.
CM CM eg eg eg eg eg eg CM eg eg eg eg eg eg eg eg CM CM eg eg cm eg eg eg pH H pH pH H pH H pH pH pH pH pH pH ^H CM fOo o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ
43 lO o cei e* -H in o 4 co cn O >0 (p( pH CO 4) eg pH o o O -1 o CO *H CM c o o in r*- eg o eg oo P- o <0 CO
o o o 0s ^ co co h* p» O in m cn eg ph o ® <0 m 4 cn eg m o eg CO m h- O eg 4 GO CO o o O' 4 h- -l oeg eg CM pH pH pH pH pH pH pH pH H H H pH pH O O o o O o o o o o GO ^ >o m in 4 CO CO CO CO eg co 4 <0 O -H
H pH pH pH pH *H pH <=} ^4 pH pH H pi H pH «=4 pH H pH H pH pH -H O o o ^ O' S' O' <y O' <7* ^ O ^ -i o
&
^ 00000000000000000000000-*-^>^^-.>H^-*.-i^r\ir\j(Ncg<\|('<3(r*44<'^• ooooooooooooooooooooooooooooooooooooooooooooUJa
®a5r^ir\-fo^<Mf^tNjao(*>r-h-ino'®ooir>'0(Nr-®h-r~^irif~fMOrr\f^f^r^oif'rrico(M(M» o^<M<\i<N<M-*-*ooff, i?'<\iifi®o<M4ir\in434N4<r'<Ni'-io<?'®®®®o,'»Hmo®04f>,-'0®rr
i
uj ooo—<<M®44'iNor-r^®-gr'3ir\®o<M4-o®o<M4'0®o-grriir>r,-0'^44><?'-g4®f'JOOQas oooooooooooo»*i-i'^>*<\i<'g<N<\i<\ir*'immrnm 444444 'rii/'mu'v®®«or»f'-®f'-3h»<
00 o O O o 00 o o o o 00 o 00 O 00 000 o 00 o o o o o o o o 00 00 o o O o
UJa. cm eg eg CM eg eg ^H pH pH pH pH ^H H pH »H pH pH H pH pH pH pH pH ^H pH pH pH pH pH o o o o o O o o o o o O pHs o o O o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o n o o o o o o1-=* UJ Ul UJ UJ Ul Ul UJ UJ (U UJ UJ UJ Ul UJ Ul UJ Ul Ul Ul UJ UJ UJ Ul UJ Ul UJ Ul UJ Ul UJ UJ UJ Ul UJ UJ UJ Ul UJ UJ UJ UJ UJ
eg co h- r- O' GO O' 00 o o o CO ® O' H O CM eg eg e* H O' 43 >0 o co CO o eg e- in o o eg CM CM O CD pH 4 00 4eg >fr r- in eg O' 4 00 CO CO CO CO CM o oo in 4 4 CD <0 pH o pH eg 4 h- O O' •H CO oo o 4 pH o e- D pH eg COco eg pH <0 co H >0 >* 4 h» pH >0 >o O* 4 O' 4> co -i O' >o in 4 co eg pH o o C0 CO eg e- CO ® 4 O' in pH O co
eg cm eg pH H ^H O' 00 0- o •a in 4 n CO CM CM eg eg ph pH pH pH *H H pH pH pH pH O'’ 00 oo e- n >0 >o in in in 4 4 o
4 4 4 CO CO co CO co CO CO CO CO eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg eg CO
O O O o o o o O o o o o O o o o o o o o o o-o o O O o o o o o o o o O o O o o o o OUJ UJ UJ UJ UJ Ul Ul UJ Ul UJ UJ Ul UJ Ul Ul UJ UJ Ul UJ UJ UJ UJ Ul UJ UJ UJ UJ Ul UJ UJ UJ UJ UJ Ul UJ UJ UJ Ul UJ UJ Ul UJeg eg in 0- ^H CO o D CO •0 O' 00 (O o eg r- co o co co 4 CO o 0- o eg eg in pH O' in pH 4 M >
0
in e- eg 00 CO X COin 00 4 r*- o 4 pH 00 00 in e- CO eg eg o ® r- o ci 4 pH CO O O' CM co pH O' O' O pH m in CD ^H •n X eg CO oin co eg eg pH H in O o- in CO eg 00 •H O' O' eg 0- <SJ ® in eg O' in 4 eg •H o co >o n co CO eg ^H o pH
i. pH i. 6. 4. 3. eg eg 1. i. i. i. O' 00 Dinin^M'cococoegeg rg eg 2. eg eg i. i. i. i. i. i. i. pH ^H 1. pH 1. 0.
og04<\i<M4~<ff'CT''0-Hm®<Ni04-*ir\r-0'ooO'i3'®ir\<N®<\iinf^®®r-m<7'.<\iroo<y'44 o(M4’r>®®ir\>4'fr^orriir\®^m^.ir\u>triin<o®ir\irti/>mtrt^'<ff'i<M>400, ®<oinm^r>^<® -o
oooooooooooooooooooooooooooooooooooooooooo o
4Of-4-0<?'44>-.mir\4®r'-4®—•<\irri44444i'’'i ,N'*o«4Nn'i<?'4>-*-0'^443in-<®® 4Q H ^ ^ N ^ 00 CO 00 CO 00 CO ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ CO 00 00 CO 00 CD ^oooooooooooooooooooooooooooooooooooooooooo o
• V w®®000000000000000000000000000000000000000®irif0rtrtN^<ao(M<fj«oinoiftomoifioinoif>oifioinoiftOK'oiftOiftoinoiAOKMr'NN
34
See
footnotes
at
the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THEMETHANE-N-PENTANE
SYSTEM
-
CONTINUED
CO oCOCO
oUJQ
oc.
3H-<0£UJaxUJ
<\J H .4 •H *4 H H o o o o o o o o o o o o o O o o o o o o o o o o o o o o oUJ o o O o O o o O o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o o<c UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ Ul UJ UJ Ul UJ UJ UJ JU Ul Ul Ul UJ Ul UJ UJX GO •o p- 4- O' o o> o O' CO CO >0 O' ^4 <o co O' CM 0- CM CM iH o in 00 •0 O' co 4- CM GO GO 4} 4> 4- oUJ o m n- m CO O' -0 p* 4^ CM CO in O' in 00 00 CM o CM m ^4 GO o in 4" 4- in in <o 00 o ^4 CO in in 4- oz o o CO in o 4- CM ^4 o co CP O' CM >0 CM 00 in CO O' p- >0 4- CO CM *4 o O' oo p- sO 'O in 4- CO CM ^4 o
•4 in CO CM CM ^4 «-4 H H 00 >0 in in 4- <* 1*1 CO CO co CM CM CM CM CM CM CM CM H *4 »4 f4 ^4 r*4 *-4 *“4 ^4
o o o o o o o o o o o o o o o O o o O o O O O O O O O O o o o o o o o o o o f-4
o o o o o o o o o o o o o o o o o o o O o o o o O O o O O o o o o o o o o o o oo
UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ Ul UJ UJ UJ UJ UJ UJ UJ Ul UJ UJ UJ UJ UJ UJ UJ>0 o * 00 4^ oo 4- GO CO O' CM m o in o m H 00 in CO CO 4- >0 O' CO H *4 in CO o n P- in oo r- 00 f«4o o CM CM CO CO 4- X* <0 p» O' o CM co in •O 00 o CM 4- <o GO ^4 4- P- o 4^ 00 CO oo in 4- in O' CM O'
UJQ-
p- p» h- p* P- p*- P» P- r*- p- p- 00 00 00 00 oo 00 O' O' O' O' cp o o o •4 ^4 rW CM CM CO 4> m 4> O' CM CO
- <4 -4 H *4 c—
«
H H -4 H *4 r*4 s4 h f4 c4 f=4 ^4 o=4 CM CM CM CM CM CM CM CM CM CM CM CM CM PO o
CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM *4 f4 f-4 f4 *4 *4 f4 f-4 t4 r4 CM COO o O o o o o o O O O o O O O O O o O o O O O o O o o o o o o o o o o o o O O
_l UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul Ul UJ UJ UJ UJ UJ UJ UJ Ul UJ UJ Ul UJ Ul UJ UJ Ul UJ UJ UJ UJ Ul Ulo 4- 00 cm p- .4 >o o 4- CP .0 CM o p- in CM o O' 00 oo OO O' o CM 4- p- P- O' P- in 4- 4- <o *o 4- 4>
o PO CM ^ o o O' O' 00 p» m 4- CM h o O' p* o m 4- CO CO <M O O' CO p» O' CM 0- *0 o f4 00 CM H o2 <N CM CM CM CM CM H H .-4 f4 <=4 •—4 o o o o o o O O o o O' O' 00 p» P- o «
0
>0 P* O' o *4
H H H H H H H H H H H H H H ^ H ^ »4 H H H H ^ H H H H ^ ^4 H f4 H »4 H ** f4 OoooooooooooooooooooooooooooooooooooooooI I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I
III ill III ift f
i^i qi III ill m m Hf 11 1 m ||| III ill III HI 111 til Hi til III III III 111 m III II* ill 1 1 1 I|f III H
^III
oortooo^(\M)oaonNooo'OinN^soaO(*un*j'rtNstojNNN*soJo^swosoin'tflNHrfOooo^rf-M'JN <N,r^ -tm-ON®ON.t®H^inoo
0<''J't'Oco»-f*>i/>F-oif'-<®4'0*“4--*coif'<\lOF-if><*if\ii-i-*-HfriF'-»*h-ift^i**<sjr'-.o4-
OOOOOHWHrtNMn®^UMflONN®J'OOHNM'tK\^^®O^Cl®«IMI'O0'OOOOOOOOOOOOOOOOOOOOO-H-i—i-i-i-H.-i-i^.j<\|i\l<\l<\lcgf*ir<1 .1-<\|
oooooooooooooooooooooooooooooooooooooooo
^O^0'(M«NHrtHNOHJ'n^N.f^^0^®O>0(fN+®HMflOmNN<|No-<-iNmj’in®f'aoNii>so'^rtrf\Nff'iHrti/\s®oN^®eoK>iA»oi,'®rtaiftOOOOOOQOOO'<HrtHHniN(MNNK\®®mrt<'^*4’4, lfl®®lft«4).ONN40. o 0, o O o o 0. 0. 0. 0. 0. o 0. 0. o 0. 0. 0. 0. 0. o o 0. 0. 0, 0. 0. 0. 0. 0. 0. 0. o o 0.
o<0. 0.
CM CM CM CM ^4 ^4 f4 f4 ^4 f-4 1*4 f4 fH f=4 «4 •4 »4 e4 *4 f4 4 *4 f4 «4 f4 f4 O o o o o O O o o O o O *4O O o O o o o o o o o o o o o o o o o o o o o o o o O o o o o o o o o o o o oUl UJ UJ Ul Ul UJ ULI Ul UJ UJ Ul Ul Ul Ul Ul UJ Ul UJ Ul Ul Ul UJ Ul Ul Ul UJ Ul UJ UJ UJ Ul Ul UJ UJ Ul Ul Ul UJ UJGO 00 4- in o h- CM in 00 f—4 X C0 CM o 4- 4- o o oo co 4) O' co f*- O' 'o PO in p- CO p- X p- PO 4 O' in 4o in -4 co H O CM in oo O' -o *4 *4 CM o 4- CM co NO CM o o o *4 CO >0 4- >0 PO CM 4- X in 4- 4- CM O'00 4^ (M r> o O' ^4 4- 00 co 4- 00 CO O >o CO ^4 O' >0 in CO P0 CM c=3 o O' CO CM P* CM p» co O' in **3 >0 CO
1. *4 •^4 O' r*-6. 5. 5. 4 3. 3. 2.
CM CM CM 4 *4 •4 i. *4 ^4 *4 *4 1. 9.O'
8. X P» 7, o >0 in5. 5. 0,
4- CO CO CO CO co PO CO CO CO CO CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM CM <M CM CM CM cm CM CM CM POo O o O o o o O o o o o o o o O o o O o O o O O O o o o o O o O o O o o o O oUJ UJ UJ UJ UJ Ul UJ Ul Ul Ul UJ Ul UJ Ul UJ UJ UJ UJ Ul Ul Ul UJ UJ Ul Ul UJ Ul Ul Ul UJ UJ UJ Ul UJ UJ Ul UJ UJ UlCO 00 4- CM O' 00 O' oo o CM o *4 r*- O' h- f4 O' oo O' o oo 30 CO o >0 in o o 4- >o in PM X O' CM in 4- P->0 oo *4 >o PO CM O' CM P- f-4 *4 p- >0 p- h- m in O' p- GO >4 in ^4 X p- -0 >o p^ O' 4 co 43 O CO oCM CO CM CM in CO in 4- CM o PO *4 f4 4- 00 CO O' o C0 o 00 n0 in co CM o O' X >0 n in 4- CO P0 CM f4 »4
4 N0 4- (O CM <M f4 f4 H *-41. 8. 7.
>0 5. 4- 3. 3. 3. 3. 2. 2. CM cm CM 2. 1. 1. •4 i. i. *4 4 *4 1. 1. 4 o
MO‘-<ONO'WirMflifiBMMHifi®ac®oo-<N^iri®-i(r.®sBifiPuao'ON®0‘^Oa'f-®Sf-9'®®n^aO®(M®^NSN®^FlJ)ON4®®K>O®»(M»n®o«OMfla-<^'OBNirw'®ooH-i-i-iHri-i-HootMoi'iin4MOff'>o^<i
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOO
oif\*'sjf>-a'aD4-^ir\rri^-friooo>of^aoa'000'0'®r~ir\rooh-oo'^, oo<Mir\f^or'h-
o in*jn-p*-xxxxxxxcpo'^o»O'O'a'<7'O'a‘(7'O'0'0'O‘<7'O'C7'XXxxxxxxn-ooooooooooooooooooooooooooooooooooooooo
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35
See
footnotes
at
the
end
of
this
table.
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEW
POINT
BUBBLE
POINT
PRESSURE
3
MOLEF
WTF
VOLUME
MOLE
F
WTF
VOLUME
"
EQUILIBRIUM
RATIO
b
ATM
METHANE
MOLAL
c
SPEaFIC
d
METHANE
MOLAL
c
SPECIFIC
11
METHANE
N-PENTANE
H H »-4 H H H H *“4 H H H H H H H H H H H H H H H H H H H H H H H ^ H OooooooooooooooooooooooooooooooooooooooI I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I I
UJUJUJUJUJUJUJUJUJUiUJUiliJUiUJUJUJUJUiUillJUJUJUJUJUJUJUJUiUJUiUilUlilUiUiUiiiJ
H c—1 «=4 H H o o o o o O O O o o o o o o o o o O O o o o o o o o o o oo o o o o o o O o o o o o o o o o o o o o o o o o o O O o o o o o o o o o oUJ UJ UJ UJ Ui UJ UJ UJ UJ UJ Ui UJ UJ UJ UJ UJ UJ UJ UJ UI UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UI UJ UJ UJ UJ UJ UJo o cm in m CO 4- —
1
o O' O' in m GO ^ o rr\ CM h- r- 4- CM GO CM O' O' o ift 4- O' in h* r** cm oo in O' r*» m GO O 'O 4- ^4 m in CM in O' <\l CM •0 4- m ® <*) o GO •o o n in >0 <0 GO O' h *4 o a oH 4- in o r- 4- cr> •4 O 4- o o m h- «M O' <0 *»4 O' f- o m m CM *4 O O' GO r- ® in 4- 4- fOCMO om 3. eg <M -i H H H 8.
h- •o in 4- 4- <»>3. 3. 3. 2. 2.
CM2. 2.
CM IM2. 1. •4 H H ^4 *4 H H *4 H -4
o O O O o o o O o o o o o o o o O o O o o o o o o o o o o o o o o o O o o •Ho o o o o o o o o o o o o o o o o o O o o o o o o o o o © o o o o o o o o oUJ UJ UJ UJ UJ UI UJ UJ UI Ui UI UJ UJ UJ UJ UJ UJ UJ UI UJ UJ UI UJ UJ UI UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJm r- CM o in o in o 4* 1^ CM GO m H o m <M O o 4* GO 4- CM PO CO >0 H CM o 4- in O' * 4- in O'4* 4> in in o >0 r* GO O' o CM m in GO o CM 4* o GO o CM in GO ^4 4- GO m CO 4- p4 o CM 4 O' ^4 O'h- h- h- r- h- r- 00 00 00 GO GO GO O' O' O' O' O' o o o o *4 H CM CM m 4- in >0 GO O -o m
OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOm ill III m III m HI III HI ill m ill ill m HI in ill III ill til ill III III III in III m ill ill m ill ill III Hi HI III HI ill
o4-0, <','r-'-, u'\oir\<\io'.o4'<Nj—<0> ®®®0'O<M4, f-Of^r~-*4, ®ci,i-*»^o®0'r-4-
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o4-
n"i
HKtinNorg^«a404N«oiA'4coinrgai 4nHOMniAinr>^iAHOMON<f'00OOOO^HHHHrgnn^^m41«MOaO'OHHM«l^in4CD9Hmv\arg9i nin^ 000000000000000000000'*-H*H-*>H-H.^rH.--i-H<\|<\|<Mf\jm«>4,
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in®os r»ff'0>oo>r-f»®fv»'0®in^ir>®^rg<Mio^)^^<^mf«.^»<r>o*®rg®»«Mui o—i<'< ,*''t«''0^h-o<Ni'*®®OfM4- ®®o(M^'inr,-o> -^Primr»0‘tM^f»of''®4"N-ooc ooooooooo-n-<>*i-i-*<\ic\j<Mf4<M<'or«,>mro<*>(*>4, 4, 44’'4mtnir»4>>0'Or'-r»'03K ooooooooooooooooooooooooooooooooooooooo<1acUIO. <\| <\l ^<1 ^ lrtririHrtriH^-lrtH»IHddri-1—If-IOOOOOOOOOOOO-^2! OOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOOUJH> UJ UI UJ UJ UI hi i 1 1 Hi 1
1
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1
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1 'll ill ill ill ill n i ill iii ill ill ill hi ill
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rrifOt^mrOrrifrirrtr^roiMrMfMiMiNiMrgiMrgrgfMcgfMfMfsirMiMtMrgfMfNjrgiNlMfMiMrsiroooooooooooooooooooooooooooooooooooooooiii ill ill m ill m iii iii m ill ill in ill iii iii ill in iii ill ill iii m m ill ui ill ill in ill ill ill ill iii ill in m iii iii
iMNrfa'^offl^o®fflO^<M7"0'Offl®ffloo-iOin^ii><i^o-i®a'inNa'M4'4, r'V<N'O.^®>O4’r'1OirirOr»'I.OOiri-*f-4''-*0'r-®4M—iO0'®f'-'Oin4- 4'('^<NJ'H-^
fr>4’004, 0'®<Njcri4’r«.ino'0'or''r04, -*0'Hf«-4'<''i«0'iOm>*4-4’4, iriin'Or-'04, 0-<lftmO^®«®»0'm®NN.O«»0'0'fflMflOin«OHOMfl'0«««N'0 O'
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oooooooooooooooooooooooooooooooooooooo o
^J'OON»®'Ol*IOm«H^Om«OJl Ol fffl«l'f'OK'lftOONKl#OII'»N'tCM»lOHO'0«fl'tlftO0'MM'0»ff'OOOOOO0'MflNff'inO’tM7‘O«rtHN —ONNN^«ON«lflhN®ff'Ji^O'OOOOOOJiO'ffff®B«f-«IIMflKINff'l' OfO in O P*> N N 00 CO 00 CO 00 00 00 GO GO GO GO ^ C O' ^ ^ ^ GO GO GO (O CO GO GO CO GO GO GO GO 00 P** ^ O'
oooooooooooooooooooooooooooooooooooooo o
• Vi *0OOOOOOOOOOOOOOOOOOOOOOOOOOOOpOOOOOOOOf^O'O'* yO QOON't'OcOOmH H H J-I H (M (\J
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oiromotool/M/> vO 'O f** CO oOO'(7'OOHHf\JfM
^4 H ^ H H H m m ^ ^ vn4- <M4 r-
36'Z
See
footnotes
at
the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEW
POINT
BUBBLE
POINT
PRESSURE
3
MOLEF
WTF
VOLUME
MOLE
F
WT
F
VOLUME
EQUILIBRIUM
RATIO
b
ATM
METHANE
MOLAL
c
SPECIFIC
11
METHANE
MOLAL
c
SPECIFIC
11
METHANE
N-PENTANE
^4 ^4 pH pH H H H H H —4 H pH H H pH p4 pH H H H sd pH pH pH pH *4 H ^4 H pH pH p4 ^4 pH pH 0009 0000 0 0 O O O O O O O O O OOOO O O O O O O O O 0 O O O 0 0 0LU UJ UJ LU UJ UJ UJ UJ LU LU UJ UJ UJ UJ LU LU UJ LU UJ UJ UJ LU LU LU LU LU UJ UJ LU UJ LU LU UJ UJ UJ UJ UJun co eg 0 co r» eg >0 0 vO 0 ro 0 0 4 'O 30 *4 4 in —< o> ao O' 0 CO CO e- CO CM O' CO ^4 UN eg 0r- ® ® >0 CO UN pH O UN 0 (M eg e- rO ^4 rsj lA ® (NI N pH p» 4 (A CO 4 ao LA >0 CO >0 0 O' UN 0co c 4 -O i-H ® ® 4* eg O' 00 r** ® 0 0 0 o <ONN ao ao a* O H fNJ CO UN O CO CO CO eg CM 006 1n 4 3. 3. 2
.
2.2.
2.pH .H h pH H »4 1—
«
H H »4 pH pH pH pH CM 2.
eg 2.(NI 2
.3, 3
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38
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footnotes
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the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
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39
See
footnotes
at
the
end
of
this
table.
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
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40
See
footnotes
at
the
end
of
this
table,
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEW
POINT
BUBBLE
POINT
PRESSURE
3
MOLEF
WT
F
VOLUME
MOLE
F
Ff
VOLUME
"
EQUILIBRIUM
RATIO
*3
ATM
METHANE
MOLAL
c
SPECIFIC
d
METHANE
MOLAL
c
SPECIFIC
41
METHANE
N-PENTANE
*4 H *4 H H H t-4 —4 H H H -4 H -4 e4 •4 ^4 H H -4 H t-4 —
(
H -4 oo o o o o o o o o O o o o o o o o o o o o o o o o o o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UI UJ UJ UJ UI UJ UJ UJ UJ UJ UJ UJ i UJ UI UJ UJ UJ UI UJo r- at >0 r- in CM o •t in o CM o H h- o CM O' >0 CM cn in 00 ao o cn o-o vD m ^4 CM H o H >0 >o o O' CM h- in >t at in o vO o H aO aO CM ^4 o>o <t >o o >0 cm in H 00 >0 at m cn CM cn cn at in <o h- 00 O CM in co cn CM -4 o8.
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41
See
footnotes
at
the
end
of
this
table.
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
-<= o.2 l
h- z<ce
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42
See
footnotes
at
the
end
of
this
table
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEW
POINT
BUBBLE
POINT
PRESSURE
3
MOLE
F
WTF
VOLUME
MOLE
F
WTF
VOLUME
EQUILIBRIUM
RATIO
b
ATM
METHANE
MOLAL
c
SPECIFIC*
METHANE
MOLAL
c
SPECIFIC
11
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N-PENTANE
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in 4 4 eg m m ^4 o O' O O' m 00 4 4 m oo CO eg m oo in 4 rO •4 O' r*- in 4 eg eg o o 4 o o m 4 4eg eg 2
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6.
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o o o o o o O o o o o o o o o O o o o o O o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ yy UJ yj UJ UJC eg oo 4 o o in •4 eg m o ^4 O' o O in CO 4 m in 4O O' eg O' in eg o eg o h- in £> CD eg 00 e- m e-oo in 4 eg o oo g> O' m 00 m O' >0 -4 CO 4 eg o 00 ^4
H H 1.i. i 00
7. 6. 5. 5. 4 4.3. 3. 3. 3. 2. 2. eg eg eg ^4 C.
ffi(fiWHH^ONS#® ,tO’OOO^NOOlflOoinr“®-*inino-*® — -*®-*®<MO'<\i4<M4in® mni4-0®m®^<M4inp“«®0'0'0'®®^'®4''*0' O'OOOCiHHHNNrgMIMNIMNMftlNNNIMM^ f\)
OOOOOOOOOOOOOOOOOOOOOOO o
f'inin<\|.»-<N—<0-0-—<-0f'-m0'O0'-00'a'4(\lrM.0 —I®f“ 400 f^<\lin®^M® 44 m,*,$-mi\|»*(T-m(\| ino-*<Nr-i44ininin'0-0'0'0-0-0'0-0'0'0-0minin -o
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• Vi W00000©0000000000000000'0»^4^taomoino^oiAOinoiftoino^oiAooc1 orf ^,^oj<MOi^i^-^-unir\®vOi>^F^®®a'0'oo-i'-<®r~
43
See
footnotes
at
the
end
of
this
table.
o oo o © o o o o o o o o o o o O o O o o o o o o o o o o o o o o o O o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ
O' o o o * in o o ^4 co 4 4- 4- o m O' o o CO o co o m UN sO <o UN <NJ 00 *0 o O o*4 •o 4 4 h» (M cm •o O' O' UN O (NJ UN r*> m O' o <N m 4- CO fNI in UN (NJ 00 CNJ (NJ o 4) o 4- oin 00 CM rsj m o p- in on CNJ CM cn 4 <£ 00 ^4 4) ^4 o © co CM 4-
O' m co (NJ •-4 (M «N m CNJ O o• 9 • • • • • • • • • • 9 9 • • • • • • # • • • • • • • • • • • • • a
O' 00 CO >
0
o m in in UN UN m in UN in 4) 4> r* © O' 00 r* 41 '
0
4) '
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^4 o o o o o o O o o o O o O O o o o o o o o o o o o O o o o O o o o oo o o o o o o O o o o o o O O o o o o o o o o o o o o o o o O o o o oUJ UJ UJ UJ UJ UJ UJ UJ Ul Ul UJ UJ UJ UJ UJ UJ UJ UJ Ul Ul UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ
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o o o o o o o o o o o o o o o o o o o o O o o O O o o o o © O o o o ©UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul Ul UJ UJ UJ UJ UJ UJ UJ UJ UJ00 p- UN CO CNJ O' O' -4 O' O' UN in ^4 00 CNJ 43 co in 00 m 4- CNJ o CM o *4 O' m CO 'o CM 4- p* 00
>0 00 o co UN 00 CNJ UN O' 4- O' m CO o ^4 00 in o 43 f>- o co 43 O' 4- CO 4- o CD CO O' o44 ^4 #4 (NJ (NJ (NJ fM ro pin co 4- 4- in in h- 00 O' CNJ 4- CM CNJ ro co co 4- 4- in 43 >0 h- O' o 4- 4
• • • • • • • • • • • • 9 • • •
2 2 2 2 2 2 2 2 2 2 2 2 CNJ 2 2 2 2 3 0 (M CM CM CM CM CM CM CM (NJ CM CM CNI CM ro co o
CM CM CNJ CM PM CM CM CM CM CM CM CM CM CM CM CM CM CM co CM (M CM (M (M CM CM CM CM PM CM CM CM CM CM CO
o o o o o o o o o o o o o o o o o o o O o o o O o o o o o o o o O o oUl Ul UJ UJ UJ UJ Ul Ul UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ Ul UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJib m 0 O' ® O' in o f- >0 00 •O l>- 4 >0 o >0 CM 00 o O CM <0 m UN O' 4 r- CO (O <0 p* ^4in in >*• co pm •4 4 o o © © © O' 00 00 <£ 00 CO PM CM *4 o O' © O' O' O CO h* (M ^4 oin in m m in m m m in 4 4 4 4 4 in ^ in oh •0 >0 •c o <0 in UN UN in <0 >
0
c P- 00 CM
44 H 44 *4 4 4 ^4 4 4 *4 ^4 ^4 e4 4 4 4 4 oom4
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o o O © o o 4 ^4 4 ^4 ^4 CM CM CM CM CO CO co CM BL o o o O o «4 4 *4 ^4 (M PM (M PM CO 4 PM• • • • • • • • • • • • • • • • • • • • © • • • • • • • • • • • • • • 9 9 9
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o o o o o o o o o o O o o o o o o
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h- © CM in O o UN cn 4 UN >0 in in CM p- ^4 ^4 UN o #4 CO 00 UN UN UN >0 o 4 (O m CO CD h- O44 O © CO r- in 4 cn 4 o © CM 4 co ^4 in 4 CO h- m 4 CO fM r4 o © o (M 4 O' ^4 42. 2.
CM r4 «4 4 >4 4 #4 ^4 © 00 00 c*- >0 vO in O 4 4 4 4 ^4 H ^4 © O' 00 >0 in UN o
co co (O CO CM CM PM CM CM (M CM CM (M CM PM PM CM CM CO CO co CM CM (M CM (M CM CM CM PM CM PM CM PM CO
o o o o o o o o o o o o o o o o o o o o o o o o o O © o o o o o O o oUl UJ Ul UJ UJ Ul UJ Ul Ul 111 111 HI 111 111 in UJ UJ Ul UJ UJ UJ UJ Ul UJ Ul Ul UJ UJ UJ UJ UJ Ul UJ UJ UJin >o *o in f- ® o 4 ,h « ® in m 4 ^4 oo ao © o P^ o P^ © CO CM 44 CO CO O' <0 44o MD ^ 4 «0 N UN N P^ CO in CM CO UN CM GO 00 co O' 00 (M fM CO 00 ^4 co UN ^4 CM o p- oUN CO m o in (*i 4 K h >o psi oo in pm © P- (M 4 CM -4 '
0
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UN O' 4 o O PM © o co CM9 9 9 9 9 9 9 9 9 9 9 9 9 9 9 9
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ro©o04f^40GO>or^co(M© CO P*" 44 © OO O 4 CO GO O' <0 0 OO 4 O O 0 fO CMM © O O 4 Hi40N0lA®« >0 O 4 UN >0 O' 00 ro 4 4 (O © CO PsJ O' CO 4 PM O PO PM *HKIlMMM mKO'HIMKWM'in 1*1 m i\i h ^ CO O 44 UN 00 44 CO 4 p- h- CD 00 GO P- M3 CO 00
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o o 6 o o 60666600600000 0 O 0 O 0 O 0 O O 0 © O O O O O O 0
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0
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9 9 9 9 9 9 9 9 9 9 9 9 9 9 9 9 9 9oddoodoooooooo d 0 0 0 0 0 © 0 0 O 0 O 0 0 O 0 0 0 0 © O O 0
0 O 0 © O 0 O O O 0 O 0 O O 0 0 OC Vi to
0 m 0 p- O O O O O 0 O 0 O 0 O O O O• *« to0 © co m
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0
co O UN O UN O m O UN O UN O in O in O UN © ^4 CO GO O UN O in 0 in 0 UN 0 UN C UN © in ^ pm ©4 4 CM PM CO ON 4* 4* m UN >0 M3 h- p- 00 GO © © © GO P*“ 44 CM PM co co 4 UN UN 'O O P^ CD GD <D r- M3
44
See
footnotes
at
the
end
of
this
table,
TABLE
3.1.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THEMETHANE-N-PENTANE
SYSTEM
-
CONTINUED
DEWPOINT
BUBBLE
POINT
PRESSURE
3
MOLE
F
WTF
VOLUME
MOLE
F
WTF
VOLUME
"
EQUILIBRIUM
RATIO
b
ATM
METHANE
MOLAL
c
SPEaFIC
d
METHANE
MOLAL
c
SPECIFIC
11
METHANE
N-PENTANE
o4-4-
*•
Oaia
cc3<CC
H H H H H H H ^ H H OooooooooooooI I I I I I I I I I I
i|i ill Ip ill ill HI III III jll III H* III4Nn0444O4lrIH0.afSiOin-— —'oo<''>r'-o
O'aor-r-r-r-r-f'-r-f-O'-*
oooooooooooooooooooooooohi n i 1
1
I iii hi i)i in ni ill m ill m0!'*000'00®—if'-'OO^NOnONNOCW'lOO
OOOOOOOOOOO-iOOOOOOOOOOOOHI Hf yj yi >11 III HI III III III ill
UTfO N >0 fO ^ O' O IfN O 00
4-4->$*inin>or*-aoo‘eg>o^®oo®*oo©oooocMegcgegegegcgegegcocoo
egegegegegegegcgegcgegroOOOOOOOOOOOOill iii ni 1
1
f ill iii hi hi 1 1
1
1. 1 1 ill niN>0«t^C0Q04, 't^a0OO^oooOHioinoN®^h-e-e-r^p*»e^e-r^aocoO'og
H H H H H H H H H rt H O
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^^co>ON^ir®^o>ts-~g^, 0'eg'00''$’—<inin*-<*H-g yt 'Offl^mma^'to^oDOOO^^HHNN^mN• ••••••••••«•DOOOOOOOOOOOO
oin>*
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LUoc
HHrtHHHHHOoooooooooI I I I I I I I
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W fO fO CO CO fO fOoooooooooLUUJUJUJUJUJUJUJUJegcgcgfOincoegmO'aoGocoaooocoo'Ocn
ooooooooo
0'0eg0'in^g0'00h»e-OOHHNrt(^'t'0(f»oooooooooooo©oooooo©oooooooooo
NNN®f^'0'tin«tNO<NJ»n^OCMlAC0^>tOOOO^HHHNHOOOOOOOOOO
H H o o o o a o O c=45 ft. eg eg H f-4 H H H HO o o o o o o o o o o o £ o o o O o o o o oUj UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ 1= UJ UJ UJ UJ UJ UJ UJ Ul UJ4- H O' co 4- eg o in o eg GO 00 >0 in co 4- H o O' GO4- CO CO -o 4- O' O' n o ee co o H o m o eg co 4- oco eg o GO o eg j- •o e- <0 4- ©9 o> co GO p- 4> in 4-
9 • 0 0 ® • 9 9 •H *-g »=l ^g o* O' GO r*» o in >4- o o o O o o o o o O
CNJ rvj eg eg eg eg eg eg eg eg eg co CO co co co co co ro CO coo o o O o O o o o o o o o o o o o o o o ouu UJ UJ UJ UJ LU UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ4- eg o o m 4- in eg •4- o o O' eg 00 © e- >o >0 e- O'GO GO o r- co O' ^g e- in r*» eg <=—
<
<»> O' O' eg >o o in o mO' ITN in e- H m *«g o eg CO 4- eg ao >0 in in 4- 4- co ro eg• • • © • 0 9 9 © © 9 9 • • © © 0 © © ®
GO <0 in m 4- •i- co co eg eg o o o O o o o o o o
O't
oUJo
UJQCol-<(XUJft,
XLU
o •g 4) <o 4- o o O' -0 inO' eg co o eg o CO eg O' O' O' CO CM 4- CO o eg o 4- O' 4-
O' o eg co CO CO eg o O' CO o eg 4- >0 r- GO 00 r- >0 GOo o o H *-g H ^g —4 *»g o <g o O o o o o o o o o9 9 9 9 9 9 9 9 9 9 9
o o o o o o o o o o o o o o o o o o o o o o
o eg eg in O' eg O ~g00 O' e* >o in H GO GO ^g vO H GO O' o GO CO o o H o 4- egGO in *H in GO o o o o in <o O o o •o eg >o GO O' GO 4- O'r*g eg co co co -g* 4- 4- 4- (O CO 4’ o »g H eg eg eg eg eg eg eg9 • 0 9 9 G 9 © 9 © 9 9 9 9 9 9 9 9 9 9 e 9
o o O o o o o O o o o O o o o Q o o o o O O
• *« 1« • *4 Wo o o o o o o o o O CO 4- CO o o o O o o o 0 5 O' O'
1 • 9 e 9 9 9 9 9 9 9 9 9 9 © 9 9 9 9 9 9 9 9 9 9
o in O in o in o in o in in CO CO in o in o in o in O eg CO in1CO co 4- 4- m in 4> <0 h* h- <0 4) eg CO CO 4 4- in in >0 o n in
45
Table 3.2. Agreement of interpolated and experimental data for the methane-n-pentane system
Source Numberof points
Average a Deviation
fraction b
Standard c
Composition d
Taylor [36] 14 0.0021 0.0042 0.0116
Dourson [37] — 4 .0078 .0198 .0164
Sage [38] 32 .0007 .0035 .0037
Pressure e
Sage [38] 34 -0.05 0.0054 0.33
Sage [35] 9 4.8 .0395 5.5
“ Average deviation defined by£^ (Gt exp -Gk sm]lN.
b Fractional deviation defined by
' Standard deviation defined by
l|[
([?
(C* exp Cfcsm ) /Gke .])«».
(^frexp ^sm)2]/(AT—
1)|111 where G = either composition or pressure.
d Composition in weight fraction methane.e Pressure in atm.
Table 3.3. Unique states for the methane-n-pentane system
Methane Critical Maxcondenbar Maxcondentherm
Mole
fraction
Weight
fraction Temperature Pressure a
Volume
Temperature Pressure a Temperature Pressure a
Molal b Specific c
K atm K atm K atm
0.0 0.0 d 469.49 33.16 294.6 4.08 469.49 33.16 469.49 33.16
.333 .1 439.9 75.9 218 4.08 408.4 91.5 446.6 58.6
.529 .2 409.7 111.3 173 4.08 355.9 133.5 427.0 70.9
.658 .3 380.6 139.0 144 4.08 328.4 152.4 408.6 76.7
.750 .4 351.4 156.4 122 4.04 310.8 162.4 390.0 78.9
.818 .5 311.7 166.5 99 3.78 e 294.7 167.5 371.5 78.4
.871 .6e 275.0 169.2 275.3 169.2 353.3 75.8
.913 .7 253.0 167.0 253.0 167.0 333.8 71.2
.947 .8 232.3 155.9 232.3 155.9 e 309.7 64.4
.976 .9 211.2 129.4 211.2 129.4 279.3 55.7
1.0 1.0 d 190.63 45.57 99.3 6.18 190.6 45.5 190.6 45.5
.1 .024 462.8 44.2 272 4.08 457.9 46.1 463.8 41.4
.2 .053 454.2 57.0 249 4.08 439.9 63.1 456.7 49.2
.3 .087 443.8 70.7 226 4.08 417.0 83.5 449.4 56.4
.4 .129 430.9 86.7 203 4.08 390.3 106.4 440.7 63.2
.5 .182 414.8 105.1 180 4.08 362.9 128.2 430.3 69.3
.6 .250 394.7 126.6 157 4.08 339.7 144.9 417.8 74.4
.7 .342 368.6 147.5 134 4.08 320.7 157.1 400.7 78.0
.8 .471 327.5 164.0 106 3.90 e 299.5 166.6 376.9 78.7
.9 .667 260.2 168.4 260.2 168.4 340.2 73.0
Estimated
uncertainty f1.0 1.0 3.0 2.0 4.0 2.0 3.0
d API 44 [16].
e Values at this and lower temperatures extrapolated.
'Estimated uncertainty expressed in percent.
a (Atm) (1.013250 X 105) = N/m 2
.
"Volume expressed in liters/kg-mol.
c Volume expressed in liters/kg.
46
TABLE
3.4.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
ooooooooooooooooooooooI I I I I I I I I I I I I I I I I I I I I
III in ill III in in m III I n l-il 1 111 111 111 111 111 111 111 III 11 J HIin«oiftoo^Oi»'OiA(fiO'tnN-4iftoo'f-NOM)lMOONO^Oi0^OMn94NO'49'OO
H.H H H H r-l -< o o O O o o o O o o o oO o o o o o o o o o o o o o o o o o o o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ<o cn Ot<NO O' fO o 00 in O' o o -l O' o if r- oo oH 00 ^ ^ ^ N it m CM CM cn m oo «t -4 00 h» in H o1.
in cn cm cm ^ i. -* -o •4-3. 2. CM CM e-4 H i.
1. 1.
H H H H H H t-4 H H H Ho 0 o
1 1
o oA
01
01
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o o oA
01
ofl
oo
01
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01
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1
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UJ1
UJ1
UJ UJB
UJ1
UJ UJ1
UJ UJ1
UJo o o H CM cn ro 4* o >0 cn o O' 00 00 H O' O' min in in in in in in in in in >o >0 r- oo 00 O' o CM m >o cnCM CM cm CM CM CM CM CM CM CM CM CM CM CM CM CM cn cn cn «n
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o o o oUJ Hi UJ UJit O' cn inh»«or- it «*» cn
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ooooooooooooooooooooo
(Minin>rr-inh-->OOcn'^cn^^mh->0^4, CMcno mNO'^M\l>0©ONfn(7'00000'®«0(VjN®a' oc\j>t'Ovor^rs.f^cocoooaoo'Os O'0'aoaocoaor->oir» o'
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® S4 Mooooooooooooooooooooomin-oIM't'ODOOMtiHOOOOOOOOOOOO®#^rf^^_lHN-t'0®OMt'0®OM't-t'ta3^HririHNlMNNN
47
See
footnotes
at
the
end
of
this
table.
TABLE
14.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
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48
See
footnotes
at
the
end
of
this
table,
TABLE
3.4.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
pHpHpHpHpHegcgegegegegegegegegegegpHpHpH.HOOOOOOOOOOOOOOOOOOOOOOOI I I I I I I I I I I I I I I I I I I I I
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49
See
footnotes
at
the
end
of
this
table,
TABLE
14.
PROPERTI
ESOF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
°°rO I
a
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n
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50
See
footnotes
at
the
end
of
this
table
TABLE
3.4.
PROPERTIESOF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
“°rSi
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51
See
footnotes
at
the
end
of
this
table
TABLE
3.4.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
OOOOOOOOOOOOOOOOOOOOOOI I I I I I I I ) I I I I I I I I I I I I
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52
See
footnotes
at
the
end
of
this
table,
TABLE
14.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
H H H H H H H ^ H H N fVJ M CM CM CM H H H H H CooooooooooooooooooooooI I I I I I I I 1 I I I I I I I I I I t I
ill hi ni III Hi ill hi III im in it) ill III ill ni ill ill ill ni ill ill ill
NOOrtONij’rtHniroNOOitinwo'-Mno
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0
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2. pH ^4 ph H 7. * re3. eg cm 2. H c=H &4 o=4 H
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m o' in H K re a O eg ao 09 O' re in eg m pH 4 N ffl mo re in 00 o h re ^ 0=4 O' O' O pH im ^ in in eg o e*o o o o o o o H *4 •h re 4 'O ® pH re >c O' re ^ pH o oo o o o o o o OOOOOOOpH pH pH ph eg CM 4* in re
6 6 6 o 6 6 6 o o 6 6 6 6 6 o 6 6 6 6 o 6 o o
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pH pH pH H pH pH pHo o o O O o o o o o o o o o o o o o o o O oLU UJ UJ UJ UJ UU UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ LU UJ UJ UJ UJ UU^ eg O o o=4 ® >* eg K ® o V® ® o in o in ^4 ® in o inO O' 4- ® o o eg O' O' pH CM eg in K ce ® K o o pH in inrf) •& 4- in o=4 ® 4> -1- <e re o eg K re eH O' ® ® ® o ce (=4
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53
See
footnotes
at
the
end
of
this
table,
TABLE
14.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
H pH p=l pH H H pH H •-4 CM CM CM CM CM pH pH pH pH pH pH ©o o o o o o o o o o o O O O ooooooooUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJo o co -4* o t- 4 cm 4 o o in o r- H cm co in © © oo m m >o O —t © 4 its in >0 CM c 9-4 h- co n © in ©in r*- co >o N ff1 s in 4 co cm pH H in 4 o cm m o o o o9. 4 co cm 2. 1. 1. pH H -i O' oo
8.00 O' H pH pH CM cn 45 pH
CM pH pH pH pH pH ^H pH pH pH © o © o © O © O o © © oO o o © o o o o o o © o o o o O o o © o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJin m CM 00 in o © pH 4 in CM pH co 4 o CM © in 00 4 opH O' <o *0 in 00 in a* o 4- O CM CM in H o 00 h- CM ©o r- in 00 m o r*- •o 4 co o 00 pH <o co o oo in rr> p* ©
pH 7, * co CM CM CM pH pH pH m (HI co CM2.
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CM CM CM CM CM CM CM CM CM <N CM CM CM 2, co co3.
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pH H pH pH i. pH i. i. pH i. i. pH H 1. pH pH pH H pH1. pH ©
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>4- co CM CM CM pH pH pH pH pH >0 <4 CO CM CM pH pH pH pH O' o
CM CM ^H pH pH pH pH pH pH pH o o O o o o o © o o pHo o o o o o o o o o o O o © o © o o o o o oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJpH <4- 0s in in CM N 4) >4- >4 4 •4 O' o h- 4> 4- 4- >0 O' 4 CM© o ao -4- O' co in 4* pH CM >0 *0 ao OO r- CO pH h- ao o >
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o o o o O O o © o o © o o o o o O o o © o o o
CO in >4- CM pH O' >o pH CO CM o >0 >6 CM CO ao OO O' ao (O© ao pH o >o •4- in pH CO CO O' CO ao © o 4> O CM pH 4 m fO ©in CM co CO pH co in >0 pH (O CO 4- CO CO co CM pH O' in pH 4o m o h- ao ao ao CO ao O' O' O' O' O' O' O' O' O' ao ao co O'• • • • • • • • • • • • • • • « • • • • • • •
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^H pH pH ^H ^H CM 4 ao o CM 4 CO O IM 4 4 rn O'^H pH pH H pH CM <M CM CM CM
54
See
footnotes
at
the
end
of
this
table
TABLE
3.4.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
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55
See
footnotes
at
the
end
of
this
table.
TABLE
3.4.
PROPERTIESOF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
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56
See
footnotes
at
the
end
of
this
table,
TABLE
3.4.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
^ °rO <
s
£
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oUJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ UJ
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57
See
footnotes
at
the
end
of
this
table,
TABLE
14.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
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58
See
footnotes
at
the
end
of
this
table.
TABLE
14.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
o °ro •
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59
See
footnotes
at
the
end
of
this
table,
TABLE
3.4.
PROPERTIESOF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
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60
See
footnotes
at
the
end
of
this
table
TABLE
14
.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
-
CONTINUED
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end
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this
table,
TABLE
14.
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PHASES
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SYSTEM,
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63
See
footnotes
at
the
end
of
this
table
TABLE
14.
PROPERTIES
OF
THE
COEXISTING
PHASES
IN
THE
METHANE-N-PENTANE
SYSTEM,
ENGINEERING
UNITS
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CONTINUED
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64
TABLE 3.5. Unique states for the methane-n-pentane system, engineering units
Methane Critical Maxcondenbar Maxcondentherm
Mole
fraction
Weight
fraction Temperature Pressure a
Volume
Temperature Pressure a Temperature Pressure a
Molal b Specific c
° F psia °F psia °F psia
0.0 0.0d 385.41 487.3 4.72 0.0654 385.41 487.3 385.41 487.3
.333 .1 332.1 1115 3.50 .0654 275.5 1344 344.2 862
.529 .2 277.8 1635 2.78 .0654 181.0 1962 308.9 1042
.658 .3 225.4 2043 2.30 .0654 131.5 2240 275.7 1127
.750 .4 172.9 2298 1.95 .0648 99.8 2387 242.3 1159
.818 .5 101.3 2447 1.59 .0605 e 70.7 2462 209.0 1152
871 .6e 35.4 2486 35.9 2486 176.3 1114
913 .7 -4.2 2454 -4.2 2454 141.2 1047
947 .8 -41.5 2291 -41.5 2291 e 97.8 947
976 .9 -79.5 1902 -79.5 1902 43.1 818
1.0 1.0d -116.54 669.7 1.59 .0990 -116.54 669.7 -116.54 669.7
.1 .024 373.4 650 4.35 .0654 364.5 678 375.1 608
.2 .053 357.8 838 3.98 .0654 332.1 927 362.3 723
.3 .087 339.2 1039 3.62 .0654 291.0 1227 349.2 829
.4 .129 316.0 1274 3.25 .0654 242.8 1564 333.5 929
.5 .182 287.0 1545 2.88 .0654 193.6 1884 314.9 1018
.6 .250 250.7 1860 2.52 .0654 151.8 2129 292.4 1093
.7 .342 203.7 2168 2.15 .0653 117.6 2309 261.7 1146
.8 .471 129.8 2410 1.70 .0624 e 79.5 2448 218.8 1157
.9 .667 8.7 2475 8.7 2475 152.6 1073
Estimated
uncertainty f 1.0 1.0 3.0 2.0 4.0 2.0 3.0
“(Psia) (6.894757 Xl03)= N/m 2
.« API 44 [16].
b Volume expressed in cu ft/lb-mol. c Values at this and lower temperatures extrapolated.c Volume expressed in cu ft/lb. ' Estimated uncertainty expressed in percent.
TABLE 3.6. Agreement of interpolated and experimental data for the methane-n-pentane
system, engineering units
Source
Numberof points
Deviation
Average a Fraction b Standard c
1
Composition d
Taylor [36]
—14 0.0021 0.0042 0.0116
Dourson [37] 4 .0078 .0198 .0164
Sage [38] 32 .0007 .0035 .0037
Pressure e
Sage [38] 34 -0.7 0.0054 4.9
Sage [35] 9 69.9 .0395 80.8
a Average deviation defined by I ^ (C* exp —Gk ,m ) I//V.
1^
b Fractional deviation defined by[ £ ^(C* exp-C ,J/Gk exJ^IN.
c Standard deviation defined bv{j^
(Gk„B- Ck sJ 2j/(V-l)
j
dComposition in weight methane.e Pressure in psia.
1,2 where G — either composition or pressure.
65
Table 3.7. Accuracy of experimental backgroundfor the methane-n-pentane system
Quantity Units Taylor [36] Dourson [37] Sage [35] Sage [38]
Sample purity
Methane Mole 0.990 0.997 0.997 0.997
n-Pentane fraction .995 .995 .992 .992
Composition
Volumetric a Atm 0.2
Phase measurements Weight
fraction 0.01-0.02 0.005 .005
Volumetric behavior Percent 0.3-3.
0
0.4 0.5
Unique states
Temperature K 1.0
Pressure Atm 0.8
Volume Percent 5
a Phase boundaries determined from first derivative of volume versus pressure. All error assumed to be in pressure.
4. References
[1] “Thermodynamic Property Values of Ordinary WaterSubstance,” International Secretariat, Sixth Inter-
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66
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