Volumetric Behavior of Benzene, Propane and Four Mixtures of these Substances Citation Glanville, James William (1948) Volumetric Behavior of Benzene, Propane and Four Mixtures of these Substances. Engineer's thesis, California Institute of Technology. doi:10.7907/DNCC-4G10. https://resolver.caltech.edu/CaltechETD:etd-10262004-153802 Abstract The volumetric behavior of benzene and of propane was investigated over a pressure range from vapor pressure to 10,000 pounds per square inch absolute and a temperature range from 100 to 4600[degrees] F. The results of these studies are presented in tabular form. The volumetric behavior of four mixtures of benzene and propane was investigated at temperatures from 100 to 4600[degrees] F. in the pressure range from substantially below bubble point to 10,000 pounds per square inch absolute. The single phase and two-phase data are presented in separate tabulations for each mixture. Deviations of the mixtures from the behavior of ideal solutions are shown graphically. Item Type: Thesis (Engineer's thesis) Subject Keywords: Chemical Engineering Degree Grantor: California Institute of Technology Division: Chemistry and Chemical Engineering Major Option: Chemical Engineering Thesis Availability: Public (worldwide access) Research Advisor(s): Lacey, William Noble (advisor) Sage, Bruce H. (advisor) Thesis Committee: Unknown, Unknown Defense Date: 1 January 1948 Record Number: CaltechETD:etd-10262004-153802 Persistent URL: https://resolver.caltech.edu/CaltechETD:etd-10262004-153802 DOI: 10.7907/DNCC-4G10 Default Usage Policy: No commercial reproduction, distribution, display or performance rights in this work are provided. ID Code: 4262 Collection: CaltechTHESIS Deposited By: Imported from ETD-db Deposited On: 27 Oct 2004 Last Modified: 21 Mar 2023 22:31 Thesis Files Preview PDF (Glanville_jw_1948.pdf) - Final Version See Usage Policy. 1MB Repository Staff Only: item control page

VOLUMETRIC BEHAVIOR OF BENZENE, PROPANE AND FOUR MIXTURES OF THESE SUBSTANCES Thesis by James William Glanville In Partial Fulfillment of the Requirements For the Degree of Chemical Engineer California Institute of Technology Pasadena, California 1948 ACKNOWLEDGEMENT The advice and guidance of Professors W. N. Lacey and B. H. Sage are deeply appreciated. The assistance of the Chemical Engineering Laboratory staff, under the direction of H. Hollis Reamer, is gratefully acknowledged. The investigation was sponsored by the Polymerization Process Corporation. ABSTRACT The volumetric behavior of benzene and of propane was investigated over a pressure range from vapor pressure to 10,000 pounds per square inch absolute and a temperature range from 100 to 460° F, The results of these studies are presented in tabular form. The volumetric behavior of four mixtures of benzene and propane was investigated at temperatures from 100 to 460° F, in the pressure range from substantially below bubble point to 10,000 pounds per square inch absolute. The single phase and two-phase data are presented in se- parate tabulations for each mixture. Deviations of the mixtures from the behavior of ideal solutions are shown graphically. TABLE OF CONTENTS A. VOLUMETRIC BEHAVIOR OF PROPANE I. II. III. IV. Introduction ...« ee. Methods and Apparatus .. Material eo «© «© © © @© © @ Experimental Results. .. B. VOLUMETRIC BEHAVIOR OF BENZENE I. II. III. Iv. Introduction eee © © @ Methods and Apparatus .. Material o 0©« ee © © «© «© @ Experimental Results. .. ‘C. VOLUMETRIC BEHAVIOR OF FOUR MIXTURES OF BENZENE AND PROPANE ... I. Il. Itt. IV. Introduction « « « e « e Methods and Apparatus .. Material eee ee © © #@ @ Experimental Results. .. Nomenclature . « « « « « « « e ReferenceS ee »« « «© «© « «© «© « « ° Page ao F DW HY Oo o ~w x 10 10 13 14 LIST OF FIGURES Page 1. Compressibility Factor for Propane~Benzene System at 460 oP Lek ee ee 8 2 Percent Deviation of Actual Specific Volume from Ideal Solution Behavior, for Benzene~Propane Mixtures at 160°F. ....e. 16 3. Percent Deviation of Bubble-Point Pressure from Ideal Solution Behavior fox 0 Benzene-Propane Mixtures at 100° and 160°F .. 1” iI. Til. Iv. VI. VII. VIII. IX. xT. LIST OF TABLES Volumetric Behavior of Propane in the Condensed-Liquid Region Specific Volume of Benzene... Specific Volume of Benzene at Bubble Point « .« »« « « « « e « Single-phase Volumetric Behavior Mixture of Propane and Benzene 88.87 Mole Per Cent Propane. . Single-phase Volumetric Behavior Mixture of Propane and Benzene 59.83 Mole Per Cent Propane. . Single-phase Volumetric Behavior Mixture of Propane and Benzene 39.48 Mole Per Cent Propane. . Single-phase Volumetric Behavior Mixture of Propane and Benzene 19.56 Mole Per Cent Propane. . Volumetric Data for a Two-phase Mixture of Propane and Benzene with 88.27 Mole Per Cent Propane. .« « « -« Volumetric Data for a Two-phase Mixture of Propane and Benzene with 59.83 Mole Per Cent Propane. . .. -» Volumetric Data for a Two-phase Mixture of Propane and Benzene with 39.48 Mole Per Cent Propane. .«. .« « « Volumetric Data for a Two-phase Mixture of Propane and Benzene with 19.56 Mole Per Cent Propane. . « « -« with of a with of a with ° of a with e Page 18 22 24 25 28 34 37 38 40 42 l. A. THE VOLUMETRIC BEHAVIOR OF PROPANE I. INTRODUCTION Propane is one of the important components of natural gas and is useful as the starting material for the preparation of a number of organic compounds of industrial interest. For this reason it is desirable to know ac- curately the influence of pressure and temperature upon the specific volume of this hydrocarbon. The volumetric be- havior of propane has been studied by a number of investi-~ gators. Dana et al. (4) measured the vapor pressure and the volume of bubble point liquid and dew point gas of propane from approximately -50° to 130° F. Later studies by Sage, Lacey and Schaafsma (6) gave values of the vapor pressure up to the critical temperature and the volume of liquid and gas from approximately 50 to 3000 pounds per square inch absolute. Beattie and co-workers studied the influence of pressure and temperature upon the volume of propane at lower pressures and at temperatures up to 525° F. (1) ana also made extensive measurements in the critical region (2). The present work was undertaken in order to obtain more accurate vapor pressure data and to extend the upper limit of the pressure range. II. APPARATUS AND METHOD The equipment used in this study has been des~ eribed in detail (5). In principle it consisted of a stain- ‘less steel chamber within which a known quantity of the material under investigation was confined. The volume occupied by the sample was varied by the introduction or withdrawal of mercury and the resulting equilibrium pres- sure measured. The quantity of mercury added to the equilibrium chamber was established from the change in elevation of a mercury~air interface within an inter- connected vessel. The weight of sample introduced was determined by weighing bomb techniques (5). After com- pleting a set of isotherms, the propane was withdrawn. A comparison of the weight of material added and later with- drawn showed agreement within 0.03 percent in all cases. The weight of sample and the accuracy of the volumetric measurements were such that the measured specific volume at a given state aia not involve uncertainties greater than 0.2 per cent. The pressure was measured by a balance based upon a piston-cylinder combination (5). This equipment was calibrated against the vapor pressure of carbon dioxide at the ice point (3). The weights used in the balance were consistent with one another within 0.002 per cent. It is believed that the pressure at equilibrium was measured within 0.1 pound per square inch or 0.05 per cent, with the Be larger uncertainty being significant. The temperature of theequilibrium vessel was controlled by immersion in an agitated oil bath. Provision was made to minimize the effect of thermal gradients in the tubing which connected this vessel with equipment outside the bath. The temperature of the oil bath was measured with a strain~free platinum resistance thermometer which was compared at periodic intervals with a standardized in- strument. In addition, the resistance of the service thermometer at the ice point was checked at frequent intervals. Attainment of thermal and phase equilibrium was accomplished rapidly by mechanical agitation within the working vessel. This agitation was provided by means of a spiral agitator (5) rotated around the major axis of the vessel by a set of externally mounted electromagnets. After introducing a measured quantity of propane, the pressure within the apparatus was raised to approximate- ly 10,000 pounds per square inch absolute and the system brought to equilibrium at a constant temperature. The total volume occupied by the sample, the pressure, and the temp- erature were then measured. The total volume was then in- creased, equilibrium re-established, and the measurements repeated. This procedure was continued throughout the single-phase region. The vapor pressure was measured at several total volumes of the system. A slightly longer time was allowed for the attainment of equilibrium in the 4. two-phase region. After the measurements were completed, the temperature was raised to the next higher predeter- mined value and the sequence repeated. Upon completion of the determinations at the maximum temperature (460°F.), a set of check measurements was made at the initial temp- erature studied. The maximum deviation between the initial and final measurements was 0.1 per cent. III. MATERIAL The propane used in these investigations was ob-= tained from the Phillips Petroleum Company. The material as supplied contained less than 0.1 per cent of impurities. It was subjected to a fractionation at a reflux ratio of approximately 40 to 1 in a column packed with glass rings. The initial and final tenths of the overhead were discarded in the course of the fractionation. The purified material showed less than 0.2 pound per square inch variation in vapor pressure at 100° F. when expanded from bubble point to a state in which more than one half of the propane was in the gas phase. The purified hydrocarbon was stored in a stainless steel container from which it was transferred into a Weighing bomb before addition to the equilibrium cell. IV. EXPERIMENTAL RESULTS The experimental results were interpolated to even values of pressure and are recorded in Table I for each of the experimentally studied temperatures. A detailed comparison of the present measurements with the data of Beattie (1) at pressures and temperatures removed from the critical state shows unusually good agree- ment. The average deviation of the two sets of data for approximately 50 states is 0.22 per cent. The maximum de-~- viation encountered was less than 0.4 per cent. The values of the vapor pressure of propane recorded in Table I are based on present measurements and agree well with the work of Beattie (1). Be VOLUMETRIC BEHAVIOR OF BENZENE I. INTRODUCTION Benzene is an aromatic compound which is widely employed as a solvent and as the starting material for the preparation of many organic compounds. The vapor pressure, critical constants, and volume of benzene as saturated liquid and saturated gas were determined by Young (13). This work was supplemented by later investigations of the vapor pressure at relatively low temperatures (11, 12). The in~ fluence of pressure and temperature upon the volume and refractive index of this compound was studied by Gibson and Kincaid (8). Limited information concerning the heat capa- city was obtained by Burlew (7). Gilliland and Lukes (9) measured directly the effect of pressure upon the enthalpy of benzene. These investigations serve to establish the volumetric behavior at low pressures. It would be possible to calculate the specific volume at higher pressures from the enthalpy-pressure measurements of Gilliland and Lukes if volumetric data were available for one temperature throughout the range of pressures. However, at the lower reduced temperatures and higher pressures there does not appear to be adequate volumetric information. For this reason a study was made of the influence of pressure and temperature upon the volume of benzene at seven temperatures between 100° and 460° F, and for pressures between vapor 7. pressure and 10,000 pounds per square inch absolute. IIT. METHOD AND APPARATUS The method and equipment employed in this in- vestigation were described in Part A. III. MATERIAL The benzene used in this investigation was obtained commercially as the chemically pure grade and was subjected to the following purification procedure. The Sample was first distilled from a glass fractionating column containing thirty plates at a reflux ratio of approximately 40 to l. The initial and final quarters of the sample were discarded. The benzene was solidified, allowed to melt partially, and the material first melted was discarded. The remaining solid material was then distilled under high vacuum and condensed as a solid. It was then transferred by distillation into a steel weighing bomb. The index of refraction for the D line of sodium at 77° F. was 1.5013. The specific volume at 100° F, and atmospheric pressure as measured in a glass pycnometer was 0.01861 cubic foot per pound. 8B. IV. EXPERIMENTAL RESULTS The specific volume of benzene was determined at seven temperatures between 100° and 460° F. The values, which were obtained at irregular pressures, were smoothed graphically to even pressures. The results are recorded in Table II. The values of the two-phase pressure given in this table are critically chosen ones based upon the recent meas- urements of Hixson et al. (10) and the earlier data of Young (13). The agreement between the two experimenters was satis- factory and no effort was made in the present investigation to determine the vapor pressure. Table III presents a comparison of the specific volumes at bubble point as measured by Young (13) with those obtained in this study. The data of Young were interpolated in order to obtain values of the specific volume at states corresponding to those reported in Table I. The average deviation of the present results from these of Young was 0.3 per cent. Similar deviations were also found with more recent date (8). The present measurements, which were car- ried out in stainless steel apparatus over mercury agree within 0.05% with the independently determined values of the specific volume of the liquid obtained with a glass pycno- meter at 100° F. and atmospheric pressure. C. VOLUMETRIC BEHAVIOR OF FOUR MIXTURES OF BENZENE AND PROPANE I. INTRODUCTION While a certain, albeit limited, amount of ex-~ perimental information is available for mixtures of ali- phatic hydrocarbons, the amount of experimental informa- tion available on the propertiss of mixtures of aromatic and aliphatic compounds is limited. In order to determine the effect of temperature, pressure, and composition on the properties of a mixture of an aliphatic and aromatic con- pound, an investigation was made on the volumetric behavior of four mixtures of benzene and propane. Wo information is) reported in the literature on mixtures of these substances. II. METHODS AND APPARATUS The method and apparatus used in this investigation were the same as those described in Part A. The Bamples of benzene and propane were added to the equilibrium cell using weighing bomb techniques. After the completion of a series of isotherms on a sample of given composition in the high pressure region, the sample was reduced in size by displacing a portion of it at a temperature and pressure which in- sured homogeneity of phase. The amount of material re- maining was accurately determined by condensing it into 10. an evacuated weighing bomb with liquid air after the comple- tion of volumetric measurements in the low pressure region. In the neighborhood of bubble point and dew point, numerous experimental measurements were made so that the pressure and volume corresponding to these points could be determined accurately. IIT. MATERIALS The propane and benzene used in this investiga- tion were part of the large supply prepared for the in- vestigation of the properties of the pure substances. Their purification and checks upon purity are described in Parts A and B. IV. EXPERIMENTAL RESULTS The volumetric properties of the propane-benzene system in the single-phase region are presented in Tables IV - VII, whereas data in the two-phase region are presented in Tables VIII - XI. The experimental data, obtained at irregular pressures at seven temperatures between 100° and 460° F., were interpolated to even values of pressure. The specific volume and the compressibility factor were used in this work, depending upon which variable lent itself to most accurate interpolation in the region under consideration. In general, the specific volume was employed in the liquid region while the compressibility factor was used in the twe- phase region. il. Because of the limited amount of data in certain portions of the two-phase region, it was not possible to accurately smooth all of these data as a function of temp- erature. It is believed that the maximum uncertainty in the two-phase region is approximately 0.5 per cent, while in the liquid region, where sufficient data are available to make accurate smoothing possible, the maximum uncertainty is not greater than 0.2 per cent. The uncertainties intro- duced in the measurement of pressure, temperature, volume, and composition are all less than the above mentioned deviations. The values of buobdle-point and dew-point pressure and volume were determined by the method described by Sage, Backus, and Lacey (14). In certain cases use was made of the compressibility factor-pressure plot instead of the specific volume-pressure plot. The effect of pressure upon the compressibility factor at 460° F. for benzene, propane, and three mixtures of these substances is shown in Figure I. In Figure III the percentage deviation of the bubble-point pressure at 100° and 160° F, from that predicted on the basis of the assump- tion of ideal solution behavior is shown. The “ideal pres- sure" is determined from the following relationship: P =X P"+X P* I a) 6 6 The wide deviations from ideal solution behavior in mixtures 12. _ high in propane is clearly shown in this Figure. In Figure II percentage deviations from the specific volume predicted from a relationship snalagous to that above are shown at 160°F. for pressures of 1000 and 5000 pounds per Square inch absolute. 13. NOMENCLATURE P & pressure, pounds per square inch, absolute V = specific volume, cubic foot per pound T = absolute temperature OR, = 459.69 + °F 2 24.5 Specific gas constant = i , (1be./ine) (ft/1b.) o u for propane = 0.24338 for propane-benzene, 88.27 mole % propane= 0.22318 for propane-benzene, 59.83 mole % propane= 0.18580 for propane-benzene, 39.48 mole % propane= 0.16592 for propane-benzene, 19.36 mole % propane= 0.15019 for benzene = 0.13740 = ul molecular weight PR= vapor pressure of pure component g= mole % of component in mixture = compressibility factor = +r SUBSCRIPTS 3 refers to propane 6 refers to benzene (1) (2) (3) (4) (5) (6) (7) (8) (9) (10) (11) (12) (13) (14) 14. REFERENCES Beattie, Kay and Kaminsky, J. Am. Chem. Soc., 59, 1589 (1937). Beattie, Poffenberger, and Hadlock, J. Chem. Phys., 3 (2), 96, (1935). Bridgman, J. Am. Chem. Soc., 49, 1174 (1927). Dana, Jenkins, Burdick, and Timm, Refrig. Eng., le, 387, (1926). Sage and Lacey, Trans. Am. Inst. Mining and Met. Mners., 136, 136 (1940). Sage, Schaafsma, and Lacey, Ind. Eng. Chen., 26, 1218 (1934). Burlew, J. Am. Chem. Soc., 62, 681, (1940). Gibson and Kincaid, J. Am. Chem. Soc., 60, 511 (1938). Gilliland and Lukes, Ind. Eng. Chem., 32, 957, (1940). Gornowski, Amick, and Hixson, Ind. Eng. Chem., 39, 1348, (1947). Smith, J. Res. Nat. Bur. Stand., 26, 129, (1941). Smith and Matheson, J. Res. Nat. Bur. Stand., 20, 641, (1938). Young, Sci. Proc. Roy, Dublin Soc., 12, 374, (1910). Sage, Backus, and Lacey, Ind. Eng. Chem., 27, 686, (1935). “g (09% ge uegeig euesueg-susdocg 2oz zogoeg £4; TTaTsseaducn ‘Tt eanSta euBsdorg *4od eugdoig °4°0d euedoarg °40d euvezgueg STON 6¢ STON O9 aTOoN ge euedoig “AT “Til “II "I ‘uy ‘Bg a2eg spunog ernsseag a OOS? 000% 00gE 000 00g¢ 000g = =—s OST OOOT 00g i FoF fT ee eee eee eee © a euBscerd UOT LoeLg e [oy b°6 9°O gto. ’°O __ 8°S 3°0 iO rt TT tt tT TT TW © *uT ‘be gegq eptumnog oCoas © . > ‘Ul ‘bg-aeg spunog GOOT Ep0ST 38 usgelg euBdogg~suesgueg LOFASUSE UCTANTOS : [RENT Wory eumMToOs, OPPpoeds fa Tangoy JO uotpetaeq jueomeg *g einsTy oe us ot U7. auBdoOas UOTLO@AY Soy —s &,09T ez 4 7 g*o raat "0 | a0 “7° meyslcq eusdodd-eue@lueg AOTARUaAG LOTINTCS [Rep] Woas einscedy etaqang fo UOTEH PASC FuBldeS oo BLT Tw GZuped 18. - TABLE I VOLUMETRIC BEHAVIOR OF PROPANE IN THE CONDENSED-LIQUID REGION 130° F, Vv Z (271.6) 003636 205626 03592 003563 03535 03488 03447 003403 03364 03329 03297 05268 03240 005215 03190 03150 03116 «03087 03051 02996 02952 002912 02875 202837 -06881 07580 21001 ol241 1477 1944 2401 22963 5514 4062 24595 5128 5644 6160 ©6668 ° 7681 8681 967 1.0630 1.2500 1.4388 1.6232 1.8047 1.9767 Figures in parentheses are vapor pres- 100° F. Pressure Vv V/ 1lb/sqein.abs. (188.2)8 Bubble Point 603391" .04685 200 -03389 .04976 300 003371 = 6.07425 400 . -03354 .09849 500 003338 1225 600 008322 .1462 800 003293 .1933 1000 203267 .2398 1250 003237 .2970 1500 003209 .3531 1750 003184 .4093 2000 03161 .4641 2250 203140 .5191 2500 003119 .5724 2750 203099 .6250 3000 03080 .6790 3500 203045 .7815 4000 03015 .8853 4500 02988 .9880 — 5000 -02964 1.0879 6000 02918 1.2826 7000 02878 1.4774 8000 02843 1.6696 9000 e02812 1.8597 10000 002782 2.0422 a sures in pounds per square inch absolute. b Volumes in cubic feet per pound. Pressure 1b/sq.in.abs. Bubble Point 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 19. TABLE I. (Cont'd.) 160° FB. 190° F, v Z Vv Z (383.9) (526.9) .03986 10146 .04874 .1624 .03974 .1054 -- -- .03908 .1295 -~ -- 203852 «41538 .04446 .1686 .03761 1995 204160 .2104 .03689 .2446 .04008 .2534 .03615 .2996 .03880 .3067 .03553 .3531 .03785 .3588 .03499 .4063 .03707 .4105 .03453 .4579 -03643 .4607 .03413 5092 .03588 .5110 .03377 5597 .03540 .5597 .03345 .6093 .03497 .6075 .03316 .6602 .03459 .6569 .03264 .7566 .03393 .7503 .03220 .8540 003337 .8441 .03180 .9502 .03289 .9345 .03145 1.0426 .03246 1.0265 .03080 1.2229 -03165 1.1986 .03028 1.4040 203109 1.3750 .02982 1.5818 .03057 1.5467 .02940 1.7562 .03010 1.7150 .02902 1.9242 .02966 1.8758 20. TABLE I. (Cont'd.) 220° F. Pressure Lb/sq.in.abs. Vv Z 200 07339 8873 300 04533 8221 400 3096 07487 500 22190 6620 600 21515 «5495 800 005152 .2491 1000 04569 2762 1250 04269 .3225 1500 204090 =.3706 1750 203966 .4198 2000 203871 .4680 2250 .03793 .5164 2500 o03727 §=«6. 6 56. 2 2750 -03670 .6095 3000 003621 .6573 3500 03537 = «6. 7476 4000 -03468 = .8385 4500 .03408 .9280 5000 003355 1.0141 6000 203266 1.1823 7000 -03194 1.3502 8000 003133 1.5151 9000 -03081 1.6779 10000 003035 1.8347 280° F, Vv z 68249 9164 .5233 68720 .3714 .8253 22793 07757 22167 .7227 01355 .6023 08593 = «64773 205991 = 641.59 .05148 ~=.4287 .04761 .4631 .04501 .5000 .04330 5417 .04196 .5826 .04091 .6242 .04004 .6678 03866 .7516 03761 8342 03669 .9180 03592 .9976 003470 «1.1544 .03374 1.3106 .03293 1.4633 .03226 1.6144 .03167 1.7592 Pressure 1b/sq.in.abs. 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 Vv 9110 5862 04236 5258 » 2604 «1780 21289 -09183 207170 -06136 05501 05112 04863 04660 04502 004271 »04102 -03970 03862 03694 003567 003466 03384 ~03310 340° FB, Z 9362 9036 «8707 08371 «8029 «7320 ©6627 5898 05523 05521 5652 5910 ©6246 «6577 26946 07672 8430 9188 ©9921 1.1565 1.2816 1.4246 1.5664 1.7007 TABLE I. Vv «9947 6459 04716 3670 02975 22107 1590 1188 09406 07830 06832 006171 05693 -05368 05118 004752 -04498 004312 04162 03936 003774 03647 03546 03458 el. (Cont'd.) 400° F. Z 9508 ©9261 ©9017 08772 8533 8057 7599 7098 »6740 «6554 -6530 «6642 6802 7048 07345 27941 08599 9283 09946 1.1265 1.2614 1.3944 1.5268 1.6527 460° FB, V Z 1.0767 29620 7039 09434 ~5176 09250 24059 29068 3317 -8891 02391 .8548 21841 08226 21409 -7870 21114 07472 209430 3=s- 67373 008231 3=.7354 007330 = 6.7375 206689 = 67471, -06200 = «7609 05832 =. 78 24 -05312 #.8298 004955 .8854 004696 .9450 04498 1.0047 004208 1.1257 -03998 1.2490 -03839 1.3721 03714 1.4949 -03613 1.6141 Pressure Lb1/Sq. In.Abs. Bubble Point 100 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 109000 BB. TABLE II SPECIFIC VOLUME OF BENZENE 100°F, (3.21)8 0.01862" 0.01859 0.01858 0.01857 0.01856 0.01855 0.01854 0.01851 0.01849 0.01845 0.01842 0.01839 0.01836 0.01832 0.01829 0.01826 0.01823 0.01816 0.01810 0.01804 0.01799 0.01790 0.01783 0.01776 0.01767 0.01758 160°F, (11.08) 0.01943 0.01941 0.01940 0.01938 0.01936 0.01935 0.01932 0.01928 0.01924 0.01920 0.01915 0.01910 0.01906 0.01902 0.01897 0.01893 0.01889 0.01881 0.01874 0.01867 0.01860 0.01848 0.01837 0.01826 0.01814 0.01804 220°R, (29.15) 0.02028 0.02026 0.02024 0.02021 0.02018 0.02015 0.02013 0.02008 0.02003 0.01997 0.01992 0.01987 0.01981 0.01976 0.01970 0.01965 0.01961 0.01952 0.01942 0.01932 0.01923 0.01907 0.01895 0.01882 0.01869 0.01856 280°R, (64.68) 0.02133 0.02131 0.02127 0.02123 0.02118 0.02114 0.02110 0.02102 0.02095 0.02087 0.02080 0.02073 0.02065 0.02058 0.02052 0.02045 0.02039 0.02027 0.02015 0.02003 0.01922 0.01974 0.01957 0.01940 0.01925 0.01911 a Figures in parentheses are vapor pressures in pounds per square inch absolute Specific volumes in cubic feet per pound 23. TABLE II. (Cont'd.) Pressure Lb./Sq. 340°R, 400°F, 460°R, In.Abs. (126.0) (222.06) (363.46) Bubble Point 0.02262 0.02441 0.02704 100 -- -~ «- 200 0.02258 -- -~ 300 0.02252 0.02432 -~ 400 0.02246 0.02422 0.02693 500 0.02241 0.02412 0.02665 600 0.02235 0.02402 0.02640 800 0.02224 0.02382 0.02598 1000 0.02214 0.02365 0.02562 1250 0.02200 0.02343 0.02526 1500 0.02188 0.02325 0.02494 1750 0.02176 0.02307 0.02466 2000 0.02165 0.02290 0.02442 2250 0.02155 0.02275 0.02420 2500 0.02145 0.02260 0.02400 2750 0.02136 0.02247 0.02381 5000 0.02128 0.02234 0.02362 3500 0.02113 0.02211 0.02330 4000 0.02099 0.02191 0.02300 4500 0.02085 0.02172 0,02274 5000 0.02071 0.02155 0.02250 6000 0.02048 0.02125 0.02210 7000 0.02025 0.02098 0.02177 8000 0.02005 0.02076 0.02147 9000 0.01988 0.02055 0.02121 10000 0.01973 0.02035 0.02098 Temperature OF, 100 160 220 280 340 400 460 Pressure Lb. /Sq. In.Abs. 32 11.1 29.2 64.7 126.0 22261 363.5 24. TABLE III. BUBBLE POINT Authors 0.01862 0.01943 0.02028 0.02133 0.02862 0.02441 0.02704 SPECIFIC VOLUME OF BENZENE AT Young 0.01862 0.01943 0.02028 0.02144 0.02278 0.02953 0.02716 % Deviation 0.0 0.0 0.0 0.5 0.7 0.5 0.4 Pressure Lb/Sq.In.Abs. 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 25. TABLE IV 100°F. v Z 0.03038" 0.04855 0.03022 0.07258 0.03012 0.09645 0.03002 0.12017 0.02992 0.14372 0.02973 0.19041 0.12955 0.2366 0.12935 0.2937 0.02916 0.3502 0.02898 0.4060 0.02882 0.4615 0.02866 0.5163 0.02851 0.5706 0.02837 0.6246 0.02823 0.02798 0.7840 0.02777 0.8893 0.02757 0.9932 0.02741 1.0972 0.02709 1.3013 0.02677 1.5002 0.02646 1.6947 0.02618 1.8863 0.02590 2.0735 SINGLE-PHASE VOLUMETRIC BEHAVIOR OF A MIXTURE OF PROPANE AND BENZENE WITH 88.27 MOLE PER CENT PROPANE 160°R, v Z 0.03385 0.09790 0.03360 0.12148 0.03336 0.14473 0.03292 0.19043 0.03252 0.2351 0.03208 0.2899 0.03171 0.3439 0.03139 0.3972 0.03111 0.4499 0.03086 0.5021 0.03063 0.5537 0.03042 0.6049 0.03022 0.6555 0.02985 0.7554 0.02950 0.8532 0.02918 0.9495 0.02892 1.0456 0.02846 1.2347 0.02807 1.4208 0.02770 1.6023 0.02735 1.7798 0.02701 1.9530 & Specific volumes in cubic feet per pound. Pressure Lb/Sq.In.Abs. 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 26. (Cont'd.) TABLE IV. 220°R, Vv v) 0.04103 0.1623 0.03876 0.2044 0.03734 0.2462 0.03623 0.2986 0.03540 0.3502 0.03475 0.4009 0.03419 0.4508 0.03372 0.5002 0.03331 0.5490 0.03293 0.5970 0.03260 0.6447 0.03199 0.7381 0.03147 0.8299 0.03102 0.9202 0.03063 1.0096 0.02997 1.1854 0.02942 1.3576 0.02897 1.5279 0.02857 1.6951 0.02816 1.8564 280°R, Vv Z 0.7377 0.8937 0.4605 0.8368 0.3195 0.7742 0.2330 0.7058 0.1719 0.6248 0.08387 0.4064 0.05151 0.3120 0.04369 0.3308 0.04180 0.3798 0.03982 0.4221 0.03857 0.4673 0.03760 0.5124 0.03681 0.5574 0.03613 0.6018 0.03555 0.6460 0.03460 0.7335 0.03378 0.8185 0.03316 0.9039 0.03257 0.9864 0.03160 1.1485 0.03088 1.3093 0.03032 1.4693 0.02983 1.6262 0.02936 1.7784 Pressure lb /sq.in. abs. 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 27. TABLE IV. (Cont'da.) 340°F, 400°F, Vv Z Vv Z 0.8020 0.8987 0.8962 0.9342 0.5225 0.8773 0.5787 0.9048 0.3732 0.8364 0.4192 0.8740 0.2821 0.7902 0.3232 0.8422 0.2217 0.7452 0.2594 0.8113 0.1440 0.6455 0.1791 0.7468 0.09736 0.5455 0.1316 0.6860 0.06687 0.4683 0.09560 0.6228 0.05444 0.4575 0.07468 0.5838 0.04853 0.4758 0.06274 0.5722 0.04540 0.5087 0.05568 0.5804 0.04331 0.5460 0.05126 0.6011 0.04169 0.5839 0.04818 0.6278 0.04045 0.6232 0.04594 0.6584 0.03943 0.6628 0.04424 0.6917 0.03782 0.7417 0.04144 0.7559 0.03660 0.8203 0.03960 0.8256 0.03560 0.8976 0.03827 0.8976 0.03479 0.9746 0.03732 0.9725 0.03349 1.1258 0.03562 1.1139 0.03248 1.2739 0.03427 1.2503 0.03171 1.4213 0.03329 1.3880 0.03111 1.5687 0.03251 1.5249 0.03060 1.7145 0.03188 1.6615 460°F. Vv 0.9747 0.6332 0.4629 0.3604 0.2921 0.2068 0.1570 0.1186 0.09421 0.07858 0.06830 0.06128 0.05639 0.05285 0.05017 0.04636 0.04373 0.04175 0.04022 0.03794 0.03625 0.03500 0.03402 0.03320 Z 0.9498 0.9255 0.9021 0.8780 0.8540 0.8062 0.7651 0.7220 0.6885 0.6700 0.6655 0.6718 0.6868 0.7081 0.7333 0.7905 0.8522 0.9153 0.9798 1.1091 122363 1.3642 1.4917 1.6175 Pressure Lb/Sq.In.Abs. 125 150 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 28. TABLE V. 100°F, Vv Z 0.02430 0.02921 0.02428 0.03502 0.02426 0.04666 0.02422 0.06987 0.02417 0.09297 0.02412 0.1160 0.02407 0.1389 0.02398 0.1845 0.02390 0.2298 0.02380 0.2861 0.02370 0.3418 0.02361 0.3973 0.02352 0.4523 0.02344 0.5071 0.02336 0.5615 0.02329 0.6158 0.08322 0.6698 0.02309 0.7771 0.02297 0.8835 0.02285 0.9887 0.02275 1.0938 0.02256 1.3015 0.02239 1.5070 0.02222 1.7092 0.02205 1.9082 0.02189 2.1048 SINGLE-PHASE VOLUMETRIC BEHAVIOR OF A MIXTURE OF PROPANE AND BENZENE WITH 59.83 Mole PER CENT PROPANE 160°R, v y) 0.02605 0.06787 0.02598 0.09026 0.02591 0.1125 0.02585 0.1347 0.02572 0.1787 0.02560 0.2223 0.02545 0.2763 0.02531 0.3297 0.02517 0.3826 0.02504 0.4349 0.02491 0.4868 0.02478 0.5380 0.02467 0.5892 0.02456 0.6399 0.02435 0.7402 0.02416 0.8393 0.02398 0.9372 0.02382 1.0344 0.02355 1.2272 0.02331 1.4171 0.02308 1.6036 0.02287 1.7876 0.02268 1.9698 Pressure 125 150 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 29. (Cont'd.) TABLE V. 220°R. Vv Z 0.02841 0.08998 0.02827 0.1119 0.02814 0.1337 0.02789 0.1767 0.02766 0.2190 0.02739 0.2711 0.02714 0.3223 0.02691 0.3729 0.02670 0.4228 0.02651 0.4723 0.02633 0.5212 0.02617 0.5699 0.02601 0.6178 0.02573 0.7130 0.02548 0.8070 0.02525 0.8997 0.02505 0.9917 0.02469 1.1729 0.02425 1.3496 0.02406 1.5240 0.02380 1.6960 0.02358 1.8670 280°R, ¥ Zz 0.9853 Q.8961 0.7983 0.8712 0.03197 0.1396 0.03118 0.1815 0.03059 0.2226 0.03000 0.2728 0.02954 0.3224 0.02917 0.3714 0.02885 0.4198 0.02855 0.4674 0.02827 0.5142 0.02802 0.5606 0.02776 0.6059 0.02733 0.6960 0.02695 0.7843 0.02662 0.8716 0.02633 0.9579 0.02587 1.1294 0.02545 1.2962 0.02509 1.4604 0.02477 1.6220 0.02448 1.7811 Pressure Lb /Sq. In. Abs. 150 200 250 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 30. TABLE V. (Cont'd.) 340°R, 400°F, v Z Vv Z 0.6456 0.8690 0.7202 0.9018 0.4963 0.8350 ~--- --- 0.3960 0.7995 0.4532 0.8512 --- --~ 0.1782 0.6692 me a — 0.09993 0.5005 0.03650 0.2457 0.05995 0.3753 0.03445 0.2898 0.04447 0.3480 0.03325 0.3357 0.03975 0.3733 0.03238 0.3814 0.03738 0.4095 0.03168 0,4251 0.03587 0.4491 0.03112 0.4713 0.03473 0.4892 0.03062 0.5152 0.03382 0.5293 0.03018 0.5586 0.03307 0.5694 0.02980 0.6017 0.03244 0.6093 0.02917 0.6871 0.03143 0.6887 0.02865 0.7713 0.03065 0.7675 0.02819 0.8538 0.03000 0.8452 0.02780 0.9355 0.02945 0.9219 0.02714 1.0960 0.02858 1.0736 0.02658 1.2523 0.02790 1.2227 0.02612 1.4064 0.02730 1.3673 0.02573 1.5586 0.02680 1.5100 0.02545 1.7129 0.02642 1.6540 460°R, V 0.7859 0.5017 0.3604 0.2741 0.2160 0.1423 0.09803 0.06655 0.05267 0.04609 0.04228 0.03993 0.03836 0.02703 0.03590 0.03427 0.03312 0.03214 0.03135 0.03011 0.02922 0.02855 0.02800 0.02748 Z 0.9198 0.8808 0.8437 0.8020 0.7584 0.6660 0.5737 0.4868 0.4623 0.4720 0.4948 0.5257 0.5612 0.5955 0.6303 0.7019 0.7753 0.8464 0.9173 1.0572 1.1970 1.2366 1.4747 1.6081 Pressure Lb/Sq.In.Abs. 100 125 150 31. TABLE VI. 100°, v Z 0.02195 0.02364 0.02194 0.02959 0.02193 0.03542 0.02192 0.04721 0.02189 0.07072 0.02187 0.09421 0.02184 0.1176 0.02182 0.1410 0.02177 0.1876 0.02172 0.2339 0.08165 0.2914 0.02159 0.3488 0.02153 0.4057 0.02147 0.4624 0.02141 0.5188 0.02135 0.5748 0.02129 0.6298 0.08124 0.6862 0.08115 0.7972 0.02106 0.9072 0.02097 1.0162 0.02089 1.1248 0.02074 1.3401 0.02061 1.5526 0.02050 1.7661 0.02040 1.9772 0.02031 2.1872 SINGLE-PHASE VOLUMETRIC BEHAVIOR OF A MIXTURE OF PROPANE AND BENZENE WITH 39.48 MOLE PER CENT PROPANE 160°R, v Z 0.02327 0.04526 0.02324 0.06781 0.02380 0.09025 0.02316 0.1126 0.02312 0.1349 0.02304 0.1793 0.02297 0.2234 0.02287 0.2780 0.02278 0.3323 0.02270 0.3864 0.02262 0.4400 0.02253 0.4930 0.02245 0.5459 0.02237 0.5983 0.02230 0.6507 0.02216 0.7543 0.02202 0.8566 0.02191 0.9589 0.02180 1.0601 0.02158 1.2593 0.02141 1.4576 0.02125 1.6534 0.02110 1.8469 0.02096 2.0385 Pressure Lb/Sq.In.Abs. 100 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 32. (Cont'd.) TABLE VI. 220°R, Vv Z 0.02490 0.06624 0.02482 0.08803 0.02474 0.1097 0.02466 0.1312 0.02452 0.1739 0.02439 0.2163 0.02424 0.2687 0.02410 0.3205 0.02397 0.3719 0.02385 0.4229 0.02374 0.4736 0.02363 0.5238 0.02352 0.5735 0.02342 0.6230 0.02322 0.7206 0.02305 0.8175 0.02289 0.9133 0.02274 1.0082 0.02247 1.1954 0.02225 1.3810 0.02204 1.5634 0.02185 1.7437 0.02169 1.9232 280°R, v Z 1.0938 0.8912 0.02688 0.1095 0.02676 0.1308 0.02653 0.1729 0.02632 0.2145 0.02607 0.2655 0.02583 0.315” 0.02561 0.3652 0.02539 0.4138 0.02520 0.4620 0.02502 0.5097 0.02487 0.5573 0.02472 0.6043 0.02445 0,6973 0.024282 0.7894 0.02402 0.8807 0.02383 0.9708 0.02349 1.1484 0.02317 1.3215 0.02289 1.4921 0.02264 1.6602 0.02242 1.8268 53. TABLE VI. (Cont'd.) Pressure 340°R, 400°F, Lb/Sq.In.Abs. Vv Z Vv Z 100 1.2221 0.9210 --~ --~ 125 0.9554 0.9000 1.0564 0.9258 150 0.7758 0.8770 0.8653 0.9100 200 0.5507 0.8300 0.6249 0.8762 300 -—= --- 0.3826 0.8046 400 “<= --~ 0.2572 0.7213 500 --- --~ --= --- 600 --= -—- --= — 800 0.02953 0.1780 --~ “<= 1000 0.02953 0.1780 0.03375 0.2366 -1250 0.02848 0.2683 0.03226 0.28287 1500 0.02804 0.3170 0.03127 0.3288 1750 0.02766 0.3648 0.03050 0.3742 2000 0.02732 0.4118 0.02990 0.4192 2250 0.02702 0.4582 0.02939 0.4636 2500 0.02676 0.5042 0.02897 0.5077 2750 0.02652 0.5496 0.02858 0.5510 3000 0.02629 00,5944 0.02824 0.5939 3500 0.02589 0.6829 0.02765 0.6785 4000 0.02556 0.7705 0.02716 0.7616 4500 0.02527 0.8570 0.02676 0.8442 5000 0.02502 0.9428 0.02639 0.9251 6000 0.02456 1.1106 0.02577 1.0840 7000 0,02415 1.2740 0.02523 1.2382 8000 0.02381 1.4355 0.02479 1.3904 9000 0.02350 1.5939 0.02441 1.5402 10000 0.02319 1.7477 0.02406 1.6868 0.9438 0.6896 0.4338 0.3037 ‘0.2237 0.1688 0.09194 0.05180 0.04028 0.03674 0.03479 0.03349 0.03247 0.03165 0.03105 0.03053 0.02963 0.02893 0.02835 0.02785 0.02704 0.02636 0.02577 0.02530 0.02490 0.9278 0.9039 0.8528 0.7960 0.7330 0.6636 0.4820 0.3395 0.3300 0.3612 0.3990 0.4390 0.4788 | 0.5185 0.5595 0.6002 0.6796 0.7584 0.8361 0.9126 1.0632 1.2093 1.3511 1.4922 1.6318 TABLE VII. SINGLE-PHASE VOLUMETRIC BEHAVIOR OF A MIXTURE OF PROPANE AND BENZENE WITH 19.56 MOLE PER CENT PROPANE 100°R. 160°R, Pressure Vv Z Vv Z hb/Sq.In.Abs. -80 0.02020 0.01922 --- --- 100 0.02019 0.02402 --- --- 125 0.02019 0.03002 0.02121 0.02849: 150 0.02018 0.03601 0.02120 0.03417 200 0.02017 0.04799 0.02117 0.04549 300 0.02016 0.07195 0.02113 0.06811 400 0.02014 0.09584 0.02109 0.09064 500 0.02012 0.1197 0.02105 0.1131 600 0.02010 0.1435 0.02102 0.1355 800 0.02007 0.1910 0.02095 0.1802 1000 0.02004 0.2384 0.02088 0.2243 1250 0.01999 0.2973 0.02081 0.2795 1500 0.01994 0.3558 0.02074 0.3343 1750 0.01990 0.4143 0.02068 0.3888 2000 0.01986 0.4725 0.02063 0.4433 2250 0.01982 0.5305 0.02058 0.4975 2500 0.01977 0.5880 0.02053 0.5515 2750 0.01973 0.6455 0.02049 0.6054 3000 0.01969 0.7027 0.02045 0.6592 3500 0.01962 0.8169 0.02036 0.7657 4000 0.01954 0.9298 0.02027 0.8712 4500 0.01947 1.0423 0.02018 0.9757 5000 0.01940 1.1539 0.02009 1.0793 6000 0.01927 1.3754 0.01994 1.2855 7000 0.01913 1.5930 0.01979 1.4884 8000 0.01900 1.8082 0.01968 1.6916 9000 0.01889 2.0225 0.01957 1.8924 10000 0.01882 2.2389 0.01945 2.0898 Pressure Lb/Sq.In.Abs. 200 300 400 500 600 800 1000 1250 1500 1750 2000 2250 2500 2750 3000 3500 4000 4500 5000 6000 7000 8000 9000 10000 35. TABLE VII. (Cont'd.) 220°R, v Z 0.02230 0.04368 0.02226 0.06541 0.02222 0.08705 0.02218 0.1086 0.02214 0.1301 0.02206 0.1789 0.02198 0.2153 0.02189 0.2680 0.02180 0.3203 0.02172 0.3723 0.02163 0.4237 0.02155 0.4749 0.02148 0.5260 0.02141 0.5767 0.02134 0.6270 0.02122 0.7274 0.02110 0.8266 0.02100 0.9256 0.02090 1.0235 0.02072 1.2176 0.02052 1.4069 0.02037 1.5961 0.02023 1.7833 0.02009 1.9677 280°R, Vv Zz 0.02377 0.06419 0.02371 0.08536 0.02365 0.1064 0.08359 0.1274 0.02348 0.1691 0.02337 0.2104 0.02323 0.2614 0.02310 0.3119 0.02298 0.3620 0.02286 0.4115 0.02275 0.4607 0.02264 0.5095 0.02253 0.5577 0.02243 0.6057 0.02225 0.7009 0.02207 0.7946 0.02192 0.8878 0.02177 0.9797 0.02150 1.1611 0.02127 1.3401 0.02107 1.5172 0.02091 1.6939 0.02075 1.8677 36. TABLE VII. (Cont'd.) Pressure 340°R . 400°R . tb/Sq.In.Abs. Z V Z 400 0.02569 6.08555 — a 500 0.02556 0.1064 oe — 600 0.02542 0.1270 0.02831 0.1316 800 0.02517 0.1676 0.02777 0.1721 1000 0.02495 0.2077 0.02730 0.2114 1250 0.02473 0.2574 0.02684 0.2598 1500 0.02453 0.3063 0.02645 0.3073 1750 0.02435 0.3548 0.02612 0.3540 2000 0.02420 0.4030 0.02582 0.3999 2250 0.02405 0.4505 0.02556 0.4454 2500 0.02390 0.4975 0.02533 0.4904 2750 0.02376 0.5440 0.02512 0.5350 3000 0.02362 0.5900 0.02492 0.5790 3500 0.02337 0.6810 0.02459 0.6666 4000 0.02313 0.7703 0.02430 0.7528 4500 0.02292 0.8587 0.02402 0.8371 5000 0.02272 0.9458 0.08375 0.9197 6000 0.02237 1.1175 0.02328 1.0818 7000 0.02207 1.2862 0.02290 1.2415 8000 0.02180 1.4520 0.02258 1.3990 9000 0.02160 1.6185 0.02232 1.5558 10000 0.02141 1.7825 0.02208 1.7100 0.03262 0.03108 0.03000 0.02921 0.02858 0.02806 0.02762 0.02723 0.02688 0.02657 0.02605 0.02562 0.02525 0.02492 0.02437 0.02390 0.02347 0.02311 0.02277 0.1889 0.2250 0.2715 0.3172 0.3621 0.4063 0.4499 0.4928 0.5351 0.5771 0.6601 0.7419 © 0.8226 0.9020 1.0506 1.2112 1.3593 1.5058 1.6484 TABLE VIII. 37. VOLUMETRIC DATA FOR A TWO-PHASE MIXTURE OF PROPANE AND BENZENE WITH 88.27 MOLE PER CENT PROPANE _ 100° F. _ 160° F. Pressure Pressure 1b./sq.in. Vv Z 1b./sqein. Vv Z abs. abs. 100 0.9243 0.7400 160 0.6787 0.7852 110 0.8006 0.7050 200 0.49283 0.7120 120 0.6893 0.6622 240 0.3573 0.6200 130 0.5804 0.6040 280 0.2343 0.4744 140 0.4638 0.5198 320 b 0.07909 0.1830 150 0.3368 0.4045 328.9 0.03402 0.08091 160 b 0.1600 0.2050 165.4 0.03035 0.04019 _ 220°R, Pressure 1b./sqein. Vv Z abs. 150 0.9002 0.8902 200 0.6479 0.8542 250 0.4939 0.8140 300 0.3854 0.7623 350 0.0325 0.6980 400 0.2366 0.6240 450 0.1801 0.5343 500 0.1275 0.4202 550 b 0.06867 0.2490 571.8 0.04152 0.1565 db Bubble=point pressure 38. TABLE Ix. VOLULISTRIC DATA FOR A TiWO-PHASE MIXTURE OF PROPANE AND BENZENE WITH 59.83 MOLE PER CENT PROPANE __ 100°. 160°R. Pressure Pressure 1b./sq.in. 7 Z 1b./sq.in. Vv Z abs. ads. 60 0.8386 0.4838 80 0.8168 0.5675 70 0.6570 0.4422 100 0.6002 0.5213 80 0.5142 0.3955 120 0.4550 0.4742 90 0.3934 0.3404 140 0.3486 0.4239 100 0.2820 0.2712 160 0.2654 0.3688 110 0.1695 0.1793 180 0.1946 0.3042 120 b 0.04888 0.05640 200 0.1304 0.2265 122.1 0.02431 0.02854 220 b 0.06600 0.1261 232.4 0.02608 0.05264 _ 220°R, 280°R, Pressure Pressure 1b./sq.in. Vv Z lb./sq.in. V Z abs. abs. 120 0.7137 0.6782 168.5% 0.6949 0.8520 160 0.4578 0.5800 200 0.5137 0.7475 200 0.2189 0.5050 250 0.3509 0.6382 240 0.2302 0.4375 300 0.2562 0.5592 280 0.1629 0.3612 350 0.1925 0.4901 320 0.1083 0.2774 400 0.1453 0.4230 360 b 0.06241 0.1779 450 0.1084 0.3548 392.0 0.02842 0.08821 500 0.07884 0.2868 550 b 0.05243 0.2138 595.4 0.03200 0.1386 Bubble-point pressure Dew-point pressure 39. TABLE IX. (Cont'd.) B40°R Pressure 1b./sq.in. Vv Z abs. 345.8% 0.3293 0.7665 350 0.3224 0.7595 400 0.2518 0.6780 450 0.2007 0.6080 500 0.1621 0.5455 550 0.1323 0.4896 600 0.1083 0.4375 650 0.08869 0.3880 700 0.07174 0.3380 750 0.05711 0.2883 g00 0.04430 0.2385 823.2 0.03913 0.2168 b Bubble-point pressure & Dew-point pressure 40. TABLE X. VOLULINTRIC DATA FOR A TWO-PHASE WIXTURE OF PROPANS AND BENZENE WITH 39.48 MOLE PER CENT PROPANE 1LOO°F. _ 160°F, Prassure Pressure 1b./sqein. Vv Z 1b./sq.in. Vv Z abs. abs. . 80 0.1292 0.3648 60 0.6772 0.3952 40 0.7603 0.3275 80 0.4303 0.3348 50 0.5315 0.2862 100 0.2959 0.2878 60 0.3722 0.2405 120 0.1934 0.2257 70 0.2507 0.1890 140 0.1219 0.1660 80 0.1459 0.1257 160 » 0.06169 0.09600 90 b 0.05757 0.05580 174.3 0.02328 0.03946 94.4 0.02195 0.02231 _ 220 F. 280 F, Pressure Pressure 1b./sq.in. Vv Z 1b./sqein. V Z abs. abs. 120 0.3799 0.4042 113.0% 0.9484 0.8732 160 0.2278 0.3232 120 0.8069 0.7890 200 0.1390 0.2465 160 0.3931 0.5579 240 0.07810 0.1662 200 0.2766 0.4507 280 0.03243 0.08051 240 0.1929 0.3772 282.3? 0.02492 0.06238 280 0.1381 0.3150 320 0.09880 0.2576 360 0.06822 0.2001 400 b 0.04427 0.1443 435.8 0.02695 0.09570 Bubble-point pressure Dew-point pressure TABLE X. 340°, Pressure 1lb./sq.in. v Z abs. 223.1" 0.4805 0.8079 250 0.3607 0.6795 300 0.2380 0.5380 350 0.1684 0.4442 400 0.12353 0.3717 450 0.09188 0.3116 500 0.06820 0.2570 550 0.04941 0.2048 600 b 0.03379 0.1528 615.2 0.03010 0.1396 b a 41. (Cont'd.) 400°F, Pressure 1lb./sq.in. V 2, abs. 410.3° 0.2478 0.7128 450 0.1940 0.6120 500 0.1481 0.5193 550 0.1167 0.4500 600 0.09331 0.3925 650 0.07547 0.3439 700 0.06083 0.2985 750 0.04884 0.2568 800 | 0.03851 0.2160 814.3 0.03600 0.2055 Buoble-point pressure Dew-point pressure 42. FABLE XI. VOLUMETRIC DATA FOR A TWO-PHASE MIXTURE OF PROPANE AND BENZENE WITH 19.56 MOLE PER CENT PROPANE 100°F, 160°R. Pressure Pressure 1b./sqein. V Zz 1b/sqein. Vv Zz abs. abs. 45 0.1303 0.06975 75 0.1243 0.1002 50 0.08154 0.04850 80 0.1019 0.08760 55 0.04244 0.02777 85 0.08157 0.07450 60 0.02208 0.01576 90 0.06332 0.06123 60.6 0.02020 0.01456 95 0.04203 0.04290 100 0.03312 0.03559 105 5 0.02446 0.02760 107.3 0.02123 0.02448 220°R, _ 280°R. Pressure Pressure 1lb./sq.in. v Z 1b./sq.in. Vv Z abs. abs. 120 0.1097 0.1289 180 0.1084 0.1757 130 0.08630 0.1099 200 0.07933 0.1428 140 0.06672 0.09150 220 0.05676 0.1124 150 0.04988 0.07330 240 0.03935 0.08501 160 0.03633 0.05695 260 , 0.02568 0.06010 170, 0.02493 0.04152 263.1 0.02380 0.05636 172.6 0.02231 0.03772 b Bubble-point pressure 43. TABLE XI. (Cont'd.) 340°F, 400°R, Pressure Pressur a4 1b./sqein. Vv Z 1b./sqein. Vv Z abs. abs. 260 0.1128 0.2442 380 0.1081 0.3182 280 0.08991 0.2096 400 0.09151 0.2835 300 0.07159 0.1788 420 0.07756 0.2523 320 0.05638 0.1502 440 0.06568 0.2238 340 0.04518 0.1279 460 0.05538 0.1973 %60 0.03487 0.1045 480 0.04673 O.1L737 380 7 0.02671 0.08450 500 0.03988 0.1525 383.7 0.02575 0.08226 520 b 0.03300 0.1329 536.6 0.02852 0.1185 | 460°R. Pressure Lb fsq.in. Vv Z abs. 520 0.1245 0.4687 540 0.1075 0.4202 560 0.09353 0.3792 580 0.08228 0.4455 600 0.07270 0.3158 620 0.06416 0.2880 640 0.05657 0.2621 660 0.04985 0.2382 680 0.04394 0.2163 700 b 0.03870 0.1961 720.8 0.03369 0.1758 & Bubble-point pressure