Volumetric Behavior of Propene and Three Mixtures of Propene and l-Butene Citation Farrington, Paul Stephen (1948) Volumetric Behavior of Propene and Three Mixtures of Propene and l-Butene. Engineer's thesis, California Institute of Technology. doi:10.7907/k5r4-tb84. https://resolver.caltech.edu/CaltechTHESIS:09172025-030633581 Abstract The volumetric behavior of propene was investigated at temperatures from 40° to 460° F. and pressures from 10,000 pounds per square inch absolute to values well below vapor pressure at 40° F. The results are tabulated and are compared graphically with the data of other investigators. Three mixtures of propene and 1-butene were subjected to volumetric study at temperatures from 40° to 280° F. in the pressure range from 10,000 to about 100 pounds per square inch absolute. The results are tabulated separately for the single-phase and two-phase regions pf each mixture. Variations of actual behavior from that 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): Sage, Bruce H. (advisor) Lacey, William Noble (advisor) Thesis Committee: Unknown, Unknown Defense Date: 1948 Record Number: CaltechTHESIS:09172025-030633581 Persistent URL: https://resolver.caltech.edu/CaltechTHESIS:09172025-030633581 DOI: 10.7907/k5r4-tb84 Default Usage Policy: No commercial reproduction, distribution, display or performance rights in this work are provided. ID Code: 17684 Collection: CaltechTHESIS Deposited By: Ben Maggio Deposited On: 04 Oct 2025 12:41 Last Modified: 04 Oct 2025 12:55 Thesis Files PDF - Final Version See Usage Policy. 13MB Repository Staff Only: item control page

VOLill\.1EI1RIC BEHAVIOR OF PROPENE AND THREE :MIXTURES OF PROPE1TE A...WD 1-BUTENE Thesis by Paul Stephen Farrington In Partial Fulfillment of the Requirements For the Degree of Chemical Engineer California Institu~e of Technology Pasadena, California 1948 ACKNOWLEDGEMENT The advice and guidance of Professors B. H. Sage and w. N. Lacey have been most helpful. In connection with the experimental work the assistance of H. H. Reamer is greatly appreciated. This investigation was sponsored by the Socony Vacuum Oil Company. ABSTRACT The volumetric behavior of p:ropene was investigated at temperatures from 40° to 460° F. and pressures from 10,000 pounds per square inch absolute to values well below vapor pressure at 40 0 F. The :results are tabulated and are com- pared graphically with the data of other investigators. Three mixtures of p:ro,pene and 1-butene were subo jected to volumetric study at temperatures from 40 to 280 0 F. in the pressure range from 10,000 to about 100 pounds per square inch absolute. The :results are tabulated separate- ly for the single-phase and two-phase regions pf each mixture. Variations of actual behavior from that of ideal solutions are shown graphically. TABLE OF CONTEN'TS Page A. VOLIDiETRIC BEHAVIOR OF PROPENE. • • • • • • • • • • • 1 I. Introduction. • • • • • • • • • • • • • • • • • 1 II. Methods and Apparatus • • • • • • • • • • • • • 2 III. Materials • • • • • • • • • • • • • • • • • • • 3 IV. Experimental Results • • • • • • • • • • • • • • 4 B. VOLUMETRIC BE..T-I.AVIOR OF THREE MIXTURES OF PROPENE A.t.~D 1-BUTENE • . . . • . • • • • • • • • I. Introduction • • • • • • • • • • • • • • • • • II. Methods and Ap:i;:aratus III. Materials 9 9 • • • • • • • • • • • • • 9 • • • • • • • • • • • • • • • • • • • 10 IV. Experimental Result.s . . • • • • • • • • • • • • 10 Nomenclature • • • • • • • • • • • • • • • • • • • • 14 References • • • • • • • • • • • • • • • • • • • • • 15 LIST OF FIGURES Page 1. Comparison of Values of Residual Vapor Pressure of Propane • • 2. Compressibility Factor for the Propane1-Butene System at 280° F• . . . . . • • • • • Deviation of Bubble-Point Pressure from Raoul t' s Law for Prop ene1-Butene Mixtures at 160° F • . • • • • • • • • 18 Percentage Deviation of Actual Specific Volume from Ideal Solution for 0 Propene-1-Butene Mixtures at 160 F. 19 3. 4. .• • • • • • • • • • • • • 16 17 LIST OF TABLES Page I. II. III. IV. v. VI. VII. VIII. IX. .. . Volumetric Behavior of Propane • • • • • • Properties of Coexisting Liquid and Gas Phases of Propane • • • • • • • • • • Latent Heat of Vapori zetion. of Propane • • • • • Single-Phase Volumetric Behavior of a Mixture of Propane and 1-But.ene With 17.050 Mole Per Cent 1-Butene • • • • • • • • Single-Phase Volumetric· Bebavio,r of a Mixture of Propane and 1-Butene With 33.153 Mole Per Cent 1-Butene • • • • • • • • Single-Phase Volumetric Behavior of a M:ix:ture of Propane and 1-Butene With 69.050 Mole Per Cent 1-Butene • • • • • • • • Two-Phase Volumetric Data for a Mixture of Propane and 1-Butene With 17.050 Mole Per Cent 1-Butene • • • • • • • • • • • Two-Phase Volumetric Data fo.r a Mixtu:re of Propane and 1-Butene With. 33.153 Mole Per Cent 1-But.ene • • • • • • • • • • • Two-Phase Volumetric Data for a Mixture of Propane and 1-Butene With. 69.050 Mole Per Cent 1-But:ene • • • • • • • • • • • 20 24 25 26 29 32 35 36 38 1. A. VOLUMETRIC BF.HAVIOR OF PROPENE I. INTRODUCTION Information concerning the vapor pressure and volumetric behavior of propene is of value in industrial practice since this hydrocarbon can serve as the starting point in the preparation of a relatively large number of compounds. Experimental data pertaining to this substanee a:re scattered and incomplete except fo:r the recent studies of Vaughan and Graves (7). Their work covered the in- fluence of pressure and temperature upon the sp_ecifio volume of propane at pressures up to approximately 1200 pounds per square ineh absolute for temperatures between 32 573° F. 0 and The measurements were carried out in glass over mercury, and contributed the most c0mplete data available for this olefin. Limited information concerning the vapor pressure of this hydrocarbon was presented by Gilliland and Scheeline (2). The specifie weight of the bubble-point liquid and dew-point gas near the cl'i ti cal temp eratu:re was studied by Winkler and Maass (8). Seibert and Burrell (6) determined the critical constants and vapor pressure of propane, whereas Powell and Giauque (3) established the heat capacity, the specific volume at atmospheric pressure, and certain other physical properties of this compound. The specifi~ volume at atmospheric pressure was also determined by Batuecas (1) and Roper (4). II. METHODS AND APPARATUS The equipme·nt employed in the volumetric studies reported was described earlier (5). In principle it con- sisted of a stainless steel chamber whose effective volume could be varied by introducing or withdrawing mercury. This chamber was submerged in an agitated oil bath, the t emperature of which was controlled within 0.03 0 F. of the desired value. below 100 0 In order to extend this work to temperatures F., a cooling unit was added. Kerosene was with- drawn from the chamber oil bath, passed over freon-cooled coils, and returned to the oil bath. Mechanical agitation of the contents of the chamber was provided .b y a cylindrical cage of vertical rods activated by means of an electromagnet rotating about the outside of the chamber. The samples of propane were introduced into the apparatus in accordance with a weighing bomb technique that has been described (5). The uncertainty in the weight of the material added was probably less than 0.1%. After introducing the propane the pressure within the equipment was raised to the desired upper value by injecting mercury. The oil bath was maintained at a predetermined temperature and after equilibrium had been attained as indicated by the .constancy of pressure with respec t to time, the total volume occupied by 3. the hydrocarbon was determined. The pressure was then de- creased somewhat and the process repeated. From these . measurements a series of corresponding equilibrium values of pressure and total volume were obtained for each of several temperatures. The same procedures were employed in the gas, liquid, and heterogeneous regions. III. MATERIALS The propane employed in this investigation was obtained from the Phillips Petroleum Company and a special analysis of the sample submitted indicated that it contained less than 0.005 mole fraction of material other than propane. The hydrocarbon as received was subjected to fractionation at atmospheric pressure in a column packed with small glass helices. The reflux ratio was approximately 40 to 1 and the first tenth and last fifth of the material were discarded in the course of each fractionation. At 100° F. the purified material showed 0~6 pound per square inch change in vapor pressure from bubble point to dew point. Two separate purifications were carried out in order to obtain an adequate supply for investigating the volumetric behavior of this compound. The material after purification was stored in a steel bomb until it was transferred to the volumetric equipment. 4. IV. EXPERDvillNTAL RESULTS Of the three samples of propane employed, the largest weighed approximately 0.22 pound and was used in the study of the condensed-liquid and single-phase regions at the higher pressures. An intermediate sample weighing approximately 0.06 pound was employed for investigations in the critical region and for studies at intermediate pressures at the higher temperatures. A small sample of about 0.015 pound was used for the study of the low-pressure, gaseous region and provided information concerning the specific volume o o· at dew point for 40, 70, and 100 0 F. Dew-point data at temperatures from 130° to 190° F. were obtained from the measurements with the sample of intermediate size. The range of specific volumes investigated with a given filling of the apparatus was such that it overlapped those measured with another sample. Upon completing a series of measurements covering twelve temperatures between 40 0 and 460 0 F. a redetermination of total volumes at 100° F. as a function of pressure was made in order to detect occurrence of any change in the sample. In the case of the intermediate and small samples no significant change in the characteristics of the material was noted. However, in the case of the larger sample a slight diminution in the total volume of the system was detected and it was not possible to recover by conventional highvacuum weighing bomb techniques {5) all of the sample 5. ori ginally introduced. Upon opening the equilibrium vessel a small quantity of an oily liquid was found. This poly- merized material apparently resulted from keeping the Jm.rge sample at temperatures above 400° F. for approximately 25 hours. Du.ring this interval the system was at pressures in excess of 5000 pounds per square inch for about 6 hours. At points at which the data for the large sample overlapped those for the intermediate sample the only significant discrepancy in specific volume was noted at 460 :reasons the data at 460 0 o F. For these F. and pressures above 1500 pounds per square inch may involve uncertainties of as much as 0.25% beyond those associated with the measurements at the lower pressures and temperatures. The experimental data for the three sets of measurements were compared in terms of the residual specific volume,.!, and the compressibility factor, z. The maximum difference found between the specific volumes as established from two samples was 0.43%. The average devia- tion of the specific volume at some 50 states taken in the :regions where comparisons were possible was 0.21%. A careful :review of the uncertainties in the absolute values of the pressure, temperature, total volume, and weight of sample indicates that the :recorded specific volume at a particular pressure and temperature probably does not involve an uncertainty greater than 0.3%. The vapor pressure of propane at 100 0 F. was also determined in another apparatus which utilized an independent set of temperature and pressure measuring instruments. The 6. value so obtained was 227.1 pounds per square inch, which agrees well with the vapor pressure of 227.3 pounds per square inch as found in this investigation. For the gaseous region from infinite attenuation to about 500 pounds per square inch (or dew point at tempo eratures below 180 F.) the smoothing of experimental data was accomplished by means of the residual specific volume, Smooth curves of the compressibility factor were most useful for the intermediate pressure range above 600 pounds per square inch; the upper pressure limit varied from 2000 pounds per square inch at 220 inch at 460 0 F. 0 F. to 6000 pounds per square All other data were correlated by means of the specific volume. In all oases· the values o_f the functions mentioned were smoothed with respect to pressure and temperature. The specific volume and compressibility factor are recorded in Table I for even values of the pressure at each of the temperatures experimentally studied. In the vicinity of the critical state, an added uncertainty of as much as 0.1% is to be expected. The values of the specific volume at bubble point and dew point and of the two-phase pressure are also recorded in Table I for temperatures below 190° F. The vapor pressure of propane has been meas~red by other investigators (2, 6, 7). Figure 1 presents comparative values of the residual vapor pressure as a function of temperature. For this comparison the residual vapor pressure is used to magnify divergences and is defined by the following 7. two equations: p" - P" ( l) r : 5.48144 - 1747 • 6 (2) T The divergence of the earlier measurements of Seibert and Burrell (6) from the later results of Vaughan and Graves (7) and from the present ones is clearly evident. The measurements of Gilliland and Scheeline (2) also differ markedly from the present data. The values of vapor pres- sure recorded in Table I were obtained from the smooth curve of Figure 1 and Equations land 2. The critical temperature has been observed by several investigators (6, 8) and the data are in reasonable agreement. From a review of available data, 197.0° F. was chosen as the crit,ical temperature of propane, whereas 196.5 0 F. was established by Vaughan and Graves (7). - Extrapolation of the relation of vapor pressure to temperature from 190 0 F. to the critieal temperature gave a value of 668 pounds per square inch. This compares with a value of 667 pounds per square inch reported by Vaughan and Graves (7). It is be- lieved that this value is within 3 pounds per square inch of the true critical pressure. An extrapolation of the average of the specific weights of the dew-point gas and bubble-point liquid from 190° F. to 197° F. gave a value for the specific volume at the critical state of 0.06944 cubic feat per pound. a. Two other published values (7, 8) for the critical specific volume are 0.0687 and 0.06916 cubic foot per pound respectively. In the interest of convenience in the utilization of data the compressibility factor and specific volume for the dew-peint gas and bubble-point liquid and the two-phase temperature have been recorded for a series of even values of pressure in Table II. The values of the two-phase temp- erature were obtained from a plot of l" versus pressure and equations land 2. It is believed that the uncertainty in the two-phase temperatures cited is not greater than 0.07° F. The volumetric behavior of propane is similar to that of other hydrocarbons when compared on a reduced basis. The volumetric data submitted in Table I supplemented by values of the heat capacity as a function of temperature (3) afford sufficient information to permit the thermodynamic properties of this hydrocarbon to be established. As an application of the data of Table I, the Clapeyron equation was used to obtain values of the latent heat of vaporization for several temperatures. Table III. The results are contained in For comparison, values obtained by Vaughan and Graves (7) are included in this tabulation. B. VOLUME'.r.RIC BEHAVIOR OF THREE MIXTURES OF PROPENE AND 1-BUTENE I. INTRODUCTION Although information concerning the volumetrio behavior of mixtures of satu:rated hydrocarbons is constantly increasing in amount, combinations of unsaturated compounds have received little attention. In connection with the propene-1-butene system, volumetric data for 1-butene (9) and for propane (Part A) are available; however, no published data for mixtures were found. Previous investigation (9) indicated that 1-butene deteriorates markedly at temperatures above 300 0 F. For this reason it was necessary to restrict the temperature range of the present work to a maximum of 280 II. 0 F. MErHODS AND APPARATUS The apparatus and procedure described in Part A were employed for this work. Samples were made up by two additions to the equilibrium cell. The 1-butene was added first, then the propane. Change of sample size for a given mixture was ac- complished by removing a portion of the sample while the temperature was high enough to insure homogeneity of the system. 10. III • MATERIALS The propane used for these mixtures was part of the lar ge quantity which was purified for the investigation of the pure substance (Part A). The 1-butene was prepared by dehydration of n-butanol with activated alumina used as a catalyst. A de- tailed description of the apparatus, preparation pro ce duxe, ai1o. met hod of puri f ication may be found in the literature (9). Before producing 1-butene for the third mixture, the 4-8 mesh catalyst was replaced with 8-14 mesh granular alumina. As a result the optimum flow rate of li quid n-butanol was increased from about 35 to about 65 drops per minute. When vaporized at 130° F., a portion of the purified 1-butene showed 0.7 pound per square inch change in vapor pressure between bubble point and dew point. IV. EXPERIMENTAL RESULTS On a molal basis the three mixtures contained 17% (17.050%}, 33% (33.153%), and 69% (69.050%) 1-butene, respectively • . The initial sample wei ght for each mixture was about 0.17 pound. After completing a series of measurements up to maximum volume of the equilibrium cell for each of the seven temperatures between 40° and 280° F., the sample wei ght was reduced to about one-tenth of its original value. In this way a lar ge and a small sample were obtained for each mixtul'e, and the entire pressure rang e from about 100 to 10,000 pounds 11. per square inch was effectively covered. Although an over- lap of specific volumes was achieved for each pair of sample weights, comparison of overlapping values is not as significant as in the ease of propane (Part A-IV). In the regions of overlap the total volume of the reduced sample was so small that uncertainties in operation of the apparatus produced relatively large percentage errors in the values of specific volume. As in the case of propane~ a redetermination of total volumes was made at 100 0 F. after each series of meas- urements at the seven temp,e:ratur es. In addition, the vapor pressure of each sample was determined immediately after reducing the sample size. No significant c~anges were noted in any of the check determinations. The experimental data for the single-phase regions were correlated by smoothing residual specific volume, compressibility factor, and specific volume in respect to pressure and temperature, using each function in regions where it was most suited to accurate interpolation. Smoothing with respect to temperature was often difficult to achieve. In several instances only two or three isotherms were available for a given region, and plotting against temperature was ineffective. It is believed, therefore, that the recorded values of specific volume and compressibility factor for the 33% and 69% mixtures may involve uncertainties up to 0.35% as compared with 0.3% for propane. Experimental data f~r the 17% mixture were slightly more scattered than the data for the 12. other mixtures because a small amount of water in the air chamber decreased the accuracy of the volume determinations. It appears that the probable uncertainty in the single-phase data recorded for the 17% mixture may be as great as 0.4%. For the three mixtures, values of specific volume and compressibility factor in the single-phase regions are presented at even pressures and the experimental temperatures in Tables IV, V, and VI . Figure 2 shows the effect of in- crea.sing proportion of 1-butene on the rels: tion of compressibility factor to pressure. It is believed that information concerning twophase specific volumes my be of assistance in correlating data for the complete propene-l~butene system. Isothermal curves relating compressibility factor to pressure were the most satisfactory for treating the two-phase data. It seemed inadvisable to attempt interpolation at 40 0 F. for any of the three mixtures because of the great rate of change of oompressibili ty factor with. pressure. • Since the two-phase data could not be smoothed with respect to temperature, uncertainties in them are higher than, for example, in those for the condensed liquid region. Additional uncertainty is introduced by the fact that equilibrium is evidently not always attained in the time allowed, particularly when the large sample is about 5o% vaporized. Considering the factors just mentioned, it appears that the recorded values of two-phase specific volume may involve uncertainties up to 0.5%. Tables VII, VIII, and IX present two-phase specific volumes and compressibility factors 13. at small p:ressure intervals for two-phase temperatures above 70° F. Sufficient values have been recorded to permit ac- curate graphical interpolation. All experimentally determined bubble-point and dew-point pressures and specific volumes have been included. As an application of the information obtained in this investigation, Figure 3 shows the deviation of the actual vapor pressures of mixtures from Raoult's law predictions at 160° F. In this case~" is defined by equation 1 (Part A), but P" is defined by the relation: r p r tt : Xp n f Xp " 1 1 2 2 (3) The percentage deviation of actual specific volumes from those calculated on the basis of ideal solutions is presented in Figure 4. equation: For this figure the ordinate is defined by the V Percent Deviation : • Idea/ -V {lOQ) (4) VIde<ll The values of Vrdeoi are gi van by a relation analogous to equation 3. It is interesting to note that the liquid mix- tures at 10~000 pounds per square inch are more nearly ideal solutions than are the gaseous mixtures at 100 pounds per square inch. 14. NOMENCLATURE 0 b - specific gas constant, R/M, (lb./sq.in.) (cu.ft./lb.)/ R Propane Mixture containing 17% 1-Butene Mixture containing 33% 1-Butene Mixture containing 69% 1-Butene b = 0.25504 b : 0.24133 b 0.22966 b: 0.20732 = P : pressure, lb./sq.in.abs. P" = residual vapor pressure, lb./sq.in. ~ vapor pressure of pure component 1 at a given temperature, lb./sq.in.abs. P" = :reference vapor pressure, lb./sq.in.abs. r T absolute temperature, 0 R.: = V : specific volume, cu.ft./lb. ;L : residual volume, (bT/P) - V, cu.ft./lb. x1 = mole fraction of co:tr!Ponent 1 z , : compressibility factor, PV/bT 15. REFERENCES (1) Batueoas, J. chim.phys., 31, 165 (1934). (2) Gilliland and Soheeline, Ind. Eng. Chem., 32, 48 (1940). (3) Powell and Giaque, J. Am. Chem. Soc., 61, 2366 (1939). (4) Roper, J. Phys. Chem., 44, 835 (1940). (5) Sage and Lacey, Trans. Am. Inst. Mining Met. Engrs., 136, 136 (1940). (6) Seibert and Burrell, J. Am. Chem. Soc., 37, 2683 (1915). (7) Vaughan and Graves, Ind. Eng. Chem., 32, 1252 (1940). (8) Winkler and Maass, Can. J. Research,~' 610 (1933). (9) Olds, Sage, and Lacey, Ind. Eng. Chem., 38, 301 (1946). 16. r, 6 -<> VAUGHAN AND GRAVES SEIBERT AND BURRELL 9 GILLILAND 0 AND 9 9 SCHEELINE AUTHORS Z 20 0 Ill ) 9 CD ..J I... -0- "'a:::> Ill Ill ~ - 5 CL 9 a: 0 CL < > ..J < ::> 0 Ill 0 J. 0--a-- -- - -<> ~ ~ - ~' ~ -0- -<>- "'a: 6 100 150 125 TEMPERATURE 0 175 F" Comparison of Values of Residual Vapor ressure of ropene 200 0 0 s A ~ CZ> m co ..... r--4 ..... .0 ..... ~ ~ 0.2 0.4 co 0.6 Ix( C) ~ 0 ~ t-::1 I o.aj 400 200 Figure 2. I I I 800 \II I I 1000 1200 ~ Pressure Pounds Per Sq. In. 600 I System at 280° F. I 1400 Compressibility Factor for the Propene-1-Butene I I ">-2' , ~~ , 1-Butene 69 Mole Pct. l•Butene 33 Mole Pct. 1-Butene 17 Mole Pot. 1-Butene V. I Propane I I I. II. III. IV. I I -::J • ..... ~l l1i 0 § rd t1l l1i Cl) fi a) 04 • H • A 4 8 12 16 20 I I 20 Figuxe 3. 10 / V I V 30 ~ 40 60 50 Mole Per Cent 1-Butene ~ ~ 70 "a ~ 80 "' \ 90 \ · Deviation of Bubble-Point Pressure from Raoult's Law for Propene-1-Butene Mixtures at 160° F. / ~ \ • t-' co Cl) • s::l :=I ,-1 'O '1-1 Cl) J-4 0 Cl) s::l .µ CD 0 t> s Art ..-t Q] H ~ 0 a, ..-1 CD s::l ,-1 0(1) 'H 0 Cl) p..µ 0 <D 'M or-I C) 'H 0 or-I l> 0 ,-1 § 1-------+-----+----+-------t------t,----------+------+-------+-----+------t l I / 20 30 I 50 60 Mole Per Cent 1-Butene 40 Liquid Phase At 10~000 Lb. Per Sq. In. 100 Lb. Per Sq. In. Gas Phase 70 80 90 Percentage Deviation of Aotual Specific Volume From Ideal Solution for Propene-1-Butene Mixtures at 160° F. I :.>-c:::: Figure 4. 10 Y 2 --------...,,,..cc----- 3----~-----t-----tc------+-----+-----+---+-----+--~..------t-----t 4 Liquid Phase At 600 Lb. Per Sq. In. 5 l------+--------+-----+----d-....-::::::======1===:::::::.....-=:-+------+---+----+---~ • ~ t-' 20. TABLE I. VOLffil,[]IpRIC BEHAVIOR OF PR0PENE Pressure lb./sq.in. abs. 40° F. V z (97.5)* Bubble Point 0.02969 Dew Point l.1227 70° F. 100 z V 0 F. z V (152.l) (227.3) 0.02271 0.8589 0.03121 0.7207 0~03614 0.8114 0.03318 0.4718 0.05284 0.7513 14.7 20 30 40 a.516 6.215 4.089 3.025 1.000 o.9a21 0.9754 0.9626 0.9494 9.053 6.615 4.362 3.235 1.000 0.9848 o.9793 0.9686 0.9578 9.689 7.013 4.633 3.443 1.000 0.9873 0.9826 0.9738 o.9649 50 60 80 100 125 2.3848 1.9568 1.4178 0.02968 0.02966 0.9357 0.9213 0.8900 0.0233 0.0291 2.5578 2.1061 1.5399 1.1982 0.9220 o.9467 0.9354 • 0~9119 0.8870 0.8532 2.7287 2.2522 1.6556 1.2966' 1.0080 0.9558 0.9467 0.9279 0.9084 0.0927 150 200 300 400 500 0.02965 0.02960 0.02952 0.02944 0.02936 0.0349 0.0465 0.0695 0.0924 0.1152 0.7344 0.03115 0.03102 0.03090 0.03078 0.8155 0.0461 0,0689 0.0915 0.1139 0.8160 o.5657 0.03303 0.03284 0.03265 o.8575 0.7926 0.0694 0,0921 0.1144 600 800 1000 1250 1500 0.02928 0.02914 0.02900 0.02882 0.02866 0.1379 0.1829 0.2276 0.2827 0.3373 0.03057 0.03046 0.03026 0.03001 0.02980 0.1362 0~1804 0.2240 0~2777 0.3309 0.03248 0.03216 0.03186 0.03153 0,03122 0.1365 0.1802 0.2232 0.2761 0.3281 1750 2000 2250 2500 2750 0.02850 0.02836 0.02822 0.02809 0.02796 0.3914 0.4451 0.4982 o.5510 0.6033 0.02961 0.02943 0.02927 0.02912 0.02897 0.3836 0.4357 0,4875 o.5389 0.5897 0.03094 0.03069 0.03047 ·0.03026 .0 ~03007 0.3793 0.4300 0.4803 o.5300 o.5793 3000 3500 4000 4500 5000 0.02784 0.02762 0.02742 0.02724 0.02707 0.6554 0.7586 0.8606 0.9619 1.0621 0.02883 0.02856 o.02a32 0.02810 0.02790 0.6402 0.7400 0.8386 0.9360 1.0326 0.02990 0.02959 0.02931 0.02906 0.02885 0.6284 0.7256 0.8214 o.9.1 $1 1.0106 6000 7000 8000 9000 10000 • 0.02677 0.02652 0.02630 0.02610 0.0259-1 1.2604 1.4567 1.6510 1.8432 2.0331 0.02755 1.2236 0.02725 1.4120 0.0269,6 l.5966 0.02670 " l.7788 0.02645 1~9580 0.02840 0,02801 0.02766 0.02734 0.02701 1.1938 1.3736 1.5502 1.7238 1.8923 0 * Figures in parentheses represent vapor pressures in pounds per square inoh absolute. 21. (Cont•d.) TABLE I. Pressure lb./sq.in. abs. . 0 130° F. V 16,0 z (327.l) Bubble Point 0.03572 0.07769 Dew Point 0.3109 0.6762 V F. 180 z (456.6) 0.03983 0.11507 0.2002 0.5782 0 14.7 20 30 40 10.12.5 7.411 4.904 3.650 1.000 0.9894 0.9855 o.9782 0.9707 10.657 7.805 50 60 80 100 125 2.8971 2.3952 1.7671 1.3895 1 .• 0865 150 200 300 400 500 V 0 F. z (562.0) 0.04501 0.15505 0.1404 0.4836 3.853 1.000 o.9909 0.9876 0.9813 0.9750 11.010 8.066 5.347 3.987 1.000 0.9918 0,.9888 0,.9831 0.9774 0.9632 0.9556 0.9400 0.9239 0.9031 3.062 2,.5344 1.8748 1.4786 1.1611 0.9686 0.9621 0.9490 0,.9355 0.9183 3.171 2.6265 1.9459 1.5373 1,2099 0.9717 0.9659 0.9542 0.9423 0.9270 0.8837 0.6276 0.3598 0~03653 0,.03521 0.88.1 4 0,.8346 0.7177 0.0945 0.1171 0~9489 006823 0.4103 0~26393 0,.03950 0.9005 0,.8633 0.7789 0,.6680 0.1250 0.9912 0.7166 0.4382 0.29327 0.19750 0.9113 0.8784 0.8058 0.7190 0.6053 600 800 1000 1250 1500 0,.03491 0.03437 0.03391 0.03337 0.03291 0.1393 0.1828 0.2255 0.2774 0,.3283 0.03863 · 0.03740 0,.03650 0,.03562 0,.03492 0.1467 0.1893 0.2309 0:2017 0.3314 0.04365 0,.04053 0.03896 0.03755 o.03655 0.1605 0.1987 0.2388 0.2877 0.3360 1750 2000 2250 2500 2750 0.03251 0.03216 0.03185 0.03157 0,.03132 0.3783 0,.4277 0,.4765 o.5248 o.5727 0.03435 0 ~03384 0.3803 0,.4282 0.03347· 0.4765 0.03310 0.5236 0.03276 0.5700 0.03579 0,.03520 0.03470 0.03428 0.03386 0.3839 0.4315 0,.4786 0.5253 0.5707 3000 3500 4000 4500 5000 0.03108 0.03067 0.03031 0.03000 0.02971 0.6200 0,.7138 0.8062 0.8977 0.9878 0,.03245 0,.03190 0.03143 0.03102 0.03066 o.6159 0.7064 o.7954 o.aa32 0.9700 0.03350 0.03288 0.03234 0.03186 0.03145 0.6160 0.7054 0.7929 0.8788 0.9638 6000 7000 8000 9000 10000 0.02922 0.02878 0.02836 0.02799 0.02763 l.1658 1.3396 1.5086 1.6750 1.8372 0.03006 0.02954 0.02909 0.02869 0.02830 1.1412 1,.3083 1.4725 1.6337 1.7906 0.03076 0.03012 0.02960 0.02914 0.02873 1.1312 1.2923 1 ~4514 1.6075 1.7610 5.170- 22. (Cont'd.) TABLE I. Pressure lb./sq.in. abs. 190° F. V (622.1) Bubble Point 0.05000 Dew Point 0.1088 220 z V 0 F. 280 z V 0 F. z 0.18772 0~4083 0 14.7 20 30 40 11.187 8.197 5.435 4.054 1.000 0.9922 0.9894 0.9840 0.9786 11.716 8.588 5.698 4.254 1.000 0.9933 0.9908 0.9862 0.9815 12.772 9.367 6.223 4.651 1.000 0.9949 0.9931 0.9896 0.9861 50 60 80 100 125 3.225 2.6722 1.9811 1.5661 1.2336 0.9731 0.9676 0.9565 o .• 9451 0.9306 3.387 2.8085 2.0857 1.6518 1.3044 0.9768 0~9721 0.9625 0.9529 0.9406 3.707 3.078 2.2919 1.8201 1.4424 0.9826 0.9790 0.9719 0.9648 0.9557 150 200 300 400 500 1.0117 0.7331 0.4512 0.3059 0.21280 0.9158 0.8849 o.81'10 0.6421 l.0'726 0.7820 0.4894 0~3406 0.24870 0.9281 o.s022 0.8470 O'o7859 0.7173 1.1905 0.8753 0.5591 0.4001 o ·. 3040 0.9466 0.9279 0.8892 0.8484 0.8057 600 800 1000 1250 1500 0.13376 0.04287 0.04050 0.03870 0,03750 0.4844 0.2070 0.2444 0.2919 0.3395 0.18375 0.08018 0.04876 0.04356 0.04127 0.6360 0.2775 0.2813 0-.3141 0.3571 0.23924 0.15665 0.10527 0.06927 o .• 05351 0.7609 0.6643 o.5580 0·. 4590 0.4255 1750 2000 2250 2500 2750 0.03661 0.03595 0.03535 o.03486 0.03441 0.3867 0.4339 0.4800 o.5260 o.5711 0.03973 0.03856 o .• 03765 0.03691 0.03628 0.4011 0~4449 0.4887 o.5323 o.5755 0.04962 0.04612 o.043a2 0.04225 0.04098 0.4603 0.4890 0.5226 o.5599 0.5974 3000 3500 4000 4500 5000 0.03401 0.03331 0.03271 0.03220 0.03175 0.6158 0.7036 0.7896 0.8745 0.9581 0.03573 0.03480 o.o340"f 0.03342 0.03288 0.6183 0.1026 0.'7862 0.8676 0.9484 0.03992 0.03835 0.03714 0.03618 0.03537 0.6348 0.7115 0.7875 0.8630 0.9375 6000 7000 8000 9000 10000 0.03100 0.03036 0.02982 0.02934 0.02895 1.1225 1.2826 1.439'7 1.5936 1.7471 0.03196 0.03125 0.03166 0.03014 0.02963 1.1062 1.2619 1.4149 1.5648 1 .• 7093 0.03409 0.03311 0.03231 0.03165 0.03105 1.0842 1.2286 1.3702 1.5099 1.6459 0.7383 23. TABLE I (Cont'd.) Pressul.'e lb ./sq.in. abs. 340 V 0 F. 400 z V 0 14.7 20 30 40 · 13.825 10.144 6.745 5.045 1.000 0.9961 0.9947 0.9921 0.9895 50 60 80 100 125 4.025 3.345 2.4955 1.9854 1 .• 5774 0.9868 0~9841 0.9788 0.9734 0.9667 4.340 150 200 300 400 500 1.3052 0.9649 0.6240 0.4528 0.3495 600 800 1000 1250 1500 0 F. 460° F. z V z 1.000 0.9970 0.9959 0.9939 0.9918 15.923 11.690 7.781 5.826 1.000 0.9976 0.9968 0.9952 0.9936 2.6959 2.1476 l.'7090 0.9898 0.9877 0.9836 0.9795 0.9743 4.654 3.872 2.8944 2.3080 1.8389 0.9920 0.9904 0.9872 0.9840 0.9800 0.9599 0ff9462 0.9178 0.8880 0.8568 1.4166 1.0511 0.6851 0.5019 0~3917 0.9691 0.9588 0.9373 0.9155 0.8933 1.5261 1.1351 0.7440 0.5480 0.4304 0.9760 0.9679 o.9515 0.9345 0.9175 0.28048 0.19504· 0.14387 0.10365 0.08009 0.8251 0.7650 0.7054 0.6352 o.5890 0.3183 - 0.22702 0.17278 0.130~1 0.10276 0.8710 0.8283 0.7330 0.7423 0.7050 0.3523 0.25529 0.19734 0.15162 0.12189 0.9012 0.8707 0.8413 0.8080 0.7?-95 1750 2000 2250 2500 2750 0.06631 0.05828 0.05333 0.04993 0.04743 0.5690 0.5715 0.5883 0.6120 0.6395- 0.08497 0.6782 0.07319 · O.e676 0.06519 0.6690 0.05957 0.6792 0.05556 0.6968 0.10163 0.08758 0.07763 0.07012 0.06454 0.7582 0.7468 0.7437 0.7474 0.7567 3000 3500 4000 4500 5000 0.04551 0.04275 0.04090 0.03947 0.03827 0.6694 0.7336 0.8021 0.8708 0.9382 0.05248 0.04816 0.04532 0.04317 0.04153 0.7181 0.7688 0.8268 0.8860 0.94153 0.06028 0.7710 0.05430 . 0.8102 0.05023 0.8566 0.04732 0.9078 0.04511 0.9616 6000 7000 8000 9000 10000 0.03648 0.03514 0.03410 0.03327 0.03257 1.0732 1.2060 1.3375 1.4681 1.5969 0.03908 0.03734 0.03603 0.03497 0.03412 1.0694 1.1921 1.3146 1.4354 1.5561 0.04206 0.03980 0.03809 0.03680 0.03577 14.875 10.918 7.264 5.437 3.609 1.0759 1.1878 1.2911 1.4120 1.5250 24. TABLE II PROPERTIES OF COEXISTING LIQUID AND GAS PHASES OF PROPENE Pressure Lb./Sq. In. Abs. Temperatur,e F. V z V z 100 42.2 1.0970 0.8570 0.02982 0.0233 125 56.3 0.8787 0.8346 0.03050 0.0290 150 69.0 0.7310 0.8132 0.03117 0.0347 200 90.1 0.5417 0.7727 0.03251 0.0464 250 107.6 0.4247 0.7339 0.03376 0.0583 300 122.6 0.3446 0.6962 0.03499 0.0707 350 135.9 0.28608 0.6592 0.03636 0.0838 400 147.8 0.24092 0.6220 0.03786 0.0978 450 158.6 0.20444 0.5834 0.03956 0.1129 500 168.6 0.17380 0.5423 0.04163 0.1299 650 177.9 0.14666 0.4960 0.04417 0.1494 600 186.5 0.12066 0.4393 0.04782 0.1741 650 194.3 0.09020 0.3515 0.05562 0.2168 0.06944 0.2770 0.06944 0.2770 668 a 8 0 197.0 Critical state. 8 Dew Point Bubble Point 25. TABLE III LATENT HEAT OF VAPORIZATION OF PROPENE Temperature oF. Authors B.t.u./lb. 40 155.6 158.4 70 144.6 146.1 100 130.6 132.5 130 113.1 115.6 160 89.1 90.8 180 64.5 65.3 190 44.8 45.6 Vaughan and Graves B.t .u./lb. 26. TABLE IV SINGLE-PHASE VOLUMETRIC BEHAVIOR OF A MIXTURE OF PROPENE AND 1-BUTENE WITH 17.050 MOLE PER CENT 1-BUTENE Pressure lb ./sq.in. abs. 40 0 70 F. z 0 F. 100 0 F. V z V z 0 14.7 20 30 40 8.543 : 6.236 4.104 3.037 1.000 .9822 .9757 .9632 .9503 9.057 6.619 4.367 3.240 1.000 .9854 .9801 .9699 .9596 50 60 80 100 125 .02873 .02871 .0238 .0298 2.3957 1.9671 1.4277 1.0978 .9371 .9233 .8935 .8588 2.5638 2.1124 1.5470 1.2062 .9311 .9491 .9383 09163 .8930 .8616 150 200 300 400 500 .02869 .02865 .02857 .02850 .02842 .0357 .0475 .0711 .0945 .1178 .03010 .03006 .02997 .02988 .02980 .0353 .0470 .0703 .0935 .1166 .7442 .03184 .03170 .03156 .03142 .8264 .0471 .0704 .0935 .1163 600 800 1000 1250 1500 .02835 .02821 .02808 .02793 .02779 .1411 .1871 .2329 .2895 .3457 .02970 .02954 .02938 .02919 .02900 .1394 .1849 .2298 .2854 .3403 .03129 .03104 .03081 .03055 .03030 .1390 .1838 .2281 .2827 .3365 1750 2000 2250 2500 2750 .02765 .02752 .02740 .02729 .02718 .4013 .4564 .5112 .5658 .6198 .02tfo3 .02866 .02850 .02835 .02821 .3947 .4484 .5016 .5544 .6069 .03007 .02985 .02965 .02945 .02928 .3896 .4420 .4939 .5451 .5961 3000 3500 4000 4500 5000 .02708 .02688 .02645 .02651 .02635 .6734 .7802 .8774 .9893 1.0925 .02807 .02783 .02761 .02740 .02720 .6588 .7620 .8640 .9646 1.0639 .02911 .6466 .02880 .7463 .8449 .02853 .02827.9418 .02803 1.0376 6000 7000 8000 9000 10000 .02605 .02579 .02554 .02530 .02507 1.2961 1~4971 1.6943 1.8882 2.0789 1.2603 1.4539 .02p2'l_ 1.6441 .02600 1.8306 .02575 2.0144 V - .02685 .02655 . .02763 .02730 .02698 .02666 .02636 1.2274 1.4148 1.5980 1.7764 1.9516 27. TABLE IV · (Cont'd.) Pressure lb./sq.in. abs. 160° F. 220 0 F. V z 0 14.7 20 30 40 10.067 7.368 4.875 3.629 1.000 .9893 .9854 .9780 .9705 11.071 8.111 5.377 4.010 1.000 .9919 .9889 .9834 .9778 50 60 80 100 125 2.8802 2.3812 1.7569 1.3818 1.0810 .9630 .9553 .9398 .9240 .9035 3.189 2.6424 1.9586 1.5481 1.2194 .9722 .9666 .9552 .9438 .9293 150 200 300 400 500 .8798 .6262 .3640 .03698 .03646 .8824 .8374 .7302 .0989 .1219 1.0001 .7252 .4478 .3054 .21576 .9146 .8842 .8189 .7447 .6577 600 800 1000 1250 1500 .03601 .03527 .03466 .03404 .03351 .1448 .1887 .2318 .2845 .3361 .14778 .04681 .04242 .03992 .~03844 .5406 .2283 .2586 .3042 .3515 1750 2000 2500 2750 .03306 .03267 .03232 .03201 .03172 .3869 .4369 .4863 .5351 .5833 .03743 .03658 .03588 .03530 .03480 .3993 .4460 .4922 .5380 .5834 3000 3500 4000 4500 5000 .03146 .03099 .03059 .03023 .02991 .6311 .7253 .8182 .9096 1.0000 .03435 .03357 .03293 .03236 .03187 .6282 .7163 .8030 .8878 .9715 6000 7000 8000 9000 10000 .02935 .02860 .02842 .02802 .02765 1.1775 1.3387 1.5203 1.6863 1.8489 .03106 .03042 .02986 .02936 .02893 1.1361 1.2982 1.4563 1.6109 1.7637 2250 V ... z 28. TABLE IV Pressure 250° F. lb ./sq.in. abs. (Cont'd.) 280 V z 14.7 20 30 40 11.571 8.481 5.626 4.199 1.000 .9929 .9903 .9855 .9806 50 60 80 100 125 3.342 2.7713 2.0574 ·l.6290 1.2862 150 200 300 400 500 600 0 V . 12.071 0 F. z 8.850 5.875 4.387 1.000 .9938 .9915 .9873 .9831 .9757 .9709 .9610 .9511 .9387 3.495 · 2.8994 2.1554 1.7091 1.3518 .9788 .9745 .9659 .9574 .9466 1.0574 .7713 .4839 .3386 .24944 .9261 .9006 .8476 .7908 .7282 1.1136 .8155 .5177 .3658 .27392 .9357 .9136 .9701 .8196 .7672 1000 1250 1500 .18725 .09743 .05405 .04579 .04267 .6560 .4551 .3156 .3342 .3737 .211s2 .13174 .08233 .05595 ;04339 .7120 .5906 .4612 .3918 .4066 1750 2000 2250 2500 2750 .04108 .03935 .03823 .03740 .03670 .4163 .4595 .5022 .5459 .5893 .04473 .04261 .04099 .;03973 .03882 .4385 .4774 .5166 .5565 .5980 3000 3500 4000 4500 5000 .03609 .03509 .03426 .03358 .03300 .6322 .7171 .8001 .8823 .9634 .03810 .03677 .03570 .03483 .03411 .6403 .7209 .0000 .8780 .9554 6000 7000 8000 9000 10000 .03200 .03123 .03061 .03009 .02960 1.1210 1.2764 1.4298 1.5812 1.7283 .03298 .03209 .03138 .03077 .03025 1.1085 1.2584 1.4063 1.5513 1.6946 800 290 TABLE V SINGLE-PHASE VOLUMETRIC BEHAVIOR OF A MIXTURE OF PROPENE AND 1-BUTENE WITH 33.153 MOLE PER CENT 1-BUTEN'E Pressure lb./sq.in. abs. 40° F. V 70 z 100° F. F. z V - 0 14.7 20 30 40 50 60 80 100 125 V 0 .... .. .02813 - -- z 8.619 6.299 4.155 3.082 1.000 .9854 .9800 .9697 .9590 2.4371 2.0064 1.4654 1.1366 .9480 .9366 .9120 .8842 .02812 .02810 .0196 .0245 .0306 .02941 .0302 150 200 300 400 500 .02809 .02806 .02800 .02794 .02788 .0367 .0489 .0732 .0974 .1215 .02939 .02935 .02926 .02918 .02910 .0362 .0483 .0722 .0959 .1196 .03085 .03073 .03061 .03060 .0480 .0717 .0953 .1186 600 800 1000 1250 1600 .02778 .02772 .02762 .02750 .02739 .1452 -.1932 .2407 .1995 .3580 .02902 .02887 .02873 .02855 .02839 .1431 .1899 .2362 .2934 .3501 .03039 .03017 002997 .02974 .02952 .1419 .1878 .2332 .2892 .3445 1750 2000 2250 2500 2750 .02727 .02717 .02706 .02696 .02681 .4158 .4735 .5305 ~6873 .6424 .02824 .02810 .02795 .02782 .02769 .4062 .4620 .5170 .5717 .6260 .02931 .02913 .02895 .02878 .02863 .3990 .4532 .5067 .5597 .6125 3000 3500 4000 4500 5000 .02676 .02658 .02640 .02623 .02606 .6995 .8106 .9202 1.0285 1~1354 .02756 .02734 .02712 .02693 .02676 .6797 .7866 .8917 .9962 1.0999 .02847 .02820 .02795 .02774 .02753 .6645 .7679 .8698 .9711 1.0709 6000 7000 8000 9000 10000 .02580 .02555 .02530 .02~05 .02481 1.3489 1.5585 l.'1637 1.99-98 2.1619 .02644 .02614 .02581 .02561 .02537 1.3041 1.5042 1.6973 1 •.8947 2.0855 .02715 .02685 .02655 .02625 •.02595 1.2673 1.4622 1.6524 1.8379 2.0188 30. TABLE V (Cont'd.) 0 Pressure lb./sq.in. abs. V z V z 0 14.7 20 30 40 9.578 7.010 4.637 3.451 1.000 .9891 .9851 .9775 .9698 10.536 7.718 5.116 3.815 1.000 .9919 .9889 .9833 .9776 50 60 80 100 125 2.7385 2.2634 1.6688 1.3112 1.0239 .9621 .9542 .9381 .9213 .8993 3.034 2.5135 1.8623 1.4711 1.1578 .9719 . 9661 , .9544 .9424 .9271 150 200 300 400 500 .8330 .5857 .8780 .8231 .03483 .03448 .0979 .1211 .9484 .6855 .4186 .27925 .18620 .9113 .8783 .8045 .7156 .5964 600 800 1000 1250 1500 .03417 .03363 .03312 .03268 .03227 .1441 .1890 .2327 .2870 .3401 .04172 .04090 .03903 .03745 .03650 .1759 .2096 .2500 .2999 .3507 1750 2000 2250 2500 2750 .03190 .03168 .03130 .03104 .03080 .3922 .4438 .4948 .5453 .5951 .03569 .03502 .03441 .03396 .0335.2 .4001 .4487 .4960 .5439 .5905 3000 3500 4000 4500 5000 .03059 .03019 .02984 .02950 .02920 .6448 .7424 .838'7 .9328 1.0259 .03313 .• 03222 .03191 .03143 .03100 .6367 .7224 .8177 .9061 .9930 6000 7000 8000 9000 10000 .02866 .02824 .02785 .02747 .02711 1.2083 1.3890 1.5655 1.7371 1.9049 .03028 .02971 .02921 .02876 .02835 1.1639 1.3323 1.4970 1.6582 1.8161 160° F. 220 . F. 31. TABLE V (Cont'd.) Pressure 250 lb./sq.in. 0 F. 280 0 F. abs. V z V z 0 14.7 20 30 40 11.014 8.073 5.356 3.997 1.000 .9931 .9906 .9858 .9809 11.492 8.426 5.595 4.179 1.000 .9942 .9920 .9880 .9839 50 60 80 100 125 3.182 2.6381 1.9583 1.5501 1.2231 .9761 .9711 .9612 .9510 .9380 3.329 2.7622 2.0537 1.6283 1.2876 .9798 .9756 .9671 .9585 .9475 150 200 300 400 500 1.0048 .7311 .4547 .3134 .22518 .9247 .8970 .8369 .7691 .6908 1.0602 .7753 .4885 .3427 .25356 .9362 .9128 .8626 .8069 .7463 600 800 1000 1250 1500 .16105 .05629 .04529 .04157 .03957 .5929 .2763 .2779 .3188 .3642 .19233 .10896 .06172 .04835 .04403 .6793 .5131 .3633 .3558 .3888 1750 2000 2250 2500 2750 .03818 .03719 .03644 .03578 .03522 .4099 .4563 .5030 .5488 .5942 .04164 .04001 .03891 .03792 .03713 .4290 .4710 .5153 .5580 .6011 3000 3500 4000 4500 5000 .03471 .03386 .03315 .03255 .03202 .6389 .7271 .8135 .8987 .9823 .03645 .03533 .03444 .03370 .03308 .6437 .7279 .8109 .8927 .9736 6000 7000 8000 9000 10000 .03116 .03050 .02993 .02941 .02892 1.1471 1.3099 1.4690 1.€3240 1.7743 .03206 .03128 .03064 .03006 .02953 1.1323 1.2889 1.4429 1.5925 1.7383 32. TABLE VI SINGLE-PHASE VOLillv!ErRIC BEHAVIOR OF A MIXTURE OF PROPENE AND 1-BUTENE WITH 69.050 MOLE PER CENT 1-BUTENE P:ressu:re lb./sq.in. abs. 0 14.7 20 30 40 40 V 0 70 F. z ... - - - V -- 0 F. 100 z V --- -- - -.. - 0 F. z 50 60 80 100 125 .02695 .02694 .02692 .02691 .02690 .0130 .0156 .0208 .0260 .0325 .02795 .02793 .02791 .0204 .0254 .0318 .02918 .0314 150 200 300 400 500 .02688 .02685 .02678 .02672 .02666 .0389 .0518 .0775 .1032 .1287 .02790 .02786 .02780 .02774 .02767 .0381 .0507 .0780 .1010 .1260 .02915 .02910 .02900 .02891 .02882 .0377 .0502 .0750 .0997 .1242 600 800 1000 1250 1500 .02660 .02650 .02640 .02630 .02619 .1541 .2046 .2548 .3173 .3792 .02760 .02749 .02737 .02723 .02710 .1508 .2003 .2492 .3099 .3702 .02874 .02857 .02841 .02824 .02806 .1486 .1970 .2449 .3042 .3628 1750 2000 2250 2500 2750 .02610 .02601 .02594 .02586 .02579 .4409 .5021 .5634 .6240 .6846 .02697 .02685 .02674 .02664 .02653 .4298 .4890 .5479 .6064 .6643 .02790 .02775 .02761 .02749 .02737 .4208 .4783 .5354 .5923 .6487 3000 3500 4000 4500 5000 .02571 .02557 .02542 .02528 .02514 .7445 .8639 .9815 1.0981 1.2133 .02644 .02610 .02610 .02595 .02580 .7223 .8369 .9506 1.0633 1.1746 .02726 .02705 .02685 .02667 .02650 .7048 .8160 .9256 1.0343 1.1419 6000 7000 8000 9000 10000 .02488 .02465 .02445 .02426 .02410 1.4409 1.6655 1.8880 2.107-5 2.3263 .02550 .02523 .02499 .02476 .02456 1.3932 1.6082 1.8204 2.0291 2.2364 .02616 .02585 .02558 .02532 .02508 1.3528 1~5595 1.7637 1.9640 2.1615 33. TABLE VI (Cont'd..) Pressure lb ./sq.in. abs. V z V 0 14.7 20 30 40 8.611 6.292 4.151 3.079 1.000 .9850 .9796 .9692 .9588 9.484 6.941 4.592 3.417 1.000 .9891. .9852 .9777 .9701 50 60 80 100 125 2.4365 2.0076 1.4707 1.1474 .8870 .9483 .9376 .9158 .8931 .8630 2.7125 2.2424 1.6544 1.3011 1.0181 .9625 .9548 .9393 .9234 .9031 .8287 .5902 .3441 .8822 .8376 .7326 .03699 .1313 . 150 160° F. 220° F. z . 7103 200 300 400 500 .8293 .03215 .03194 .03173 .0751 .0994 .1235 600 800 1000 1250 1500 • .03154 .03120 .03092 .03065 .03033 .1473 .1943 .2407 .2982 .3541 .03640 .03544 .03421 .03400 .03340 .1550 .2012 .2428 .3016 .3555 1750 2000 2250 2500 2750 .03009 .02986 .02965 .02945 .02925 .4099 .4649 .5193 .5731 .6261 .03290 .03246 .03208 .03173 .03141 .4086 .4607 .5122 .5629 .6130 3000 3500 4000 4500 5000 .02907 .02874 .02843 .02815 .02790 .6788 .7830 .8852 .9860 1.0859 .03113 .03062 .03018 .02979 .02945 .6628 .7606 .8567 .9514 1.0450 6000 7000 8000 9000 10000 .02743 .02703 .02670 .02638 .• 02608 1.2811 1.4728 1.6626 1.8481 2.0300 .0.2886 .02835 .02793 .02753 .02715 1.2289 1.4083 1.5857 1.7584 1.9268 - 34. TABLE VI Pressure (Conttd.) 250° F. lb./sq.in. 280° F. abs. V z V z 0 14.7 20 30 40 9.917 7.262 4.810 3.583 1.000 .9906 .9872 .9807 .9742 10.349 7.582 5.025 3.747 1.000 .9918 .9888 .9831 .9775 50 60 80 100 125 2.8475 2.3568 1.7431 1.3746 1.0793 .9677 .9611 .9478 .9343 .9170 2.9804 2.4690 1.8297 1.4459 1.1385 .9718 .9660 .9545 .9429 .9280 150 200 300 400 500 .8822 .6345 .3827 .24953 .8994 .8624 .7804 • .6784 .9334 .6764 .4170 .28368 .19870 .9130 .8821 .8157 .7400 .6479 600 800 1000 1250 1500 .• 04193 .03906 .03764 .03641 .03550 .1710 .2124 .2558 .3093 .3619 .13258 .04739 .04234 .03942 .03783 .5187 .2472 .2761 .3213 .31700 1750 2000 2250 2500 2750 .03476 .03414 .03361 .03315 .03273 .4134 .4641 .5140 .5633 .6118 .03687 .03606 .03533 .03470 .03417 .4208 .4703 .5183 .5657 .6128 3000 3500 4000 4500 5000 .03236 .03173 .03119 .03072 .03031 .6598 .7548 .8480 .9396 1.0300 .03371 .03293 .03229 .03174 .03126 .6595 .7516 .8423 09314 1.0192 6000 7000 8000 9000 10000 .02963 .02905 ~02856 .02813 .02775 1.2083 1.3821 1.5529 1.7207 1.8861 .03045 .02980 .02924 .02873 .02828 1.1914 1.3603 1.5254 1.6861 1.8441 • TABLE VII TWO-PHASE VOLUMETRIC DATA FOR A MIXTURE OF PROPENE AND 1-BUTENE WITH 17.050 MOLE PER CENT 1-BUTENE Pressure lb./sq.in. abs. 82.8 8 40 0 70° F. F. V z .02874 .0197 Pressure lb./sq.in. abs. a 130.6b 103.6 105 108' 111 114 117 120 122 124 126 128 129 100° F. Pressure lb./sq.in. abs. z .03013 1.0511 .0308 .8518 1.0057 . 9089 ' .8106 .7109 .6092 .5031 .4258 .3429 .25383 .15539 .10207 .8261 .7679 .7039 .6340 .5576 .4723 .4064 .3326 .2502 .1556 .1030 160° F. V z Pressure lb./sq.in. abs. 195.~ 161.4 .03185 .6767 .0461 .8086 165 168 171 174 177 180 183 186 188 190 192 194 .6164 .5671 .5177 .4673 .4161 .3629 .3058 .24501 .20189 .15768 .10974 .05953 .7530 .7053 .6554 .6020 .5452 .4836 .4143 .3374 .2810 .2218 .1560 .0855 a - Bubble point V V z 389.7b 346.9 .03705 .2864 .0965 .6643 350 355 360 365 370 375 380 385 .27398 .25183 .22653 .19773 .16693 .13460 .10106 .06736 .6412 .5978 .5453 .4826 .4130 .3375 .2568 .1734 a b- Dew point 36. TABLE VIII TWO-PHASE VOLlJii.[ETRIC DATA FOR A MIXTURE OF PROPENE AND 1-BUTENE WITH 33.153 MOLE PER CENT 1-BUTENE Pressure lb./sq.in. abs. 70.5 a 40 0 70° F. F. V z .02814 .0173 Pressure lb./sq.in. abs. a 111.3 82 85 88 91 94 97 100 103 105 107 109 100° F. Pressure lb./sq.in. abs. V z 166.9b 124.7 .03090 .8694 .0401 .8434 128 131 134 .7875 .7183 .6521 .5892 .5289 .4707 .7842 8 137 140 143 146 149 152 155 158 161 164 .4132 .3572 .3021 .24630 .19183 .13748 .08386 Pressure lb./sq.in. abs. a 334.3b 277.6 280 285 290 .7320 .6798 .6280 295 .5761 .5237 .4693 .• 4140 300 305 310 315 ,.3572 .2~70, ~2358 .1722 320 325 330 .1070 a - Bubble point. b - Dew point V z .02942 .0269 1.1711 .9313 .9010 .7780 .6624 .5509 .4416 .7894 .7206 .6518 .5820 .5118 04393 .3630 .3334 .26137 .18839 .11406 160 0 .2823 .2256 .1657 .1022 F. V z .03509 .14881 .0824 .5183 .3517 .3206 .29043 .26052 .23080 .20153 .6920 •.6420 .5918 .5400 .4865 .4319 .3758 ;3179 .17253 .14359 .11448 .08122 .05714 .2574 ~1946 .1325 37. TABLE VIII (Cont'd.) Pressure lb./sq.in. abs. 220 0 F. V z 594.5b 543.7 .04192 .14881 .1751 .5183 550 555 560 565 570 575 580 585 590 .13544 .12488 .11443 .10432 .09434 .08465 .07495 .06532 .05548 .4772 .4440 .4105 .3776 .3445 .3118 .2785 .2448 .2097 a a - Bubble point b - Dew point 38. TABLE IX TWO-PHASE VOLUMETRIC DATA FOR A :MIXTURE OF PROPENE AND 1-BUTENE WITH 69.050 MOLE PER CENT 1-BurrENE 40 Pl'essuxe lb ./sq.in. abs. 43.6 8 0 F. V z Pressure lb./sq.in. abs. .02695 .0113 70.9 8 53 55 57 59 61 63 65 67 69 0 Pressure lb ./sq.in. abs. 100 F. V z Pressure lb./sq.in. abs. 108.4b .02920 1.2501 .0273 .8705 83 85 87 89 91 93 95 l .0657 .7623 ,. 6724 .5918 .5182 .4517 .3906 .3355 .2841 .2358 .1884 .1422 .0978 .0560 a so.a 97 99 101 103 105 10'7 70 0 F. V z .02795 .0180 l.4034 1.1337 .9131 .7250 .5676 .4318 .3114 .20456 .10823 .6773 .5678 .4739 .3895 .3153 .2477 .1843 .1248 .0680 160 0 F. V z 224.9b 184.1 .03233 .5369 .0566 .7694 186 188 190 193 196 200 204 208 212 216 220 .5055 .4702 .4321 .3786 .3316 .27576 .22621 .18202 .14204 .10516 .07107 .7318 .6880 .6390 .5687 .5057 .4293 .3592 .2947 .2344 .1768 .1217 a .9179 .7893 .6756 .5759 .4873 .4098 .3398 • 27636· .21644 .16019 .10807 .06073 a - Bubble point b - Dew point 39. TABLE IX 0 Pressure lb./sq.in. abs. a 413.lb 365.4 370 375 380 385 390 395 400 405 410 220 F. (Cont'd.) V z Pressure lb./sq.in. abs. .03777 .24583 .1107· .6375 .21852 .19081 .16527 .14131 .11959 .09924 .08067 .06322 .04726 .5738 .• 5078 .4457 .3861 .3310 .2782 .2290 .1817 .1375 a - Bubble point b - Dew point 250 0 F. V z 540.8b 497.7 .04356 .15602 .1601 .5278 500 605 510 515 520 525 530 535 540 .14884 .13387 .11889 .10436 .09099 .07839 .06674 .05569 .04496 .5058 .4595 .4121 .3653 .3216 .2797 .2404 .2025 01650 a