1、Designation: D2889 95 (Reapproved 2015)Standard Test Method forCalculation of True Vapor Pressures of Petroleum DistillateFuels1This standard is issued under the fixed designation D2889; the number immediately following the designation indicates the year oforiginal adoption or, in the case of revisi
2、on, the year of last revision. A number in parentheses indicates the year of last reapproval. Asuperscript epsilon () indicates an editorial change since the last revision or reapproval.1. Scope1.1 This test method describes the calculation of true vaporpressures of petroleum distillate fuels for wh
3、ich distillationdata may be obtained in accordance with Test Method D86without reaching a decomposition point prior to obtaining 90volume % distilled.1.2 The test method may be used to calculate vapor pres-sures at temperatures between the 0 % equilibrium flashtemperature and the critical temperatur
4、e of the fuel. Provisionis included for obtaining a calculated critical temperature forfuels for which it is not known.1.3 Critical pressure-temperature data are usually not avail-able for petroleum fuels. However, if both the critical pressureand critical temperature are known, the values shall be
5、used asthe coordinates in Fig. 1 to establish a critical point to be usedinstead of the focal point established as described in 6.5.4; andthe calculations described in 6.5 through 6.5.4 are not required.If either a determined true boiling point or determined equi-librium flash vaporization temperatu
6、re at 0 % distilled atatmospheric pressure is known, the determined value shall beused to establish the lower limit of the bubble-point linereferred to in 6.4.1.4 The method is not reliable for distillate fuels having aboiling range of less than 100 F (38 C) between the TestMethod D86 10 volume % an
7、d 90 volume % distilled tem-peratures.1.5 The values stated in inch-pound units are to be regardedas standard. The values given in parentheses are mathematicalconversions to SI units that are provided for information onlyand are not considered standard.1.6 This standard does not purport to address a
8、ll of thesafety concerns, if any, associated with its use. It is theresponsibility of the user of this standard to establish appro-priate safety and health practices and determine the applica-bility of regulatory limitations prior to use.2. Referenced Documents2.1 ASTM Standards:2D86 Test Method for
9、 Distillation of Petroleum Products atAtmospheric PressureD287 Test Method for API Gravity of Crude Petroleum andPetroleum Products (Hydrometer Method)2.2 ASTM Adjuncts:Temperature Pressure Conversion Chart (16 by 20 in. draw-ings)33. Summary of Test Method3.1 Equilibrium flash vaporization (EFV) te
10、mperatures arecalculated from distillation data (Test Method D86) determinedon the sample. The distillation data, calculated EFV data, andAPI gravity of the sample are used with a graphical correlationprocedure to obtain two pairs of temperature-pressure coordi-nates through which the bubble-point l
11、ine of the phase diagramfor the sample may be drawn. The calculated true vaporpressure at a specified temperature is obtained by reading thepressure at the intersection of the bubble-point line andspecified temperature.NOTE 1Details of the procedure and data substantiating its validity forestablishi
12、ng equilibrium flash vaporization temperatures have been pub-lished.44. Significance and Use4.1 The true vapor pressure of a distillate fuel is a relativemeasurement, both of the tendency of the most volatile portionof the fuel to gasify, and of the restraining pressure required toprevent gasificati
13、on of the most volatile portion. Thus themeasurement is of importance when a fuel is to be utilized inapplications where no gasification may be tolerated, and1This test method is under jurisdiction of ASTM Committee D02 on PetroleumProducts, Liquid Fuels, and Lubricants and is the direct responsibil
14、ity of Subcom-mittee D02.04.0K on Correlative Methods.Current edition approved Oct. 1, 2015. Published December 2015. Originallyapproved in 1970. Last previous edition approved in 2010 as D2889 95 (2010).DOI: 10.1520/D2889-95R15.2For referenced ASTM standards, visit the ASTM website, www.astm.org, o
15、rcontact ASTM Customer Service at serviceastm.org. For Annual Book of ASTMStandards volume information, refer to the standards Document Summary page onthe ASTM website.3Available from ASTM International Headquarters. Order Adjunct No.ADJD2889. Original adjunct produced in 1987.4Edmister, W. C., and
16、Okamoto, K. K., “Applied HydrocarbonThermodynamics, Part 12: Equilibrium Flash Vaporization Correlations for Petro-leum Fractions,” Petroleum Refiner, PEREA, Vol 38, No. 8, 1959, p. 117.Copyright ASTM International, 100 Barr Harbor Drive, PO Box C700, West Conshohocken, PA 19428-2959. United States1
17、temperature-pressure conditions are expected to be near thetrue vapor pressure of the fuel.5. Data Requirements5.1 Distillation temperatures at the initial boiling point(IBP) and 10 volume %, 30 volume %, 50 volume %, 70volume %, and 90 volume % distilled obtained in accordancewith Test Method D86.5
18、.2 API gravity determined in accordance with Test MethodD287, or a method of equivalent accuracy.6. Procedure6.1 Calculate the 10/70 slope, F/%, of theTest Method D86distillation using the 10volume % and 70 volume % distilledtemperature. Using this slope and the Test Method D86 50volume % distilled
19、temperature, obtain to the nearest 61Fatemperature difference, F, from Fig. 2. Add F to the MethodD86 50 volume % temperature to obtain the equilibrium flashvaporization (EFV) 50 volume % temperature.6.2 Calculate the differences between the Test Method D86IBPand 10 volume %, the 10 volume % and 30
20、volume %, andthe 30 volume % and 50 volume % temperatures. Using thesedifferences, obtain to the nearest 1 F, the temperature differ-ences between corresponding EFV percentages from Fig. 3.6.3 Calculate the EFV zero volume percent temperature bysubtracting the sum of the three differences obtained f
21、rom Fig.3, from the EFV 50 volume % temperature calculated inaccordance with 6.1.6.4 Plot a point on Fig. 13,5at the coordinates, 14.7 psia andthe calculated EFV 0 % temperature. This point establishes thelower end of the phase boundary line commonly referred to asthe bubble-point line. If the EFV 0
22、 % temperature at atmo-spheric pressure has been measured, use the measured valueinstead of the calculated value.6.5 Use the following procedure and the curves on the rightportion of Fig. 1 to obtain coordinates for the upper end, orfocal point, of the bubble-point line. If both the criticaltemperat
23、ure and critical pressure of the fuel are known, thecalculations described in 6.5.1 through 6.5.4 are not carriedout. The critical temperature and critical pressure are used as5Precision of the test method as given in Section 6 was obtained using 812 by11in. charts and should be improved using the 1
24、6 by 20in. charts.FIG. 1 Test Method D86 Distillation Temperature and Equalization Flash Vaporization Temperature Pressure Conversion ChartD2889 95 (2015)2the coordinates in Fig. 1 to define a critical point to be usedinstead of the focal point.6.5.1 Calculate to the nearest 0.1 unit the 10/90 slope
25、 of theTest Method D86 distillation curve, F/volume %, as thedifference between 10 volume % and 90 volume % distilledtemperatures divided by 80.6.5.2 Calculate to the nearest 1 F, the volumetric averageboiling point (VABP) as the sum of the Test Method D86 10volume %, 30 volume %, 50 volume %, 70 vo
26、lume %, and 90volume % distilled temperatures divided by 5.6.5.3 Calculate to the nearest 0.1 unit the ratio:VABP/10/90 Slope116.0! (1)6.5.4 Enter Fig. 1 on the lower right scale at theTest MethodD86 VABP temperature. From the intersection of the VABPtemperature and the line of constantAPI gravity c
27、orrespondingto the gravity of the sample, proceed horizontally to the pointof intersection with the line corresponding to the 10/90 slope ofthe Test Method D86 distillation. From this point proceedvertically to the intersection with the ratio calculated for thesample according to the previous sectio
28、n. This point ofintersection establishes the upper end, or focal point of thebubble-point line.6.6 Draw the bubble-point line on Fig. 1 by connecting thetwo points (6.4 and 6.5.4) with a straight line.6.7 Obtain the calculated true vapor pressure psia, at anyspecified temperature below the critical
29、temperature by readingthe vertical pressure scale of Fig. 1 at the intersection of thebubble-point line with the specified temperature.6.7.1 If either a determined critical temperature or deter-mined critical pressure is known, the point of its intersectionwith the bubble-point line defines the maxi
30、mum vapor pressureto be reported.6.7.2 If neither the critical temperature nor critical pressureis known, obtain a calculated approximate critical temperaturefrom Fig. 4.6The point of intersection of the calculated criticaltemperature with the bubble-point line defines the maximumvapor pressure to b
31、e reported.7. Report7.1 Report the results as indicated in the following tabula-tion:Vapor Pressure Range, psia: Report to the Nearest:100 and below 1100 to 200 2200 to 500 5Above 500 107.2 The calculated true vapor pressure psia may be con-verted to the International System of Units (SI) of kilopas
32、cals(kPa) by multiplying the results obtained in 7.1 by theconversion factor 6.894757 and then rounding to the appropri-ate number of significant digits.8. Precision and Bias8.1 PrecisionThe precision of this test method as deter-mined by statistical examination of interlaboratory results is asfollo
33、ws:8.1.1 RepeatabilityThe difference between successive testresults, obtained by the same operator with the same apparatusunder constant operating conditions on identical test material,would, in the long run, in the normal and correct operation ofthe test method, exceed the following value only in o
34、ne case intwenty: the larger of 2 psia (14 kPa) or 4 % of the mean of thetwo results.8.1.2 ReproducibilityThe difference between two, singleand independent results, obtained by different operators work-ing in different laboratories on identical test material, would, inthe normal and correct operatio
35、n of the test method, exceed thefollowing value only 1 case in 20: the larger of 2 psia (14 kPa)or 8 % of the mean of the two results.NOTE 2The preceding repeatability and reproducibility were obtainedfrom results submitted by seven laboratories that cooperatively tested fourturbine fuels with initi
36、al boiling points in the range 320 F to 400 F(160 C to 204 C), and end points in the range 430 F to 534 F (221 Cto 279 C). Each laboratory determined the required distillation andgravity data in duplicate, and performed the calculations required for thisprocedure once for each of the two sets of det
37、ermined data for eachsample. Vapor pressures were not determined during the cooperativeprogram.8.2 BiasThe bias of the true vapor pressures obtained bythis test method has not been evaluated. Determined true vaporpressures were not known for the fuels cooperatively tested.6Technical Data Book-Petrol
38、eum Refining, American Petroleum Institute, 2101L St. NW, Washington, DC 20037. Fig. 4 is a modified version of Fig. 4 A1.2,Chapter 4.FIG. 2 Test Method D86 50 % Distilled Temperature versus Equi-librium Flash Vaporization 50 % TemperatureD2889 95 (2015)39. Keywords9.1 API gravity; D86 distillation;
39、 true vapor pressureFIG. 3 Test Method D86 Distillation Temperature Differences Ver-sus Equilibrium Flash Vaporization Temperature DifferencesFIG. 4 Critical Temperature, Gravity, and Test Method D86 Volu-metric Average Boiling Point FD2889 95 (2015)4APPENDIX(Nonmandatory Information)X1. EXAMPLE OF
40、TRUE VAPOR PRESSURE CALCULATIONX1.1 Calculate the true vapor pressure at 400 F, for a fuelfor which the following data have been determined:API gravityMethod D86 distillation, F(IBP)-IP 12340.00 % 27510 % 34530 % 40450 % 43670 % 46590 % 505X1.1.1 From Fig. 2, using the 10/70 slope of 2.0 % and the50
41、 % distillation temperature, a value of 6 is obtained as theincrement to add to the 50 % distillation temperature to obtainthe EFV 50 % temperature. Thus the calculated 50 % tempera-ture is 436 6, or 430 F.X1.1.2 From Fig. 3, usingASTM temperature differences of70 for 0 % to 10 %, 59 for 10 % to 30
42、%, and 32 for 30 % to50 %, EFV temperature differences of 34, 37, and 17,respectively, were obtained and their sum determined to be 88.Thus the calculated EFV 0 % temperature is 430 88, or342 F. The coordinates for the lower end of the bubble-pointline are 342 F and 14.7 psia (distillation pressure)
43、, as plottedon Fig. 1.X1.1.3 The slope of the Test Method D86 distillation curvefrom 10 % to 90 % is equal to (505 345)80, or 2.0 F%.X1.1.4 The volumetric average boiling point is equal to(345 + 404 + 436 + 465 + 505)5, or 431 F.X1.1.5 The ratio, VABP/(10/90 Slope + 16.0) is 431/(2.0 + 16.0), or 23.
44、9.X1.1.6 The results of the calculations, X1.1.1 to X1.1.5 areshown in Fig. 1. The first datum entered in Fig. 1 was theVABP, 431 F, on the lower right scale, and other data wereused as required and indicated by the heavy broken line toestablish the focal point. The bubble-point line then was drawnb
45、y connecting the focal point and the point obtained asexplained in X1.1.2.X1.1.7 The calculated true vapor pressure at 400 F, as readfrom the bubble-point line is 27 psia.ASTM International takes no position respecting the validity of any patent rights asserted in connection with any item mentionedi
46、n this standard. Users of this standard are expressly advised that determination of the validity of any such patent rights, and the riskof infringement of such rights, are entirely their own responsibility.This standard is subject to revision at any time by the responsible technical committee and mu
47、st be reviewed every five years andif not revised, either reapproved or withdrawn. Your comments are invited either for revision of this standard or for additional standardsand should be addressed to ASTM International Headquarters. Your comments will receive careful consideration at a meeting of th
48、eresponsible technical committee, which you may attend. If you feel that your comments have not received a fair hearing you shouldmake your views known to the ASTM Committee on Standards, at the address shown below.This standard is copyrighted by ASTM International, 100 Barr Harbor Drive, PO Box C70
49、0, West Conshohocken, PA 19428-2959,United States. Individual reprints (single or multiple copies) of this standard may be obtained by contacting ASTM at the aboveaddress or at 610-832-9585 (phone), 610-832-9555 (fax), or serviceastm.org (e-mail); or through the ASTM website(www.astm.org). Permission rights to photocopy the standard may also be secured from the Copyright Clearance Center, 222Rosewood Drive, Danvers, MA 01923, Tel: (978) 646-2600; http:/ 95 (2015)5
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