1、Designation: D 2889 95 (Reapproved 2005)e1An American National StandardStandard Test Method forCalculation of True Vapor Pressures of Petroleum DistillateFuels1This standard is issued under the fixed designation D 2889; the number immediately following the designation indicates the year oforiginal a
2、doption or, in the case of revision, the year of last revision. A number in parentheses indicates the year of last reapproval. Asuperscript epsilon (e) indicates an editorial change since the last revision or reapproval.e1NOTEAdjunct references were corrected editorially in April 2006.1. Scope1.1 Th
3、is test method describes the calculation of true vaporpressures of petroleum distillate fuels for which 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
4、 pres-sures at temperatures between the 0 % equilibrium flashtemperature and the critical temperature 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 f
5、uels. However, if both the critical pressureand critical temperature are known, the values shall be 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 requir
6、ed.If either a determined true boiling point or determined equi-librium flash vaporization temperature 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 distil
7、late fuels having aboiling range of less than 100F (38C) between the TestMethod D8610 and 90 volume % distilled temperatures.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 informat
8、ion onlyand are not considered standard.1.6 This standard does not purport to address all 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
9、limitations prior to use.2. Referenced Documents2.1 ASTM Standards:2D86 Test Method for Distillation of Petroleum Products atAtmospheric PressureD 287 Test Method forAPI Gravity of Crude Petroleum andPetroleum Products (Hydrometer Method)2.2 ASTM Adjuncts:Temperature Pressure Conversion Chart (16 by
10、 20in. draw-ings)33. Summary of Test Method3.1 Equilibrium flash vaporization (EFV) temperatures arecalculated from distillation data (Test Method D86) deter-mined on the sample. The distillation data, calculated EFVdata, and API gravity of the sample are used with a graphicalcorrelation procedure t
11、o obtain two pairs of temperature-pressure coordinates through which the bubble-point line of thephase diagram for the sample may be drawn. The calculatedtrue vapor pressure at a specified temperature is obtained byreading the pressure at the intersection of the bubble-point lineand specified temper
12、ature.NOTE 1Details of the procedure and data substantiating its validityfor establishing equilibrium flash vaporization temperatures have beenpublished.44. Significance and Use4.1 The true vapor pressure of a distillate fuel is a relativemeasurement, both of the tendency of the most volatile portio
13、nof the fuel to gasify, and of the restraining pressure required toprevent gasification of the most volatile portion. Thus themeasurement is of importance when a fuel is to be utilized in1This test method is under jurisdiction of ASTM Committee D02 on PetroleumProducts and Lubricants and is the dire
14、ct responsibility of Subcommittee D02.04on Hydrocarbon Analysis.Current edition approved Nov. 1, 2005. Published November 2005. Originallyapproved in 1970. Last previous edition approved in 2000 as D 2889 95 (2000).2For referenced ASTM standards, visit the ASTM website, www.astm.org, orcontact ASTM
15、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.ADJD2889.4Edmister, W. C., and Okamoto, K. K., “Applied Hydrocarbon Thermodynam-
16、ics, Part 12: Equilibrium Flash Vaporization Correlations for Petroleum Fractions,”Petroleum Refiner, PEREA, Vol 38, No. 8, 1959, p. 117.1Copyright ASTM International, 100 Barr Harbor Drive, PO Box C700, West Conshohocken, PA 19428-2959, United States.applications where no gasification may be tolera
17、ted, andtemperature-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, 30, 50, 70, and 90 volume % distilled obtained inaccordance with Test Method D86.5.2 API gravity determined i
18、n accordance with Test MethodD 287, or a method of equivalent accuracy.6. Procedure6.1 Calculate the 10/70 slope, F/%, of the Test MethodD86 distillation using the 10 and 70 volume % distilledtemperature. Using this slope and the Test Method D8650volume % distilled temperature, obtain to the nearest
19、 61F atemperature difference, F, from Fig. 2. Add F to the MethodD8650 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 and 30 volume %, and the 30 and50 volume % tempera
20、tures. Using these differences, obtain tothe nearest 1F, the temperature differences between corre-sponding EFV percentages from Fig. 3.6.3 Calculate the EFV zero volume percent temperature bysubtracting the sum of the three differences obtained from Fig.3, from the EFV 50 volume % temperature calcu
21、lated 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 % temperature at atmo-spheric pressure has been meas
22、ured, 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 criticaltemperature and critical pressure of the fuel are known, thec
23、alculations 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 16 by 20in. charts.FIG. 1 Test Method D86Distillation
24、Temperature and Equalization Flash Vaporization Temperature Pressure Conversion ChartD 2889 95 (2005)e12the 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 of theTest Method D86 distillation curve, F/volume
25、 %, as thedifference between 10 and 90 volume % distilled temperaturesdivided by 80.6.5.2 Calculate to the nearest 1F, the volumetric averageboiling point (VABP) as the sum of the Test Method D8610,30, 50, 70, and 90 volume % distilled temperatures divided by5.6.5.3 Calculate to the nearest 0.1 unit
26、 the ratio:VABP/10/90 Slope 1 16.0! (1)6.5.4 Enter Fig. 1 on the lower right scale at theTest MethodD86VABP temperature. From the intersection of the VABPtemperature and the line of constantAPI gravity correspondingto the gravity of the sample, proceed horizontally to the pointof intersection with t
27、he 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 section. This point ofintersection establishes the upper end, or focal point of thebubble-point line.6.
28、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 temperature by readingthe vertical pressure scale of Fig. 1 at the intersection of thebubble-poin
29、t 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 maximum vapor pressureto be reported.6.7.2 If neither the critical temperature nor critical pressurei
30、s 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 be reported.7. Report7.1 Report the results as indicated in the following tabula-tion:Vapor Pressu
31、re Range,psia:Report to theNearest: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 kilopascals(kPa) by multiplying the results obtained in 7.1 by theconversion factor 6.894757 and then round
32、ing 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 asfollows:8.1.1 RepeatabilityThe difference between successive testresults, obtained by the same operator w
33、ith 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 one case intwenty: the larger of 2 psia (14 kPa) or 4 % of the mean of thetwo results.8.1.2 Reproduci
34、bilityThe difference between two, singleand independent results, obtained by different operators work-ing in different laboratories on identical test material, would, inthe normal and correct operation of the test method, exceed thefollowing value only 1 case in 20: the larger of 2 psia (14 kPa)or 8
35、 % 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 initial boiling points in the range 320 to 400F (160 to204C), and end points in the range 430 to 534F (22
36、1 to 279C). Eachlaboratory determined the required distillation and gravity data in dupli-cate, and performed the calculations required for this procedure once foreach of the two sets of determined data for each sample. Vapor pressureswere not determined during the cooperative program.8.2 BiasThe bi
37、as of the true vapor pressures obtained bythis test method has not been evaluated. Determined true vaporpressures were not known for the fuels cooperatively tested.9. Keywords9.1 API gravity; D86distillation; true vapor pressure6“Technical Data Book-Petroleum Refining,” American Petroleum Institute,
38、2101 L St. NW Washington DC 20037. Fig. 4 is a modified version of Fig. 4 A1.2,Chapter 4.FIG. 2 Test Method D8650 % Distilled Temperature versusEquilibrium Flash Vaporization 50 % TemperatureD 2889 95 (2005)e13FIG. 3 Test Method D86Distillation Temperature Differences Versus Equilibrium Flash Vapori
39、zation Temperature DifferencesFIG. 4 Critical Temperature, Gravity, and Test Method D86Volumetric Average Boiling Point FD 2889 95 (2005)e14APPENDIX(Nonmandatory Information)X1. EXAMPLE OF TRUE VAPOR PRESSURE CALCULATIONX1.1 Calculate the true vapor pressure at 400F, for a fuelfor which the followin
40、g data have been determined:API gravityMethod D86distillation, F40.0(IBP)-IP 123 0 % 27510 % 34530 % 40450 % 43670 % 46590 % 505X1.1.1 From Fig. 2, using the 10/70 slope of 2.0 and the50 % distillation temperature, a value of 6 is obtained as theincrement to add to the 50 % distillation temperature
41、to obtainthe EFV 50 % temperature. Thus the calculated 50 % tempera-ture is 436 6, or 430F.X1.1.2 From Fig. 3, usingASTM temperature differences of70 for 0 to 10 %, 59 for 10 to 30 %, and 32 for 30 to 50 %, EFVtemperature differences of 34, 37, and 17, respectively, wereobtained and their sum determ
42、ined to be 88. Thus the calcu-lated EFV 0 % temperature is 430 88, or 342F. The coordi-nates for the lower end of the bubble-point line are 342F and14.7 psia (distillation pressure), as plotted on Fig. 1.X1.1.3 The slope of the Test Method D86distillation curvefrom 10 to 90 % is equal to (505 345)/8
43、0, or 2.0F/%.X1.1.4 The volumetric average boiling point is equal to(345 + 404 + 436 + 465 + 505)/5, or 431F.X1.1.5 The ratio, VABP/(10/90 Slope + 16.0) is 431/(2.0 + 16.0), or 23.9.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 the
44、VABP, 431F, 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 drawnby connecting the focal point and the point obtained asexplained in X1.1.2.X1.1.7 The calculated true vapor pressure at 40
45、0F, 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 mentionedin this standard. Users of this standard are expressly advised that determination of the validity of any such patent rights
46、, 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 must be reviewed every five years andif not revised, either reapproved or withdrawn. Your comments are invited either for re
47、vision of this standard or for additional standardsand should be addressed to ASTM International Headquarters. Your comments will receive careful consideration at a meeting of theresponsible technical committee, which you may attend. If you feel that your comments have not received a fair hearing yo
48、u 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 C700, 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).D 2889 95 (2005)e15
