CHAPTER ELEVEN. Product Blending GASOLINE OCTANE BLENDING
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1 CHAPTER ELEVEN Product Blending GASOLINE OCTANE BLENDING The research (RON) and motor (MON) octane numbers of a gasoline blend can be estimated using the following equations: 1 where and R = R 1 + C x x (R 2 - Ri x J x ) + C 2 X (Oi - O 2 ) + C 3 (Ai - A 2 ) R = research octane numbers of blend; R 0 = research octane number of each component; R 1 = volume average of octane number; R 2 = volume average of product of R 0 and /; J x = volume average of sensitivity; O\ = volume average of squared olefin content; 02 = square of volume average olefin content; Ai = volume average of squared aromatic content; A2 = square of volume average aromatic content. (11-1) M = M^D 1 X(M 2 -M 1 X J x ) +D 2 (O 1 - O 2 ) + D 3 [^"^j (11-2)
2 where M = motor octane of the blend; Mo = motor octane of each component; Mi = volume average motor octane; M 2 = volume average of product of M 0 and J. These equations represent straight-line blending with three correction terms added to account for the blending deviations normally experienced with gasoline blends. The first term (sensitivity function) is a correction for the blending deviation arising because octane numbers are determined at compression ratio different from those at which the blends are rated. The second (function of olefin content) and third terms (function of aromatic content) are corrections that reflect the influence of chemical interaction of the components in the blend. The coefficients to be used in octane blending follow. The RON equation coefficients are C 1 = C 2 = 061 C The MON equation coefficients are D 1 = D 2 = 081 D 3 = -645 These coefficients are derived from the regression analysis of RON and MON data of actual laboratory blends. EXAMPLE 11-1 Determination of the RON and MON of a gasoline blend are done with the help of a spreadsheet program, assuming the RON, MON, aromatic, and olefin content of all blend components are available. Sample data on the properties of gasoline blend components such as the RON, MON,
3 aromatic, and olefin content of the blend components and calculations for computing the RON and MON of the blend by equations (11-1) and (11-2) are shown in Tables 11-1 and GASOLINE BLENDING BY THE INTERACTION COEFFICIENT METHOD 2 In a given refinery, where the maximum number of gasoline blend components and their properties are known, it is possible to develop an accurate blending spreadsheet program, using the individual blendstock properties and the binary blend interaction coefficients. The only additional laboratory work required is the determination of the properties: RON, MON, and ASTM distillation of all possible binary blends for a given number of blend components. Interaction coefficients are determined for all binary blends and used in the model to accurately predict the properties of any gasoline blend of these components. BLENDING ALGORITHM A study of the gasoline blending data has shown that nonlinear gasoline blending behavior can be described by an equation of the following type: where PcALC = PyOL + /(1,2) X Xi X X 2 + /(1,3)^1 X X /(8,9) XX 8 XX 9 ^CALC = calculated property; / 3 VOL = volumetric weighted average property; /(1,2) /(8,9) =the component interaction coefficients; X\...Xg = volume fraction of each component. The interaction coefficient for a binary blend can be calculated as follows: (11-4)
4 Table 11-1 Research Octane Blending COMPONENT VOL % RON, R (1) (2) MON (3) OLEFIN VOL % (4) OLEF 2 (5) AROMATIC VOL % (6) AROM 2 (7) SENSITIVITY, (8) R*J O) VOUMETRIC, R*J (10) LSR REF 90 REF 95 REF 97 LCN MCN VBU NAPH POLY BUTANE MTBE VOL AVG NOTES: BLEND MON = COLUMNS ARE IN PARENTHESES 2 = RON OF BLEND COMPONENTS. 3 = MOTOR OCTANE OF BLEND COMPONENTS. 5 = SQUARE OF OLEFIN CONTENT (4). 7 = SQUARE OF AROMATIC CONTENT (6). 8 = SENSITIVITY (RON - MON) OF COMPONENTS 9-COL 8 x COL = COL 9 x COL 1.
5 Table 11-2 Motor Octane Blending COMPONENT VOL %, (1) RON, (2) MON, (3) OLEFIN AROMATIC M,VOL %, OLEF 2, VOL %, AROM 2, (4) (5) (6) (7) SENSITIVITY, (8) R*J, (9) VOUMETRIC, R*J, (10) LSR REF 90 REF 95 REF 97 LCN MCN VBU NAPH POLY BUTANE MTBE VOL AVG NOTES: BLEND MON = COLUMNS ARE IN PARENTHESES 2 = RON OF BLEND COMPONENTS. 3 = MOTOR OCTANE OF BLEND COMPONENTS. 5 = SQUARE OF OLEFIN CONTENT (4). 7 = SQUARE OF AROMATIC CONTENT (6). 8 = SENSITIVITY (RON - MON) OF COMPONENTS 9 = COL 8 x COL = COL 9 x COL 1.
6 where 1(A 1 B) interaction coefficient of components A and B\ ^ACTUAL = property of the blend, as determined in the laboratory; P VOL = volumetric weighted average property of the blend; VA j VB = volume fractions of components A and B. In this model, the concept of a blending interactions coefficient is considered and a spreadsheet model developed to predict the octane and volatility of the multicomponent blend. EXAMPLE 11-2 An example of the interaction coefficient method spreadsheet for a multicomponent blend follows. We want to determine the RON, MON, and ASTM distillation of a blend of these components: FCC light naphtha (LCN) FCC medium naphtha (MCN) Light straight run (LSR) Polymer gasoline (POLY) Reformate 95 RON (REF 95) Reformate 97 RON (REF 97) The following properties are determined in the laboratory for each of the blend components and for all possible binary blends: RON, MON, and ASTM distillation; percent evaporated at 150, 195, 250, and 375 F. The number of binary blend components determines how many binary blends are possible. Hence, for a six-component blend, 15 binary blends are possible. All the 15 binary blends are made in the laboratory and their properties determined for computing the interaction coefficient for each binary blend. Once the binary interaction coefficients are known, the properties for any blend composition can be determined by means of the blending equation. The calculations are facilitated by means of a spreadsheet program. The properties of the pure components and all binary blends interaction coefficients are shown in Tables 11-3 to To calculate the properties (RON, MON, distillation) of the blend, the blend composition is entered in Table 11-6 and the blend properties are read from Table 11-7.
7 COMPONENT Table 11-3 Blend Component Properties LCN MCN LSR POLY REF 97 BUTANE DENSITY VAP. PRESSURE psia ASTM DISTILLATION VOL% EVAPORATED IBP 0 C C C C C C FBP, C FIA ANALYSIS SATURATES VoI % OLEFINS VoI % AROMATICS VoI % SULFUR %W/W OCTANE NUMBER RON MON ASTM DISTILLATION BLENDING Two methods are available for estimating the ASTM distillation of a blend: Edmister's method and empirical correlation. EDMISTER'S METHOD ASTM distillation is converted to the true boiling point (TBP) distillation using Edmister's correlation. The blend TBP can be determined simply by adding together the volumes contributed by all the components at a chosen temperature, dividing by the total volume, and plotting a temperature vs. percent distillation chart. The TBP distillation vs. temperature graph can be converted back into ASTM distillation again, by using Edmister's correlation in the reverse. This procedure is not very accurate and the blend can be off by as much as C. The inaccuracy can be attributed to the inadequacy of
8 Table 11-4 Quality of Binary Blends and Interaction Coefficients COMPONENT PAIR LCN MCN 0) LCN LSR (2) LCN POLY (3) LCN REF 97 (4) LCN BUTANE (5) MCN LSR (6) MCN POLY (7) MCN REF 97 (8) MCN BUTANE O) LSR POLY (10) LSR REF 97 (11) LSR BUTANE (12) POLY REF 97 (13) POLY BUTANE (14) REF 97 BUTANE (15) COMPONENT A, VOL% COMPONENT B, VOL% VAPOR PRESSURE bar ASTM DISTIL VOL% C RON 0.40 TEL 0.84 TEL MON 0.40 TEL 0.84 TEL COEFHCIENTS VAPOR PRESSURE, psia ASTM DISTL VOL% O 0 C MON ^ ^ NOTE: COLUMN NUMBERS ARE IN PARENTHESES.
9 Table 11-5 Weighted Coefficients COMPONENT PAIR LCN MCN (1) LCN LSR (2) LCN POLY (3) LCN REF 97 (4) LCN BUTANE (5) MCN LSR (6) MCN POLY (7) MCN REF 97 (8) MCN IBUTANE (9) LSR POLY (10) LSR REF 97 (11) LSR BUTANE (12) POLY REF 97 (13) POLY BUTANE (14) REF 97 BUTANE (15) TOTAL INTERACTION COEFFICIENT (16) VOL. AVG QUALITY (17) ESTIMATED QUALITY (18) VAPOR PRESSURE ASTM 60 0 C RON MON ( () ( ( ( ( ( ( ( ( ( ( ( ( ( ( :
10 Table 11-6 Blend Composition BLEND VOL% LCN 0.30 MCN 0.10 LSR 0.05 POLY 0.12 REF BUTANE 0.03 TOTAL Table 11-7 Blend Results by Interaction Coefficient Method VAPOR PRESSURE psia 9.7 ASTM DISTILLATION 60 0 C RON CLEAR 93.3 MON CLEAR 84.4 Edmister's correlation, particularly in converting ASTM distillation to TBP distillation. GRAPHICAL SUMMATION METHOD An empirical method is described for estimating ASTM distillation of a blend from its composition and ASTM distillation temperature of blend components. This method is used for the following calculations: estimate of the initial boiling point (IBP), 10%, 20-90% points and the estimation of the ASTM end point. Determination of ASTM IBP, 10%, 20-90% Points of Blend This method is applicable to blends containing distillate stocks having an ASTM initial boiling point higher than 85 F and an ASTM end point
11 lower than F. It is based on the observation that a straight summation line can be drawn through an ASTM distillation point of a blend. The slope of this line is such that the sum of the proportions of each blend component corresponds to its intersection with ASTM distillation curve. For TBP distillation, the summation lines are parallel to volume percent axis on an ASTM distillation plot. ASTM summation lines slope due to poor fractionation of ASTM distillation, and the slope varies according to distillation end point. The slope to be used follows: DISTILLATION POINT SLOPE OF SUMMATION LINE, F IBP F PER 100% DISTILLED 10% F PER 100% DISTILLED 20% -100 F PER 100% DISTILLED 30% F PER 100% DISTILLED 40% -50 F PER 70% DISTILLED 50-90% -20 F PER 70% DISTILLED ASTM 10-90% Points ASTM distillation curves are drawn for each blend component, with the temperature on the vertical axis and the volume percent distilled on the horizontal axis. Distillation must be on a consistent basis for all components; that is, either percent evaporated or percent recovered. A guess is made on the temperature at which a given proportion of the blend is distilled, and the corresponding point is marked on the graph. A summation line of specified slope is drawn through the point. The vol% distilled is read off vertically below the intercept of the summation line and ASTM distillation curve of the each component (Figure 11-1). The sums for all blend components should equal the proportion of blend originally estimated. If not, a new guess of temperature at which the specified proportion of blend is distilled is made and the procedure repeated. If the second estimate also does not give the required result, an interpolation is made between the earlier determinations. Initial Boiling Point This method is identical to 10-90% points, except that the distillation curves for the components are extrapolated to 1.4%. Therefore, 1.4%
12 becomes zero of the modified scale and 10% becomes 11.4%. The volume distilled at 1.4% is next calculated by previous procedure to give the IBP of the ASTM curve. EXAMPLE 11-3 Calculate the IBP and 10-90% points of a blend of FCC naphtha (50% volume), coker naphtha (16% volume), and cat reformate (34% volume) with the following ASTM distillation: FCC COKER CAT VOL% NAPHTHA, 0 F NAPHTHA, 0 F REFORMATE, 0 F IBP EP The IBP of the blend, is calculated as follows. Assume that the IBP represents 1.4% distilled instead of 0% and modify the preceding data as follows: FCC COKER CAT VOL% NAPHTHA, 0 F NAPHTHA, 0 F REFORMATE, F Now draw the ASTM distillation curves with percent distilled on the X- axis and distillation temperature on Y-axis. Read off the temperature at which 1.4% volume is distilled off. Assuming IBP (1.4% distilled) at F,
13 TEMPERATURE, 0 F CAT REFORMATE FCCU NAPHTHA COKER NAPHTHA F F 50% BLEND TEMPERATURE PERCENT RECOVERED Figure ASTM distillation blending procedure. BLEND COMPONENT VOL% AT F % IN BLEND TOTAL FCCNAPHTHA COKERNAPHTHA CATREFORMATE TOTAL As the percent distilled is less than 1.4%, next assume a higher IPB temperature, at F, and repeat the procedure: BLEND COMPONENT VOL% AT F % IN BLEND TOTAL FCCNAPHTHA COKERNAPHTHA CATREFORMATE TOTAL
14 Therefore, the blend distilled at F is 2.13 vol%. By interpolation between these two values (0.7% and 2.13%), we determine the temperature at which 1.4% of the blend is distilled off; that is, F. Calculations for ASTM 10-90% points are shown in Table ASTM End Point of Blend The end point of a two-component blend is a function of the end point, proportion of blend component, and slope of the tail of the distillation curve of the higher-boiling component. Procedure From Table 11-9, read off the factor relating the difference between the end point of the components and their proportion in the blend. From Table 11-10, read off the factor relating slope of the tail of the higherboiling component and its proportion in the blend. Add the product of these two factors to the end point of the lower-boiling component, and the result is the predicted end point of the blend. Multicomponent blends are calculated as though the final blend were the result of a series of binary blends, starting with lowest-end-point component and successively adding higher-end-point components. This procedure is elaborated in Table VAPOR LOCK PROTECTION TEMPERATURE When the volatility of gasoline is too high or when high temperatures or low pressure conditions prevail, bubbles of vapor can form at critical points in the fuel systems. This prevents adequate supply of fuel to the engine by preventing the fuel pump from operating because of low or negative suction pressure. Vapor lock has a number of unwelcome effects, such as difficulty restarting a hot engine, uneven running, and reduced power output at high speed. Vapor lock is influenced by the volatility characteristics of the fuel. The degree to which a fuel is liable to produce vapor lock depends mainly on the front-end volatility of the fuel blend.
15 ASTM DISTILLATION FCC NAPHTHA, % DISTILLED COKER GASOLINE, % DISTILLED Table 11-8 Calculation of the ASTM Distillation of the Blend CAT REFORMATE, % DISTILLED FCC NAPHTHA, % DISTILLED x VOL% COKER GASOLINE, % DISTILLED x VOL% CAT REFORMATE, % DISTILLED x VOL% BLEND, % DISTILLED ASTM BLEND TEMPERATURE, 0 F INTERPOLATED ASSUME IBP = F ASSUMEIBP= F ASSUME 10% = F ASSUME 10% = 130 F ASSUME 30% = 150 F ASSUME 30% = 160 F ASSUME 50% = 180 F ASSUME 50% = 190 F ASSUME 70% = F ASSUME 70% = F ASSUME 90% = 270 F ASSUME 90% = 28O 0 F NOTE: IBP IS THE TEMPERATUTRE ON MODIFIED SCALE WITH ORIGIN SHIFTED TO -1.4% VOLUME, WHERE 1.4% BLEND DISTILLS OFF.
16 Table 11-9 ASTM End-Point Coefficients, High-End-Point Component in Blend PROPORTION OF HIGH-END-POINT COMPONENT IN BINARY BLEND, A 0 F NOTE: DELTA IS THE DIFFERENCE IN THE END POINTS OF COMPONENTS. The vapor lock protection temperature (VLPT) of a gasoline blend is the temperature at which a certain fixed vapor/liquid ratio (usually 20 or more) exists. Although a number of different indices exist, they are equally valid for predicting the susceptibility of the fuel to cause vapor lock problems.
17 Table ASTM End-Point Coefficients, Difference between 90% Point and End Point of Higher-Boiling Component % HIGHER END POINT STOCK IN BLEND DIFFERENCE
18 Table ASTM End Point of Blend Calculate the end point of the following blend: FCC naphtha = 50% Coker naphtha= 16% Cat reformate = 34% ASTM distillation of the blend components are as per earlier example (1) CONSIDER A BINARY BLEND OF FCC NAPHTHA AND COKER NAPHTHA. ASTM END POINT, 0 F % FCC GASOLINE IN BLEND REFERRING TO TABLE 11-9, FACTOR 1 DIFFERENCE BETWEEN END POINT AND 90% POINT (HIGHER-END POINT COMPONENT) REFERRING TO TABLE 11-10, FACTOR 2 FACTOR 1 x FACTOR 2 THEREFORE END POINT OF BINARY FCC NAPHTHA AND COKER NAPHTHA (2) NEXT CONSIDER A BLEND OF ABOVE BINARYAND CAT REFORMER NAPHTHA DIFFERENCE IN END POINTS (FCC + COKER) BINARY AND C. REFORMATE NAPHTHA PROPORTION OF C. REFORMATE IN BLEND REFERRING AGAIN TO TABLES 11-9 AND FACTOR 1 FACTOR 2 FACTOR 1 x FACTOR 2 END POINT OF THE BLEND (FCC Naphtha + Coker Naphtha + Cat Reformate) FCC NAPHTHA 295 COKER NAPHTHA ( ) ( ) 293 F F 34% ( ) F DELTA
19 Jenkin Equation 3 VLPT, T 2 O is the temperature at which vapor/liquid ratio is 20. VLPT is expressed as a function of the RVP (Reid Vapor Pressure) and the ASTM 10 and 50% points: where VLPT = x (RVP) x (10% point) x (50% point) VLPT = temperature, 0 C; RVP = RVP, kpa; 10%, 50% = ASTM distillation point, 0 C. Acceptable VLPT numbers depend on the maximum ambient temperature of the area where the gasoline is designed to be used. For example, if the maximum summer temperature touches 50 0 C at any location, the VLPT must be more than 50 0 C by reducing the lower-volatility blend components in the gasoline formulation. VISCOSITY BLENDING The viscosities of petroleum fractions do not blend linearly, and viscosity blending is done with the help of blending indices. Table presents volume blending indices, and Table presents weight blending indices at 122 F. EXAMPLE 11-4 Determine the amount of cutter stock need to blend vacuum resid with a kinematic viscosity of 80,000 cst at 122 F to finished fuel oil with viscosity of 180 centistokes at 122 F. The cutter stock viscosity is 8.0 cst. To estimate the cutter requirements, determine the viscosity blend indices for vacuum residuum, cutter stock and finished fuel oil from the viscosity blend indices table and blend these values linearly. We see from the table on page 330 that 42.7% cutter stock is required to reduce the final blend viscosity to 175 centistokes.
20 Table Viscosity Blending Indices CSt
21 Table Continued CSt NOTE: VISCOSITIES OF PETROLEUM PRODUCTS DO NOT BLEND LINEARLY ON VOLUME OR WEIGHT BASIS. BLENDING INDICES ARE THEREFORE EMPLOYED. INDICES FOR VOLUMETRIC BLENDING ARE PRESENTED IN THE TABLE. THE UNITS OF KINEMATIC VISCOSITY ARE IN CENTISTOKES.
22 Table Viscosity Blending Indices, Weight Basis cst ,
23 Table Continued VISCCST H VISCCST H VISC, CST H VISC, CST H 10, , ,000, ,000, , , ,000, ,000, , , ,000, ,000, , , ,000, ,000, , , ,000, ,000, , , ,000, ,000, , , ,000, ,000, , , ,000, ,000, , , ,000, ,000, NOTES: VISCOSITIES OF PETROLEUM PRODUCTS DO NOT BLEND LINEARLY ON VOLUME OR WEIGHT BASIS. BLENDING INDICES ARE THEREFORE EMPLOYED. INDICES FOR A WEIGHT BASIS BLENDING (ALSO CALLED REFUTAS FUNCTIONS) ARE PRESENTED IN THE TABLE. THE UNITS OF KINEMATIC VISCOSITY ARE IN CENTISTOKES. BLENDING INDICES FOR VARIOUS VISCOSITY RANGES ARE PRESENTED. THESE ARE CALCULATED BY THE FOLLOWING RELATIONSHIPS: I = *LOG LOG(V + 0.8) V = KINEMATIC VISCOSITY IN CENTISTOKE UNITS IN CASE VISCOSITY BLENDING INDEX IS KNOWN, VISCOSITY IN CENTISTOKES IS CALCULATED AS FOLLOWS: V = (io( 1() ( VI O97 > / >) I = VISCOSITY INDEX (WT. BASIS BLENDING) COMPONENT VISCOSITY, CST BLEND INDEX, H VOL% VACUUMRESID 80, CUTTERSTOCK BLEND BLENDING MARGIN A blending margin of 4-5 H is normally allowed. Therefore, to meet a guaranteed specification of 464 //, corresponding to 180cst, fuel oil must be blended to 460 H or 170 cst. POUR POINT BLENDING The pour point and freeze point of the distillate (kerosene, diesels, etc.) do not blend linearly, and blending indices are used for linear blending by
24 volume. Tables and show the blending indices used to estimate the pour point and cloud point of distillate petroleum products. A blending margin of 10 PI (pour index) is allowed between the guaranteed specification and the refinery blending. For example, to guarantee a pour spec of 6 C (21.2 F, pour index 336.3), the blending target would be PI. In terms of the pour point, this corresponds to a blending margin of 1 F. EXAMPLE 11-5 Determine the amount of kerosene that must be blended into diesel with a 43 F pour point to lower the pour point to 21 0 F. The properties of kerosene and diesel stream are as follows: KEROSENE DIESEL SPECIFIC GRAVITY POUR POINT F 43 F To determine the pour point of the blend, determine the pour indices, from the pour blend table, corresponding to the pour points of kerosene and diesel, then the target pour point and blend linearly as follows: BLEND COMPONENT POUR POINT, 0 F BLEND INDEX VOL% DIESEL KEROSENE BLEND Therefore, to lower the pour point to 21 0 F, 46.4% kerosene by volume must be blended. FLASH POINT BLENDING The flash point of a blend can be estimated from the flash point of the blend components using flash point blend indices, which blend linearly
25 Table Pour Point of Distillate Blends POUR POUR POUR POINT, 0 R INDEX POINT, 0 R INDEX POINT, 0 R INDEX NOTES: ALSO APPLICABLE TO FREEZE POINTS AND FLUIDITY BLENDING IS ON A VOLUME BASIS. POUR POINT BLEND INDEX = * x (POUR POINT, R/1000) 125 POUR POINTER = 1000 x (Index/316000) 008 POUR POINT, 0 F = POUR POINT ( 0 R) CORRELATION OF HU AND BURNS.
26 Table Continued POUR POUR POUR POINT, 0 R INDEX POINT, 0 R INDEX POINT, 0 R INDEX
27 Table Cloud Point of Distillate Blends CLOUD CLOUD CLOUD POINT, 0 R INDEX POINT, R INDEX POINT, 0 R INDEX NOTES: FOR CLOUD POINTS BELOW 0 0 F THE INDEX SHOULD BE BLENDED ON WEIGHT BASIS. THE BLENDING INDEX IS GIVEN BY THE FOLLOWING EQUATION: / = exp[2.303( x D].
28 Table Continued CLOUD CLOUD CLOUD POINT, F INDEX POINT, F INDEX POINT, F INDEX
29 on volume basis. The flash point (in 0 F) vs. flash blend indices are presented in Table EXAMPLE 11-6 Determine the flash point of a blend containing 30 vol% component A with a flash point of F, 10% component B, with a flash of 90 0 F, and 60% component C with a flash point of F. From the flash blending tables, find the blend indices for the three components and blend linearly with the volume as follows: FLASH FLASH VOLUME x COMPONENT VOL% POINT, 0 F INDEX FLASH INDEX A B C BLEND The flash index of the blend is computed at 478.1, which corresponds to a flash point of 111 F. ALTERNATIVE METHOD FOR DETERMINING THE BLEND FLASH POINT The flash index is first determined from Table Two empirical indices are worked out, the 154 index and the 144 index. The 154 index is a criteria for meeting the 154 F flash point and 144 index is criteria for meeting the 144 F flash point. If the value of the 154 index is positive for any component or blend, it will meet the 154 F flash criteria; that is, the flash will be equal to or higher than 154 F. Similarly, if the 144 flash index is positive, it will meet the 144 F flash criteria. If the 144 index is negative, the corresponding flash point will be lower than 144 F: 154 index - ( x FI) x MB where FI is the flash index (Table 11-17) and MB is moles/barrel.
30 Table Flash Point (Abel) vs. Flash Blending Index 4 FLASH POINT, 0 F HO NOTES: FLASH INDEX = io( / (^ASHPOINT ) FLASH POINT = /(LOG (FLASH INDEX) ) WHERE FLASH POINT (ABEL) IS IN 0 F. 144 index = ( x FI) x MB This estimation requires data on molecular weight of the fraction. For routinely blended stocks, the values of the 144 and 154 indices are prepared, and these can be used to determine whether or not the given blend will meet the flash index. Each index blends linearly with volume and has zero as a reference point.
31 Table Flash Point vs. Flash Index (for 154 and 144 Indices) FLASH POINT, 0 C FLASH INDEX - io^050-86^ ) )) F = FLASH POINT ( 0 C)
32 EXAMPLE 11-7 Determine whether the following fuel oil blend will meet the 154 and 144 flash criteria: STREAM VOL% SPECIFIC GRAVITY API MB FLASH, C Fl 144 INDEX 154 INDEX VACUUM RESID FCC CUTTER KEROSENE LT. DIESEL BLEND As the 144 and 154 indices are positive for this blend, the blend meets both 144 and 154 flash specifications. REID VAPOR PRESSURE BLENDING FOR GASOLINES AND NAPHTHAS Gasolines of different Reid vapor pressures (RVPs) do not blend linearly. For accurately estimating the RVP of the blends, RVP blend indices are used. These are presented in Table EXAMPLE 11-8 Calculate the RVP of a blend of n-butane, alkylate, and cat reformate with following properties: COMPONENT VOLUME FRACTION VAPOR PRESSURE (VP), kpa VP BLEND INDEX (VPBI) VOL*VPBI rc-butane ALKYLATE REFORMATE BLEND
33 Next Page PRESSURE Table Vapor Pressure vs. RVP Index of Gasolines RVPINDBt kpa RVP INDEX OF LPG GASES FOR GASOLINE BLENDING: VAPOR PRESSURE, RVP COMPONENT kpa INDEX* PROPANE i-butane rc-butane *RVP INDEX (VP/6.8947) 1 25 Given the RVP of the blend components the vapor pressure blend index for individual components is read from the RVP vs. RVP indices table. The RVP index for the blend is next estimated by linear blending the component RVP indices. Thus, a blend index of 9.6 corresponds to a RVP of 42.IkPa for this blend.
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