CHAPTER ELEVEN. Product Blending GASOLINE OCTANE BLENDING

Size: px
Start display at page:

Download "CHAPTER ELEVEN. Product Blending GASOLINE OCTANE BLENDING"

Transcription

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.

Product Blending & Optimization Considerations. Chapters 12 & 14

Product Blending & Optimization Considerations. Chapters 12 & 14 Product Blending & Optimization Considerations Chapters 12 & 14 Gases Polymerization Sulfur Plant Sulfur Gas Sat Gas Plant LPG Butanes Fuel Gas Gas Separation & Stabilizer Light Naphtha Isomerization Alkyl

More information

On-Line Process Analyzers: Potential Uses and Applications

On-Line Process Analyzers: Potential Uses and Applications On-Line Process Analyzers: Potential Uses and Applications INTRODUCTION The purpose of this report is to provide ideas for application of Precision Scientific process analyzers in petroleum refineries.

More information

Table of Contents. Copyright and Trademarks 5. Copyright 5 Revision 5 Disclaimer of Liability 5 Copy and Use Restrictions 5.

Table of Contents. Copyright and Trademarks 5. Copyright 5 Revision 5 Disclaimer of Liability 5 Copy and Use Restrictions 5. Table of Contents Copyright and Trademarks 5 Copyright 5 Revision 5 Disclaimer of Liability 5 Copy and Use Restrictions 5 Introduction 6 Blending Quality Models Equations 7 Overview 7 Common Terms 7 Density

More information

Crude Assay, ASTM, TBP distillations, Evaluation of crude oil properties.

Crude Assay, ASTM, TBP distillations, Evaluation of crude oil properties. Crude Assay, ASTM, TBP distillations, Evaluation of crude oil properties. Crude Oil Distillation Crude oil distillation is an open art technology. The crude oil is distilled at atmospheric pressure and

More information

CHAPTER 2 REFINERY FEED STREAMS: STREAMS FROM THE ATMOSPHERIC AND VACUUM TOWERS

CHAPTER 2 REFINERY FEED STREAMS: STREAMS FROM THE ATMOSPHERIC AND VACUUM TOWERS CHAPTER 2 REFINERY FEED STREAMS: STREAMS FROM THE ATMOSPHERIC AND VACUUM TOWERS About This Chapter The previous chapter introduced crude oil as a mixture of compounds. The characteristics of these compounds

More information

EXPERIMENTAL STUDY ON THE INFLUENCE OF ETHANOL AND AUTOMOTIVE GASOLINE BLENDS By

EXPERIMENTAL STUDY ON THE INFLUENCE OF ETHANOL AND AUTOMOTIVE GASOLINE BLENDS By EXPERIMENTAL STUDY ON THE INFLUENCE OF ETHANOL AND AUTOMOTIVE GASOLINE BLENDS By 1. Department of Mining and Petroleum Engineering, Al-Azhar University, Egypt. tarekfetouh@yahoo.com 2. Department of Chemical

More information

On-Line NIR Analysis for Blending

On-Line NIR Analysis for Blending Application Note On-Line NIR Analysis for Blending Introduction Gasoline and Diesel blending is a refinery operation that blends different component streams into various grades of final product. The main

More information

Kolmetz Handbook of Process Equipment Design REFINERY ATMOSPHERIC CRUDE TOWER SELECTION AND SIZING (ENGINEERING DESIGN GUIDELINE)

Kolmetz Handbook of Process Equipment Design REFINERY ATMOSPHERIC CRUDE TOWER SELECTION AND SIZING (ENGINEERING DESIGN GUIDELINE) Page: 1 of 164 SOLUTIONS, STANDARDS AND SOFTWARE www.klmtechgroup.com Rev 01 KLM Technology #03-12 Block Aronia, Jalan Sri Perkasa 2 Taman Tampoi Utama 81200 Johor Bahru Malaysia Kolmetz Handbook of TOWER

More information

Estimation Procedure for Following Vapor Pressure Changes

Estimation Procedure for Following Vapor Pressure Changes Estimation Procedure for Following Vapor Pressure Changes through Repeated Blending of Petroleum Stocks from Boiling Point Curves A practical method to estimate the vapor pressures of blended and reblended

More information

White Paper. Improving Accuracy and Precision in Crude Oil Boiling Point Distribution Analysis. Introduction. Background Information

White Paper. Improving Accuracy and Precision in Crude Oil Boiling Point Distribution Analysis. Introduction. Background Information Improving Accuracy and Precision in Crude Oil Boiling Point Distribution Analysis. Abstract High Temperature Simulated Distillation (High Temp SIMDIS) is one of the most frequently used techniques to determine

More information

Crude Assay Report. Crude Oil sample marked. Barrow Crude Oil. On Behalf Of. Chevron Australia Pty Ltd. Laboratory Supervisor. Crude Assay Chemist

Crude Assay Report. Crude Oil sample marked. Barrow Crude Oil. On Behalf Of. Chevron Australia Pty Ltd. Laboratory Supervisor. Crude Assay Chemist Crude Assay Report on Crude Oil sample marked Barrow Crude Oil On Behalf Of Chevron Australia Pty Ltd. Reported by: Approved by: Michelle Fernandez Laboratory Supervisor Jhonas Fernandez Crude Assay Chemist

More information

MB3600-HP10 Laboratory FT-NIR analyzer for hydrocarbon applications Pre-calibrated for blended gasoline, diesel, reformate and naphtha

MB3600-HP10 Laboratory FT-NIR analyzer for hydrocarbon applications Pre-calibrated for blended gasoline, diesel, reformate and naphtha Measurement & Analytics Measurement made easy MB3600-HP10 Laboratory FT-NIR analyzer for hydrocarbon applications Pre-calibrated for blended gasoline, diesel, reformate and naphtha Hydrocarbon Applications

More information

Exceeding Expectations

Exceeding Expectations Technical Notes # 028 Linear vs. Non-Linear that is the question Exceeding Expectations When blending, it is important to understand whether the specification you are blending for is linear or non-linear

More information

MUTINEER EXETER CRUDE OIL. Santos Limited

MUTINEER EXETER CRUDE OIL. Santos Limited Crude Assay Job Number 08-January-2015 43.1 API 0.10 mgkoh/g TAN 0.038 %m Sulphur 11.8 K Factor on behalf of Santos Limited :Report By Approved By: Joshua Camens Lab. Supervisor Jhonas Fernandez Lab. Manager

More information

Ceiba Crude (31.44 API, Sul WT%)

Ceiba Crude (31.44 API, Sul WT%) Ceiba Crude (31.44 API, 0.398 Sul WT%) Crude Name: Ceiba Crude API Gravity API 31.44 Component Wt % Vol % Crude ID: CEIBA2015 Density @15 deg C KG/L 0.8679 C2 Minus 0.004 0.01 Country: Equatorial Guinea

More information

Supporting Information for: Economic and Environmental Benefits of Higher-Octane Gasoline

Supporting Information for: Economic and Environmental Benefits of Higher-Octane Gasoline Supporting Information for: Economic and Environmental Benefits of Higher-Octane Gasoline Raymond L. Speth Eric W. Chow Robert Malina Steven R. H. Barrett John B. Heywood William H. Green Contents Supporting

More information

Supply of Services for Detailed OEB Crude Assay Analysis

Supply of Services for Detailed OEB Crude Assay Analysis Tender Number [9900009229] Supply of Services for Detailed OEB Crude Assay Analysis SCOPE OF WORK SCOPE OF WORK 1. Introduction Orpic is the brand name for Oman Oil Refineries and Petroleum Industries

More information

White Paper.

White Paper. The Advantage of Real Atmospheric Distillation Complying with the ASTM D7345 Test Method in the Distillation Process Introduction / Background In the past, refiners enjoyed a constant supply of the same

More information

Refinery Stock Balancing

Refinery Stock Balancing CHAPTER TWELVE Refinery Stock Balancing Before the advent of linear programming (LP) models, process-planning studies were done by hand with desktop calculators and usually large printed or duplicated

More information

Crude Distillation Chapter 4

Crude Distillation Chapter 4 Crude Distillation Chapter 4 Gases Gas Sat Gas Plant Polymerization LPG Sulfur Plant Sulfur Alkyl Feed Alkylation Butanes Fuel Gas LPG Gas Separation & Stabilizer Light Naphtha Heavy Naphtha Isomerization

More information

Prediction of Physical Properties and Cetane Number of Diesel Fuels and the Effect of Aromatic Hydrocarbons on These Entities

Prediction of Physical Properties and Cetane Number of Diesel Fuels and the Effect of Aromatic Hydrocarbons on These Entities [Regular Paper] Prediction of Physical Properties and Cetane Number of Diesel Fuels and the Effect of Aromatic Hydrocarbons on These Entities (Received March 13, 1995) The gross heat of combustion and

More information

A new simple and robust process FT-NIR Spectrometer with small footprint and extended maintenance interval

A new simple and robust process FT-NIR Spectrometer with small footprint and extended maintenance interval Thomas Buijs, Michael B. Simpson, ABB Quebec, BU MA Analytical Measurements Oil & Gas Industry A new simple and robust process FT-NIR Spectrometer with small footprint and extended maintenance interval

More information

Specifications Of Straight Run Naphtha for Exportation

Specifications Of Straight Run Naphtha for Exportation Specifications Of Straight Run Naphtha for Exportation ASTM Specific Gravity @ 60/60 F 1298 160 0.690-0.730 Colour VISUAL Colourless R.V.P @ 100 F kg/cm2 max 323 69 0.07 Sulphur, Total %mass max 1266 107

More information

The Advantage of Real Atmospheric Distillation using D7345 Test Method. Presented by Jonathan Cole, PAC

The Advantage of Real Atmospheric Distillation using D7345 Test Method. Presented by Jonathan Cole, PAC The Advantage of Real Atmospheric Distillation using D7345 Test Method Presented by Jonathan Cole, PAC Distillation - a Critical Measurement Crude feedstock has a complex mixture of hydrocarbons Separate

More information

Heartland Pipeline. Heartland Pipeline Company Product Specifications. Effective Date: 10/1/2015

Heartland Pipeline. Heartland Pipeline Company Product Specifications. Effective Date: 10/1/2015 Company Product Name Gasoline, Subgrade, 83 octane (87 after 0% ETOH addition) Destination(s) V Grade Gasoline, Conventional, 9 octane (no ethanol) A Grade Distillate, #2 Diesel Fuel / Fuel Oil, Ultra-Low

More information

Petroleum Refining Fourth Year Dr.Aysar T. Jarullah

Petroleum Refining Fourth Year Dr.Aysar T. Jarullah Oil Products 1- Gaseous Fuels. Natural gas, which is predominantly methane, occurs in underground reservoirs separately or in association with crude oil. The principal types of gaseous fuels are oil (distillation)

More information

ANNEX 3 REFERENCE FUELS. Parameter Unit Limits (1) Test method Minimum Maximum Research octane number, RON

ANNEX 3 REFERENCE FUELS. Parameter Unit Limits (1) Test method Minimum Maximum Research octane number, RON WLTP-2012-018 Annex 3 Draft Reference fuels 03.06.2012 ANNEX 3 REFERENCE FUELS The reference fuel specifications listed in this annex are those that are to be used for the WLTP Validation 2 exercise and

More information

ANNEX 2, REFERENCE FUELS

ANNEX 2, REFERENCE FUELS ANNEX 2, REFERENCE FUELS A.2.1. A.2.1.1. EUROPE, INDIA, SOUTH AFRICA Petrol (E5) Parameter Unit Limits (1) Test method Research octane number, RON 95.0 EN 25164 pren ISO 5164 Motor octane number, MON 85.0

More information

COOPER BASIN CRUDE OIL. Santos Limited

COOPER BASIN CRUDE OIL. Santos Limited Crude Assay Job Number 13-September-2016 43.1 API

More information

Lecture 3: Petroleum Refining Overview

Lecture 3: Petroleum Refining Overview Lecture 3: Petroleum Refining Overview In this lecture, we present a brief overview of the petroleum refining, a prominent process technology in process engineering. 3.1 Crude oil Crude oil is a multicomponent

More information

SCOPE OF ACCREDITATION TO ISO/IEC 17025:2005

SCOPE OF ACCREDITATION TO ISO/IEC 17025:2005 SCOPE OF ACCREDITATION TO ISO/IEC 17025:2005 LABORATORY & ON-STREAM ANALYSER DIVISION, SAUDI ARAMCO TOTAL REFINING AND PETROCHEMICAL COMPANY LAB & OSA Division Saudi Aramco Total Refining and Petrochemical

More information

Module8:Engine Fuels and Their Effects on Emissions Lecture 36:Hydrocarbon Fuels and Quality Requirements FUELS AND EFFECTS ON ENGINE EMISSIONS

Module8:Engine Fuels and Their Effects on Emissions Lecture 36:Hydrocarbon Fuels and Quality Requirements FUELS AND EFFECTS ON ENGINE EMISSIONS FUELS AND EFFECTS ON ENGINE EMISSIONS The Lecture Contains: Transport Fuels and Quality Requirements Fuel Hydrocarbons and Other Components Paraffins Cycloparaffins Olefins Aromatics Alcohols and Ethers

More information

Conversion of Peanut Oil into Jet and Diesel Fuels. Panama City, Florida 22 July 2016 Edward N. Coppola

Conversion of Peanut Oil into Jet and Diesel Fuels. Panama City, Florida 22 July 2016 Edward N. Coppola Conversion of Peanut Oil into Jet and Diesel Fuels Panama City, Florida 22 July 2016 Edward N. Coppola SOLVING PROBLEMS OF GLOBAL IMPORTANCE About ARA, Inc. Founded 1979, Albuquerque, New Mexico 1,086

More information

Oil & Gas. From exploration to distribution. Week 3 V19 Refining Processes (Part 1) Jean-Luc Monsavoir. W3V19 - Refining Processes1 p.

Oil & Gas. From exploration to distribution. Week 3 V19 Refining Processes (Part 1) Jean-Luc Monsavoir. W3V19 - Refining Processes1 p. Oil & Gas From exploration to distribution Week 3 V19 Refining Processes (Part 1) Jean-Luc Monsavoir W3V19 - Refining Processes1 p. 1 Crude Oil Origins and Composition The objective of refining, petrochemical

More information

Petroleum Refining Fourth Year Dr.Aysar T. Jarullah

Petroleum Refining Fourth Year Dr.Aysar T. Jarullah Catalytic Operations Fluidized Catalytic Cracking The fluidized catalytic cracking (FCC) unit is the heart of the refinery and is where heavy low-value petroleum stream such as vacuum gas oil (VGO) is

More information

Sensitivity analysis and determination of optimum temperature of furnace for commercial visbreaking unit

Sensitivity analysis and determination of optimum temperature of furnace for commercial visbreaking unit ISSN : 0974-7443 Sensitivity analysis and determination of optimum temperature of furnace for commercial visbreaking unit S.Reza Seif Mohaddecy*, Sepehr Sadighi Catalytic Reaction Engineering Department,

More information

Characterization of crude:

Characterization of crude: Crude Oil Properties Characterization of crude: Crude of petroleum is very complex except for the lowboiling components, no attempt is made by the refiner to analyze for the pure components that contained

More information

Product Loss During Retail Motor Fuel Dispenser Inspection

Product Loss During Retail Motor Fuel Dispenser Inspection Product Loss During Retail Motor Fuel Dispenser Inspection By: Christian Lachance, P. Eng. Senior Engineer - ment Engineering and Laboratory Services ment Canada Date: Product Loss During Retail Motor

More information

National Oil Corporation Libyan Petroleum Institute. Crude oil assay Sarir crude oil

National Oil Corporation Libyan Petroleum Institute. Crude oil assay Sarir crude oil National Oil Corporation Libyan Petroleum Institute Crude oil assay Sarir crude oil Work Order No. LPI- 00344/10/IL02/2008 Client: National Oil Corporation Date of Issue: Dec., 2008 Prepared by: Industrial

More information

Atmospheric Crude Tower with Aspen HYSYS V8.0

Atmospheric Crude Tower with Aspen HYSYS V8.0 Atmospheric Crude Tower with Aspen HYSYS V8.0 1. Lesson Objectives Assign petroleum assay to stream Configure column pre-heater Configure crude tower 2. Prerequisites Aspen HYSYS V8.0 Introduction to distillation

More information

National Oil Corporation Libyan Petroleum Institute. Crude Oil Assay Messla Crude Oil

National Oil Corporation Libyan Petroleum Institute. Crude Oil Assay Messla Crude Oil National Oil Corporation Libyan Petroleum Institute Crude Oil Assay Messla Crude Oil Work Order No. LPI- 00344/08/IL02/2008 Client: National Oil Corporation Date of Issue: Nov., 2008 Prepared by: Industrial

More information

Quenching Our Thirst for Clean Fuels

Quenching Our Thirst for Clean Fuels Jim Rekoske VP & Chief Technology Officer Honeywell UOP Quenching Our Thirst for Clean Fuels 22 April 2016 Petrofed Smart Refineries New Delhi, India UOP 7200-0 2016 UOP LLC. A Honeywell Company All rights

More information

Preface... xii. 1. Refinery Distillation... 1

Preface... xii. 1. Refinery Distillation... 1 Preface... xii Chapter Breakdown... xiii 1. Refinery Distillation... 1 Process Variables... 2 Process Design of a Crude Distillation Tower... 5 Characterization of Unit Fractionation... 11 General Properties

More information

Changes to America s Gasoline Pool. Charles Kemp. May 17, Baker & O Brien, Inc. All rights reserved.

Changes to America s Gasoline Pool. Charles Kemp. May 17, Baker & O Brien, Inc. All rights reserved. Changes to America s Gasoline Pool Charles Kemp May 17, 2016 Baker & O Brien, Inc. All rights reserved. Discussion Points Light Naphtha Definitions Sources and Uses of Light Naphtha Octane Challenges Tier

More information

Commercial installations : BP Lavera steam cracker, France, BP Grangemouth (UK), COPENE Camaçari (Brazil) and a number of undisclosed plants.

Commercial installations : BP Lavera steam cracker, France, BP Grangemouth (UK), COPENE Camaçari (Brazil) and a number of undisclosed plants. ETHYLENE PLANTS provide optimization systems with timely and accurate quality information. Analysis of naphtha feeds to the furnaces, computing every 30 seconds : specific gravity, molecular weight, PIONA

More information

Simulation studies of Naphtha Splitter unit using Aspen Plus for improved product quality

Simulation studies of Naphtha Splitter unit using Aspen Plus for improved product quality Simulation studies of Naphtha Splitter unit using Aspen Plus for improved product quality Pranab K Rakshit*, AbhijeetNeog # *Corporate R&D Center, Bharat Petroleum Corporation Ltd, Greater Noida 201306

More information

SIMULATION AND OPTIMIZATION OF GASOLINE BLENDING IN A NIGERIAN PETROLEUM REFINING COMPANY.

SIMULATION AND OPTIMIZATION OF GASOLINE BLENDING IN A NIGERIAN PETROLEUM REFINING COMPANY. GSJ: VOLUME 6, ISSUE 3, MARCH 2018 7 GSJ: Volume 6, Issue 3, March 2018, Online: ISSN 2320-9186 SIMULATION AND OPTIMIZATION OF GASOLINE BLENDING IN A NIGERIAN PETROLEUM REFINING COMPANY. JOHN T. IMINABO,

More information

OIL REFINERY PROCESSES

OIL REFINERY PROCESSES OIL REFINERY PROCESSES 1 Types of hydrocarbons Types of hydrocarbons (parafffins, naphthenes, and aromatics). This rating is important to the refinery since the value of the crude oil decreases from classification

More information

Study on Relative CO2 Savings Comparing Ethanol and TAEE as a Gasoline Component

Study on Relative CO2 Savings Comparing Ethanol and TAEE as a Gasoline Component Study on Relative CO2 Savings Comparing Ethanol and TAEE as a Gasoline Component Submitted by: Hart Energy Consulting Hart Energy Consulting 1616 S. Voss, Suite 1000 Houston, Texas 77057, USA Terrence

More information

Energy Efficiency and Greenhouse Gas Emission Intensity of Petroleum Products at U.S. Refineries

Energy Efficiency and Greenhouse Gas Emission Intensity of Petroleum Products at U.S. Refineries Energy Efficiency and Greenhouse Gas Emission Intensity of Petroleum Products at U.S. Refineries Amgad Elgowainy, a Jeongwoo Han, a Hao Cai, a Michael Wang, a Grant S. Forman, b Vincent B. DiVita c a Systems

More information

Approach to simulation of phase behavior

Approach to simulation of phase behavior Approach to simulation of phase behavior Classical approach Assay analysis Based on TBP, API gravity, Distillation behavior Water solubility by special correlations Presentation at CEN/TC19/WG21/TF E85,

More information

R&D on New, Low-Temperature, Light Naphtha Isomerization Catalyst and Process

R&D on New, Low-Temperature, Light Naphtha Isomerization Catalyst and Process 2000M1.1.2 R&D on New, Low-Temperature, Light Naphtha Isomerization Catalyst and Process (Low-temperature isomerization catalyst technology group) Takao Kimura, Masahiko Dota, Kazuhiko Hagiwara, Nobuyasu

More information

Reducing octane loss - solutions for FCC gasoline post-treatment services

Reducing octane loss - solutions for FCC gasoline post-treatment services Reducing octane loss - solutions for FCC gasoline post-treatment services Claus Brostrøm Nielsen clbn@topsoe.com Haldor Topsoe Agenda Why post-treatment of FCC gasoline? Molecular understanding of FCC

More information

Fig:1.1[15] Fig.1.2 Distribution of world energy resources. (From World Energy Outlook 2005, International Energy Agency.)[16,17]

Fig:1.1[15] Fig.1.2 Distribution of world energy resources. (From World Energy Outlook 2005, International Energy Agency.)[16,17] Introduction :Composition of petroleum,laboratory tests,refinery feedstocks and products Fig:1.1[15] Fig.1.2 Distribution of world energy resources. (From World Energy Outlook 2005, International Energy

More information

HQCEC has contracted KBC to obtain an assessment of future market and market pricing. The market study results have been used as the basis of study.

HQCEC has contracted KBC to obtain an assessment of future market and market pricing. The market study results have been used as the basis of study. 3 STUDY BASIS 3.1 Production goals of the refinery SERESCO is studying the feasibility of expanding the Refinery, and the associated utilities to support a capacity of 400 m 3 /h (60,000 barrels per day

More information

D 5966 Roller Follower Wear Test. Final Report Cover Sheet. Report Packet Version No. Conducted For:

D 5966 Roller Follower Wear Test. Final Report Cover Sheet. Report Packet Version No. Conducted For: Final Report Cover Sheet Report Packet Version No. Conducted For: V = Valid I = Invalid Test Stand Stand Run Engine Engine Run A Alternate Codes Time Completed In my opinion this test been conducted in

More information

Remote Process Analysis for Process Analysis and Optimization

Remote Process Analysis for Process Analysis and Optimization Remote Process Analysis for Process Analysis and Optimization Gregory Shahnovsky gregorys@modcon-systems.com +44-208-1447904 Amir Or Amir_or@galil-eng.co.il +972-528785252 The Challenges Ahead The worldwide

More information

On-Line NIR Analysis of Crude Distillation Unit

On-Line NIR Analysis of Crude Distillation Unit Application Note On-Line NIR Analysis of Crude Distillation Unit Introduction Petroleum refining is the process of separating the many compounds present in crude petroleum. The principle which is used

More information

Advantages of Using Raman. Spectroscopy to Monitor Key. Gasoline Blending Parameters

Advantages of Using Raman. Spectroscopy to Monitor Key. Gasoline Blending Parameters Advantages of Using Raman Spectroscopy to Monitor Key Standards Certification Education & Training Publishing Conferences & Exhibits Gasoline Blending Parameters Presenter : Lee Smith, PhD President -

More information

Test Method D5967 Mack T-8. Version. Method: Conducted For

Test Method D5967 Mack T-8. Version. Method: Conducted For Method D5967 Mack T-8 Version Method: Conducted For T-8A: T-8: T-8E: V = Valid I = Invalid N = Not Interpretable The Reference Oil/Non-Reference Oil was evaluated in accordance with the test procedure.

More information

Sweeny to Pasadena Pipeline

Sweeny to Pasadena Pipeline click on product information to go to associated specification Spec Ref. # 8301 Product Name Distillate, Jet A, High Sulfur (3000 ppm ) Destination(s) Colonial PL- Grade 54; Explorer PL- Code 51; 8302

More information

UOP UNITY Hydrotreating Products

UOP UNITY Hydrotreating Products Satyam Mishra UOP UNITY Hydrotreating Products 19 February 2018 Honeywell UOP ME-TECH Seminar Dubai, UAE UOP 8080A-0 2018 UOP LLC. A Honeywell Company All rights reserved. Outline 1 Unity UNITY UOP Unity

More information

Report. Refining Report. heat removal, lower crude preheat temperature,

Report. Refining Report. heat removal, lower crude preheat temperature, Delayed coker FCC feed hydrotreater FCCU Crude unit Hydrotreater Hydrotreater P r o c e s s i n g Better fractionation hikes yields, hydrotreater run lengths Scott Golden Process Consulting Services Houston

More information

Refining/Petrochemical Integration A New Paradigm. Anil Khatri, GTC Technology Coking and CatCracking Conference New Delhi - October 2013

Refining/Petrochemical Integration A New Paradigm. Anil Khatri, GTC Technology Coking and CatCracking Conference New Delhi - October 2013 Refining/Petrochemical Integration A New Paradigm Anil Khatri, GTC Technology Coking and CatCracking Conference New Delhi - October 2013 Presentation Themes Present integration schemes focus on propylene,

More information

Distillation process of Crude oil

Distillation process of Crude oil Distillation process of Crude oil Abdullah Al Ashraf; Abdullah Al Aftab 2012 Crude oil is a fossil fuel, it was made naturally from decaying plants and animals living in ancient seas millions of years

More information

Testing Catalyst Additives for Sulfur Reduction in Cat-Naphtha

Testing Catalyst Additives for Sulfur Reduction in Cat-Naphtha Testing Catalyst Additives for Sulfur Reduction in Cat-Naphtha María Paz Chiavarino Axion Energy FCC Process Engineer Collaboration: Uriel Navarro Uribe PhD in W. R. Grace & Co Tech Service Kick Off Maximum

More information

Effects of Ethanol Blends on Light-Duty Vehicle Emissions: A Critical Review

Effects of Ethanol Blends on Light-Duty Vehicle Emissions: A Critical Review Effects of Ethanol Blends on Light-Duty Vehicle Emissions: A Critical Review FINAL REPORT 24 December 2018 Completed for Urban Air Initiative Study Team: Nigel Clark, Consultant Terry Higgins, Consultant,

More information

Paragon Scientific Ltd Proficiency Testing Scheme Schedule

Paragon Scientific Ltd Proficiency Testing Scheme Schedule Paragon Scientific Ltd Proficiency Testing Scheme Schedule Proficiency Testing Scheme Schedule Page 1 of 16 Issue : 29/01/2015 Print : 25/06/2018 Viscosity ASTM D445 - Standard Test Method for Kinematic

More information

Conversion Processes 1. THERMAL PROCESSES 2. CATALYTIC PROCESSES

Conversion Processes 1. THERMAL PROCESSES 2. CATALYTIC PROCESSES Conversion Processes 1. THERMAL PROCESSES 2. CATALYTIC PROCESSES 1 Physical and chemical processes Physical Thermal Chemical Catalytic Distillation Solvent extraction Propane deasphalting Solvent dewaxing

More information

On Purpose Alkylation for Meeting Gasoline Demand

On Purpose Alkylation for Meeting Gasoline Demand On Purpose Alkylation for Meeting Gasoline Demand Matthew Clingerman MERTC Annual Meeting, Bahrain 23 rd 24 th January 2017 DuPont Clean Technologies www.cleantechnologies.dupont.com Copyright 2017 E.

More information

Fundamentals of Petroleum Refining Refinery Products. Lecturers: assistant teachers Kirgina Maria Vladimirovna Belinskaya Natalia Sergeevna

Fundamentals of Petroleum Refining Refinery Products. Lecturers: assistant teachers Kirgina Maria Vladimirovna Belinskaya Natalia Sergeevna Fundamentals of Petroleum Refining Refinery Products Lecturers: assistant teachers Kirgina Maria Vladimirovna Belinskaya Natalia Sergeevna 1 Refinery Products Composition There are specifications for over

More information

TYPES OF BLENDING PROCESS

TYPES OF BLENDING PROCESS SYSTEMS LTD Blending operations became a major strategy as an answer to the ever-growing competitions between refineries. The strategy of blending crude oils and refinery products is to increase refining

More information

Balancing the Need for Low Sulfur FCC Products and Increasing FCC LCO Yields by Applying Advanced Technology for Cat Feed Hydrotreating

Balancing the Need for Low Sulfur FCC Products and Increasing FCC LCO Yields by Applying Advanced Technology for Cat Feed Hydrotreating Balancing the Need for Low Sulfur FCC Products and Increasing FCC LCO Yields by Applying Advanced Technology for Cat Feed Hydrotreating Brian Watkins Technical Service Engineer Advanced Refining Technologies

More information

एमआरप एल ग णव नय ण य गश ल उप दन व श:२०१७ MRPL QC LABORATORY

एमआरप एल ग णव नय ण य गश ल उप दन व श:२०१७ MRPL QC LABORATORY एमआरप एल ग णव नय ण य गश ल उप दन व श:२०१७ MRPL QC LABORATORY PRODUCTS SPECIFICATIONS:2017 INDIAN STANDARD (IS) SPECIFICATIONS FOR DOMESTIC PRODUCTS: 2017 S.No Product Name Specification Number 1 Liquefied

More information

The purpose of this rule is to limit VOC emissions from the transfer of organic liquids.

The purpose of this rule is to limit VOC emissions from the transfer of organic liquids. RULE 4624 TRANSFER OF ORGANIC LIQUID (Adopted April 11, 1991; Amended September 19, 1991; Amended May 21, 1992; Amended December 17, 1992; Amended December 20, 2007) 1.0 Purpose The purpose of this rule

More information

Tung Xiao Dan Assistant Chemist Mark Tan Section Head Feedstock Evaluation Department

Tung Xiao Dan Assistant Chemist Mark Tan Section Head Feedstock Evaluation Department Sample ID : Lab ID : Date : Client : Chim Sao Crude 2014-FED-051699 01 October 2014 Premier Oil Sample Number : Sample Date : Sample Time : Location : 4/4 10/9/2014 1500hrs Run Down Reported by : Approved

More information

REFINING SOLUTIONS IN A CHANGING WORLD RFG, RFS, SULFUR, BENZENE, TIER 3 AND BEYOND

REFINING SOLUTIONS IN A CHANGING WORLD RFG, RFS, SULFUR, BENZENE, TIER 3 AND BEYOND REFINING SOLUTIONS IN A CHANGING WORLD RFG, RFS, SULFUR, BENZENE, TIER 3 AND BEYOND Thomas R. Hogan, P.E. Senior Vice President January 22, 2015 Turner, Mason & Company Privately held established 1971

More information

AlkyClean Solid Acid Alkylation

AlkyClean Solid Acid Alkylation Development of a Solid Acid Catalyst Alkylation Process AlkyClean Solid Acid Alkylation October 6, 2006-1 - AlkyClean solid acid alkylation Presentation Outline Introduction Process Development Demonstration

More information

Smoke Point Significance and Use

Smoke Point Significance and Use Smoke Point The maximum height, in millimetres, of a smokeless flame of fuel burned in a wick-fed lamp of specified design. The sample is burned in an enclosed wick-fed lamp that is calibrated against

More information

Recycle and Catalytic Strategies for Maximum FCC Light Cycle Oil Operations

Recycle and Catalytic Strategies for Maximum FCC Light Cycle Oil Operations Recycle and Catalytic Strategies for Maximum FCC Light Cycle Oil Operations Ruizhong Hu, Manager of Research and Technical Support Hongbo Ma, Research Engineer Larry Langan, Research Engineer Wu-Cheng

More information

Composition distribution and characteristic of a typical commercial gasoline in market

Composition distribution and characteristic of a typical commercial gasoline in market International Journal of Smart Grid and Clean Energy Composition distribution and characteristic of a typical commercial gasoline in market Li Na, Guo Xin, Tao Zhiping, Long Jun Research Institute of Petroleum

More information

Potential Environmental and Economic Benefit s of Higher-Oct ane Gasoline

Potential Environmental and Economic Benefit s of Higher-Oct ane Gasoline Potential Environmental and Economic Benefit s of Higher-Oct ane Gasoline Raymond Speth, Eric Chow, Robert Malina, Steven Barrett, J ohn Heywood, W illiam Green CRC W orkshop, Argonne National Laboratory

More information

Optimizing Distillate Yields and Product Qualities. Srini Srivatsan, Director - Coking Technology

Optimizing Distillate Yields and Product Qualities. Srini Srivatsan, Director - Coking Technology Optimizing Distillate Yields and Product Qualities Srini Srivatsan, Director - Coking Technology Email: srini.srivatsan@amecfw.com Optimizing Distillate Yields and Product Properties Overview Delayed coker

More information

A Balanced Approach to Octane Replacement

A Balanced Approach to Octane Replacement A Balanced Approach to Octane Replacement Policy Development Meeting on Clean Fuels and Vehicles for the Middle East and North Africa 24 May 2006 Cairo, Egypt Lee Chook Khean Communications Director http://www.acfa.org.sg

More information

Refinery Feedstocks & Products Properties & Specifications

Refinery Feedstocks & Products Properties & Specifications Refinery Feedstocks & Products Properties & Specifications Gases Gas Sat Gas Plant Polymerization LPG Sulfur Plant Sulfur Alkyl Feed Alkylation Butanes Fuel Gas LPG Gas Separation & Stabilizer Light Naphtha

More information

The Role of a New FCC Gasoline Three-Cut Splitter in Transformation of Crude Oil Hydrocarbons in CRC

The Role of a New FCC Gasoline Three-Cut Splitter in Transformation of Crude Oil Hydrocarbons in CRC 8 The Role of a New FCC Gasoline Three-Cut Splitter in Transformation of Crude Oil Hydrocarbons in CRC Hugo Kittel, Ph.D., Strategy and Long Term Technical Development Manager tel. +0 7 80, e-mail hugo.kittel@crc.cz

More information

Process Analyzer. Reid Vapor Pressure Analyzer Model P-700. Credible Solutions for the Oil and Gas Industry

Process Analyzer. Reid Vapor Pressure Analyzer Model P-700. Credible Solutions for the Oil and Gas Industry Process Analyzer Reid Vapor Pressure Analyzer Model P-700 Credible Solutions for the Oil and Gas Industry Reid Vapor Pressure Process Analyzer Model P-700 Analyzer To remain competitive, today s refiners

More information

A Theoretical Study in Maximizing Crude Unit Kerosene

A Theoretical Study in Maximizing Crude Unit Kerosene A Theoretical Study in Maximizing Crude Unit Kerosene Introduction W. Doug McDaniel, MPEC, Inc., Feb. 26, 2014, Ver. 1 (email address: wdmcdaniel@mpec-inc.com) Not long ago I was asked how low the D-86

More information

Canadian Bitumen and Synthetic Crudes

Canadian Bitumen and Synthetic Crudes Understanding the Quality of Canadian Bitumen and Synthetic Crudes Pat Swafford Spiral Software Limited Crude Oil Quality Group Meeting February 26, 2009 Introduction Canadian crude production is increasing

More information

LOW TEMPERATURE OPERABILITY STARTABILITY & CHARACTERISTICS

LOW TEMPERATURE OPERABILITY STARTABILITY & CHARACTERISTICS ENGINE OIL TESTS LOW TEMPERATURE OPERABILITY STARTABILITY & CHARACTERISTICS The ability of an engine oil to flow or be pumped at low temperatures especially at start up is critical to the life of an engine.

More information

Replacing the Volume & Octane Loss of Removing MTBE From Reformulated Gasoline Ethanol RFG vs. All Hydrocarbon RFG. May 2004

Replacing the Volume & Octane Loss of Removing MTBE From Reformulated Gasoline Ethanol RFG vs. All Hydrocarbon RFG. May 2004 Replacing the Volume & Octane Loss of Removing MTBE From Reformulated Gasoline Ethanol RFG vs. All Hydrocarbon RFG May 2004 Prepared and Submitted by: Robert E. Reynolds President Downstream Alternatives

More information

FUELS. Product Specifications

FUELS. Product Specifications FUELS Product Specifications This Lesson Is Designed: To provide you with an understanding of specifications and terms used in the marketing of fuels. To show you how to use the information contained in

More information

D ISM Lubricant Performance Test. Report Packet Version No. Method. Conducted For:

D ISM Lubricant Performance Test. Report Packet Version No. Method. Conducted For: D 7468 - ISM Lubricant Performance Test Report Packet Version No. Method Conducted For: V = I = N = Valid; The reference oil / non-reference oil was evaluated in accordance with the test procedure. Invalid;

More information

Regional Laboratory, Indian Oil Corporation Limited, Korukkupet Terminal, Kathivakkam High Road, Chennai, Tamil Nadu

Regional Laboratory, Indian Oil Corporation Limited, Korukkupet Terminal, Kathivakkam High Road, Chennai, Tamil Nadu Regional, Indian Oil Corporation Limited, Korukkupet Last Amended on 07.01.2014 Page 1 of 5 Specific Method Specification against Range of ing / I. PETROLEUM PRODUCTS 1. JetA1, JP5 Acidity, Total P-113

More information

Chapter 11 Gasoline Production

Chapter 11 Gasoline Production Petroleum Refining Chapter 11: Gasoline Production Chapter 11 Gasoline Production INTRODUCTION Convert SR naphtha to motor gasoline stocks through 1. Reforming 2. Isomerization Production of motor gasoline

More information

Small GTL A New Midstream Opportunity

Small GTL A New Midstream Opportunity Small GTL A New Midstream Opportunity March 4, 2014 Mark Agee VP Business Development Some Definitions: In this presentation, GTL (Gas-To-Liquids) refers to the conversion of natural gas into hydrocarbon

More information

CRUDE DISTILLATION. Overview. Purpose To recover light materials. Fractionate into sharp light fractions.

CRUDE DISTILLATION. Overview. Purpose To recover light materials. Fractionate into sharp light fractions. Overview Purpose To recover light materials. Fractionate into sharp light fractions. CRUDE DISTILLATION Configuration May be as many as three columns in series Crude Stabilizer/Preflash Column Reduce traffic

More information

Analysis of gas condensate and its different fractions of Bibiyana gas field to produce valuable products

Analysis of gas condensate and its different fractions of Bibiyana gas field to produce valuable products Available online at www.banglajol.info Bangladesh J. Sci. Ind. Res. 50(1), 59-64, 2015 Analysis of gas condensate and its different fractions of Bibiyana gas field to produce valuable products S. M. A.

More information

Optimization of Motor Gasoline Production

Optimization of Motor Gasoline Production Optimization of Motor Gasoline Production Research Article 100 M.G.Diab 1, H.M. Mustafa 2, I.H. M.Elamin 3, G.A.Gasmelseed 4 (1-4) Department of Chemical Engineering, Faculty of Engineering, University

More information

Synthetic Fuel Formulation from Natural Gas via GTL: A Synopsis and the Path Forward

Synthetic Fuel Formulation from Natural Gas via GTL: A Synopsis and the Path Forward Synthetic Fuel Formulation from Natural Gas via GTL: A Synopsis and the Path Forward Elfatih Elmalik 1,2, Iqbal Mujtaba 1, Nimir Elbashir 2 1 University of Bradford, UK 2 Texas A&M University at Qatar

More information