Boiling point distribution of crude oils based on TBP and ASTM D

Transcription

Petroleum & Coal
ISSN 1337-7027
Available online at www.vurup.sk/petroleum-coal
Petroleum & Coal 53 (4) 275-290, 2011
BOILING POINT DISTRIBUTION OF CRUDE OILS BASED
ON TBP AND ASTM D-86 DISTILLATION DATA
Angel Nedelchev, Dicho Stratiev, Atanas Ivanov, Georgy Stoilov
Lukoil Neftochim Bourgas – Chief Process Engineer Department, 8104 Bourgas,
Bulgaria, Nedelchev.Angel.D@neftochim.bg, Stratiev.Dicho@neftochim.bg
Received July 4, 2011, Accepted October 15, 2011
Abstract
The True Boiling Point (TBP) analysis according to ASTM D-2892 standard is the single
reliable tool for characterization of crude oil and petroleum mixtures in terms of their boiling
point distribution. However, the analytical procedure is expensive and time consuming, which
is inappropriate for quick estimation of crude oil distillation characteristics. Thirty three
crude oil samples were characterized by means of TBP distillation and ASTM D-86. This
paper presents an attempt to test the applicability of the major methods available in the
open literature for converting ASTM D-86 to TBP for the whole range of the distillation
curve. The whole distillation curve was obtained by using the Riazi’s distribution model
((Ti-To)/To=[АT/ВT.Ln( 1/(1-xi))]1/BT), which demonstrated high accuracy with r2 ≥ 0.99.
All methods demonstrated lower accuracy in converting the ASTM D-86 into TBP than the
reproducibility of the ASTM D-2892.
Key words: crude oil, true boiling point, distillation, ASTM D-2892, ASTM D-86.
1. Introduction
Having in mind that crude oil cost accounts for more than 80% of refinery
expenditure the proper operation of crude distillation unit has great impact on
refinery profitability. In order to find the adequate technological regime that
provides maximum yields of high value products in a crude distillation unit the
process engineer needs to have laboratory analyses data of crude oil that is
processed in the unit. The True boiling point distillation (TBP) is the single most
important information for any crude oil for modeling of a crude distillation column.
The TBP distillation tends to separate the individual mixture components relatively
sharply in order of boiling point and is a good approximation of the separation
that may be expected in the plant. Unfortunately the TBP analyses are costly and
time consuming, a TBP analysis takes about 48 hours. That is why it is impractical
to use it as a tool for daily monitoring of the crude distillation unit operation. For
refineries, which often switch the crude oils the lack of information about the crude
oil quality could negatively impact the optimum operation and in this way the
profitability of the crude distillation unit. It was found that boiling point distribution
of crude oils and oil fractions obey the Riazi’s distribution model [1]:
Ti T0
T0
AT
1
ln
BT
1 xi
1 / BT
(1)
Equation 1 can be converted into a linear form :
Y
(2)
C1 C2 . X
where: Y
ln
T
T0
T0
;
X
ln ln
1
1 xi
;
BT
1
; AT
C2
BT . exp(C1.BT )
A. Nedelchev, D. Stratiev, A.Ivanov, G. Stoilov/Petroleum & Coal, 53(4) 275-290, 011
276
To = initial boiling point in K; Ti = temperature at which i per cent is distilled in
K; xi = volume or weight part of distillate.
Equation 2 has been tested on several hundreds samples of different crude oils,
gas condensates, bitumen and oil fractions in the Lukoil Neftochim research laboratory
and has been proved to be valid for all tested samples. Figure 1 is an illustration
of validity of equation 2 applied to different distillation data of crude oil, straight
run atmospheric residue, visbreaker residue, and visbreaker diesel. Regardless of
the distillation method used (TBP, ASTM D-1160, ASTMD-5236, ASTM D-86,
ASTM D-2887 and distillation according to Bogdanov – GOST 10120) the boiling
point distribution is perfectly approximated by equations 1 and 2. It could be inferred
from these data that one can safely extrapolate distillation curve from a set of
data that does not cover the full distillation range of an oil. For example data of
TBP distillation of vacuum residue obtained in one of the Lukoil vacuum distillation
units is given in Table 1. Due to known limitation of the equipment the distillation
was performed for temperature not higher than 5400C. Figure 2 presents graph of
equation 2 applied for the data of Table 1. It is evident from these data that eq.2
perfectly describes the boiling point distribution of the vacuum residue (r2 = 0.9977).
Taking into account the proof of validity of equation 2 for the whole distillation range
we can build the vacuum residue TBP distillation curve (Figure 3) based on the
data for AT and BT extracted from Figure 2.
Table 1 Distillation characteristics of Atmospheric Residue from Ural Crude Oil
Properties
Atmospheric Residue
1. Density @ 20 °С, g /сm 3
2. TBP Distillation
0.9489
%
∑%
9.57
9.57
380-400°С
5.02
14.59
400-430°С
10.77
25.36
430-470°С
11.65
37.01
470-490°С
5.98
42.99
490- 540 °С
13.65
56.64
315-380°С
360-400°С
> 540 °С
Losses
42.34
0
Ln((Ti-To)/To)
-2.5
-2
-1.5
-1
-0.5
0
-0.5
y = 0.5806x - 0.8782
R2 = 0.9977
-1
-1.5
-2
-2.5
Ln(Ln(1/(1-xi))
Boiling Temperature, oC
1.02
1000
900
800
700
600
500
400
300
200
100
0
0
20
40
60
80
100
Distillate, wt.%
Fig. 2 Application of the Riazi’s model
(eq.2) for approximation of TBP distillation
curve of Atmospheric Residue from Ural
Crude Oil
Fig. 3 Full range TBP distillation curve
of Atmospheric Residue from Ural
Crude Oil obtained by the use of the
Riazi’s model (eq.2)
Following this way of thinking we decided to test applicability of equations 1 and 2
on ASTM D-86 distillation of 33 crude oil samples with the aim to build the whole
range (from 0 to 99%) crude ASTM D-86 distillation curve based on distillation data
boiling up to 3000C. The ASTM D-86 distillation is performed within 45 minutes
and for that reason it could be used for daily monitoring of the crude distillation
unit operation if the whole crude oil curve is available and it could be converted
into TBP. Further we tested the ability of the methods available in the open literature
for conversion of ASTM D-86 into TBP distillation of the crude oil samples investigated
in this study. The aim of this paper is to discuss the obtained results
2. Experimental
TBP distillation of all 33 investigated crude oil samples was carried out in the
AUTODEST 800 Fisher column according to АSTM-D 2892 for the atmosphere part
of the test and according to АSTM-D 5236 for the vacuum one. The TBP distillation
was performed in the AUTODEST 800 Fisher column at pressure drop from 760 to
2 mmHg and in the AUTODEST 860 Fisher column from 1 to 0, 2 mmHg. The results
of the TBP distillation of the studied crude oil samples are presented in Table 2.
Distillation of the 33 crude oil samples up to 3000C was performed in accordance
with ASTM D-86 and the results of the distillation are given in Table 3. The density at
200C was analyzed according to АSTM-D 1298.
3. Results and Discussions
Table 4 presents data of TBP distillation of the 33 crude oil samples estimated
on the base of the parameters AT and BT computed by eq.2 and assuming T0 =-11.70C,
which is the boiling point of isobutane. The isobutane is assumed to be the lightest
compound in a crude oil [1]. The squared correlation coefficient r2 for all crude oil
samples except that of the Light Siberian crude oil is above 0.99. For the Light
Siberian crude the r2 = 0.9898 which is also high enough. This implies that the
Riazi’s distribution model describes very well the TBP distillation curve of crude oil.
Table 5 presents data of ASTM D-86 distillation of the 33 crude oil samples
estimated on the base of the parameters AT and BT computed by eq.2. The squared
correlation coefficient r2 for all crude oil samples except that of the Buzachinmski
crude oil is above 0.99. For the Buzachinmski crude the r2 = 0.9751 which is also
high. This indicates that the Riazi’s distribution model also describes very well the
ASTM D-86 distillation curve of crude oil. It may be concluded that by the use of
calculated AT and BT and the initial boiling point the distillation curve could be
safely extrapolated to 99 vol.%. In other words by applying the Riazi’s distribution
model from ASTM D-86 distillation data of a crude oil boiling up to 300 0C it can be
estimated the amount of compounds boiling above this temperature and build the
full range distillation curve.
In order to examine the capabilities of the available in the open literature
correlations for conversion of ASTM D-86 into TBP distillation we had to convert
the TBP distillation data from weight % in volume % because all correlations
convert ASTM D-86 into TBP vol.%. Table VI presents data of TBP distillation of
the 33 crude oil samples in vol.% assuming constant Kw factor for all crude
fractions and using the data from Table 5. The squared correlation coefficient r 2
for this data set is above 0.99.
There is number of empirical approaches for converting ASTM D 86 distillations
to true boiling point (TBP) distillations. Three of them are the most applicable for
engineering purposes.
From chronological point of view the earliest method for conversion of the
distillation curves is the method of Edmister [2]. It is a graphical approach, which
was developed in the period 1948÷1961. First step in application of the method is
definition of the TBP 50% as a function of D 86 50% in Fahrenheit using the
graph that is illustrated in Figure 3.
277
278
Figure 3 Relationship between ASTM D 86 and TBP distillation curves developed
by Edmister and al. [2]
Next step requires making a graphical definition of the temperature differences
between the segments of ASTM D 86 distillation curve (0%÷10%; 10%÷30%;
30%÷50%; 50%÷70%; 70%÷90% and 90%÷100%) by means of the same graph.
These values are needed in order to define the correspondent temperature differences
in TBP. By means of defined temperature differences in TBP and TBP50%, which
is available in advance, it is easy to draw the TBP curve. Table VII illustrates the
corresponding values from Figure 3, which facilitate conversion procedure.
Riazi-Daubert method for the interconversion of ASTM D 86 distillations to TBP
distillations is based on the generalized correlation in the following form [3]:
TBP
a( ASTM
D86) b
(3)
where both TBP and ASTM temperatures are for the same vol.% distilled and
are in Kelvin. Constants a and b at various points along the distillation curve with
the range of application are given in Table 8.
Table 8 Correlation constants in eq. 3
vol%
0
10
30
50
70
90
95
a
0.9177
0.5564
0.7617
0.9013
0.8821
0.9552
0.8177
b
1.0190
1.0900
1.0425
1.0176
1.0226
1.0110
1.0355
range a, oC
20-320
35-305
50-315
55-320
65-330
75-345
75-400
279
Daubert and his group developed a different set of equations to convert ASTM
to TBP, which is also known as a Daubert’s method [3]. The following equation is
used to convert an ASTM D 86 distillation at 50% point temperature to a TBP
distillation 50% point temperature.
TBP(50%) 255.4 0.8851[ ASTM D86(50%) 255.4]1.0258
(4)
where ASTM (50%) and TBP (50%) are temperatures at 50% volume distilled
in Kelvin. Equation (4) can also be used in a reverse form to estimate ASTM from
TBP. The following equation is used to determine the difference between two cut
points:
Yi
AX iB
(5)
Where:
Yi = difference in TBP temperature between two cut points, K;
Xi = observed difference in ASTM D 86 temperature between two cut points, K;
A, B = constants varying for each cut point and are given in Table IX.
Table 9 Correlation constants in eq. 5
i
1
2
3
4
5
6
Cut point range,
%
100-90
90-70
70-50
50-30
10-30
10-0
A
B
0.1403
2.6339
2.2744
2.6956
4.1481
5.8589
1.6606
0.7550
0.8200
0.8008
0.7164
0.6024
To determine the true boiling point temperature at any percent distilled, calculation
should begin with 50% TBP temperature and addition or subtraction of the proper
temperature difference Yi.
TBP (0%) = TBP (50%) - Y4 - Y5 - Y6
TBP (10%) = TBP (50%) - Y4 - Y5
TBP (30%) = TBP (50%) - Y4
TBP (70%) = TBP (50%) + Y3
TBP (90%) = TBP (50%) + Y3+Y2
TBP (100%) = TBP (50%) + Y3 + Y2 + Y1
The three approaches for conversion of ASTM D 86 distillations to TBP distillations
were applied to the experimental data for 33 crude oil samples. Tables 10-12
present data of absolute deviation calculated as measured value – estimated
value. The data in tables X-XII indicate that all three methods of conversion of
ASTM D 86 distillation to TBP one used in this work: the Riazi-Daubert Conversion
Method, the Daubert Conversion Method and the Edmister Conversion Method do
not adequately predict TBP distillation from data of ASTM D-86 distillation data.
The maximum deviation in the boiling temperature for each per cent evaporate
should not go beyond 100C. No one of the conversion method used do not achieve
this requirement. Therefore, a new method for conversion of ASTM D 86 distillation to
TBP distillation applicable for crude oils should be developed.
4. Conclusions
It was found in this work that distribution of boiling point of the compounds
containing in 33 crude oil samples measured by TBP or ASTM D-86 can be approximated by the Riazi’s distribution model:
Ti T0
T0
AT
1
ln
BT
1 xi
1 / BT
This distribution model allows from incomplete distillation data the entire distillation
curve of a crude oil to be built regardless of the method used for measuring of the
distillation characteristics. On this base the entire distillation curve can be constructed
by the use of ASTM D-86 method for measuring of the evaporate boiling up to
300ºC. An attempt to apply the Riazi-Daubert Conversion Method, the Daubert
Conversion Method and the Edmister Conversion Method for converting ASTM D86 into TBP of the investigated crude oils was found to be unsuccessful. Therefore
a new method for conversion of ASTM D 86 distillation to TBP distillation applicable
for crude oils should be developed.
Reference
[1]
[2]
[3]
Riazi, M.R., “A Continuous Model for C7+ Fraction Characterization of
Petroleum Fluids”, Ind. Eng. Chem. Res., vol. 36 (10), 1997, pp 4299–4307.
Edmister, W.C., Pollock, D.H., “Phase Relations for Petroleum Fractions”,
Chem. Eng. Progr., vol. 44, 1948, pp. 905-926.
Riazi, M.R., “Characterization and Properties of Petroleum Fractions”,
American Society for Testing and Materials, 2005.
280
-3.5
-3.000
-1.000
Ln(Ln(1/1-xi))
-2.000
-1.500
-1.000
-0.500
0.000
0.000
0.500
1.000
1.000
-3
-2.5
-2
Ln(LN(1/(1-xi))
-1.5
-1
-0.5
ASTM D-1160 of Visbreaker Residue
-4.000
y = 0.4828x + 0.5452
R2 = 0.999
y = 0.6338x - 0.0972
R2 = 0.9925
Ln((Ti-To)/To)
-2.5
-2
-1.5
-1
-0.5
0
0
-3.5
-3.00
-2.00
-1.50
-1.00
-0.50
-2.5
-2
Ln(Ln(1/(1-xi)))
y = 0.8195x + 0.4739
R2 = 0.9934
-3
-1.5
GOST 10120 (Bogdanov) of
Visbreaker Residue
Ln(Ln(1/1-xi))
y = 0.5797x - 0.7879
R2 = 0.9998
-2.50
ASTM D-5236 of Atm.Residue
-2.5
-2
-1.5
-1
-0.5
0
-1
-2.50
-2.00
-1.50
-1.00
-0.50
0.00
0.00
-4
-3.5
-2
-1.5
-1
-0.5
0
-4
-3.5
-3
-2.5
-2
-1.5
-1
-0.5
0
-2
-1
0
-0.5
0
Ln(Ln(1/(1-xi)))
-3.5
-3
-2.5
-2
y = 0.5053x - 1.6827 -1
-1.5
R2 = 0.9897
-3
1
ASTM D-86 of Visbreaker Diesel
Ln(Ln(1/(1-xi)))
y = 0.7303x - 1.1788
R2 = 0.9993
-2.5
ASTM D-1160 of Atm.Residue
-3
2
0.5
Figure 1 Application of the Riazi’s model (eq.2) for approximation of distillation curves of different crude and crude oil fractions by
the use of different methods for measuring of distillation characteristics
Ln((Ti-To)/To)
Ln((Ti-To)/To)
Ln((Ti-To)/To))
Ln((Ti-To)/T0)
Ln((Ti-To)/To)
ASTM D-2892 of Crude Oil
281
TUN
TUAP
BUZ
LIB1
LIB2
GOS
SYR
LIR
LAR
HIR
AMCO
LSYR
KUW
IRQ
LSIB
ZAIK
TENG
HUR
UOR
KUM
URL
REM
LAZ
REBCO1
REBCO2
REBCO3
ABCO1
ABCO2
ABCO3
ABCO4
ABCO5
ABCO6
ABCO7
Crude Oil Sample
IBP-70
3.1
4.4
1.9
2.3
8.5
3.5
4.2
4.3
4.0
6.0
4.3
4.5
4.6
6.6
7.0
11.0
9.4
3.9
2.7
7.5
3.9
3.0
5.5
3.2
3.0
3.0
3.3
3.3
2.9
3.2
3.2
3.3
2.6
Table 2 TBP distillation of 33 crude oil samples
70-100
3.0
4.2
2.8
2.8
6.3
3.1
2.4
4.3
3.1
6.8
2.7
3.6
3.1
5.2
5.1
8.1
7.4
5.3
4.8
7.1
6.9
3.5
5.5
3.8
3.8
3.8
3.0
3.2
3.2
3.0
3.1
3.9
2.9
ASTM D 2892 / D 5236, wt.%
100-180
180-240
240-360
9.9
8.0
23.5
14.1
10.9
23.0
6.1
8.0
23.0
8.1
7.3
22.4
17.9
10.9
22.5
11.0
8.6
22.8
9.5
6.4
15.8
13.8
10.4
21.8
13.0
9.9
24.5
9.1
9.1
20.0
11.9
9.3
23.4
13.8
11.0
27.7
11.8
9.2
20.6
13.9
10.9
21.4
15.0
11.6
22.1
21.7
12.9
25.7
24.0
16.1
24.6
4.8
9.0
20.0
5.5
9.0
19.0
20.7
10.2
22.4
6.2
11.0
22.0
11.4
8.1
23.3
14.7
11.2
22.9
13.5
7.5
17.4
13.1
7.9
18.2
14.4
7.8
18.7
11.5
9.1
22.1
11.6
9.6
22.2
10.9
9.2
22.1
10.9
9.0
22.4
11.4
8.9
22.0
11.5
8.9
20.6
12.2
10.7
20.9
360-540
27.8
26.2
29.5
29.6
21.7
31.4
29.1
25.0
25.8
23.8
25.7
30.8
23.7
23.3
29.0
18.3
16.2
32.0
33.0
21.6
27.0
28.2
23.5
27.9
28.5
29.2
27.1
26.3
28.1
27.7
28.0
28.8
27.2
540+
24.8
17.2
28.7
27.6
14.3
19.6
32.4
20.6
19.8
26.7
22.8
9.5
27.1
18.7
12.8
5.3
2.4
25.0
26.0
13.3
23.0
22.5
16.7
28.2
26.8
24.6
23.9
23.9
23.7
23.8
23.4
23.1
23.5
282
TUN
TUAP
BUZ
LIB1
LIB2
GOS
SYR
LIR
LAR
HIR
AMCO
LSYR
KUW
IRQ
LSIB
ZAIK
TENG
HUR
UOR
KUM
URL
REM
LAZ
REBCO1
REBCO2
REBCO3
ABCO1
ABCO2
ABCO3
ABCO4
ABCO5
ABCO6
ABCO7
Crude Oil
Sample
62.0
40.0
60.0
61.0
40.0
61.0
55.0
33.0
30.0
46.0
51.0
30.0
30.0
44.0
28.0
40.0
35.0
50.0
47.0
50.0
51.0
47.0
60.0
53.0
30.0
25.0
62.0
60.0
51.0
53.0
47.0
58.0
62.0
IBP,
ºC
Up to
62ºC,
%vol.
3.0
3.0
1.0
3.5
2.0
2.0
1.5
2.0
3.0
2.0
3.0
4.0
7.0
1.5
2.0
2.0
2.0
1.0
1.0
0.5
1.5
2.5
0.5
1.0
1.5
-
Up to
85ºC,
%vol.
1.0
7.0
2.0
1.5
8.5
3.0
5.0
6.0
4.0
6.0
5.0
5.0
6.0
7.0
5.0
9.0
14.0
4.0
5.0
6.0
5.0
4.0
13.0
2.5
3.0
4.5
2.0
2.0
4.0
4.0
3.5
3.0
2.0
Up to
120ºC,
%vol.
4.0
13.0
7.0
5.0
18.0
10.0
10.0
12.5
11.0
12.0
10.0
10.0
12.0
14.0
13.0
19.0
25.0
9.0
9.0
11.0
11.0
10.0
20.0
9.0
8.0
9.5
8.0
7.0
10.0
9.0
8.5
8.0
8.0
Table 3 ASTM D-86 distillation of 33 crude oil samples
Up to
150ºC,
%vol.
10.0
20.0
8.0
10.0
27.0
15.0
14.0
19.0
17.0
19.0
16.0
16.0
18.0
21.0
20.0
30.0
34.0
13.5
14.0
20.0
17.0
15.0
28.0
13.0
13.0
14.5
13.0
12.0
15.0
14.0
14.0
13.0
13.0
ASTM D 86
Up to
180ºC,
%vol.
14.0
26.0
15.0
14.0
33.0
20.0
19.0
25.5
23.0
25.0
21.0
23.0
23.0
28.0
27.0
40.0
44.0
18.0
18.0
26.0
22.0
20.0
32.0
19.0
18.0
19.5
18.0
17.0
20.0
16.0
19.0
18.0
17.0
Up to
200ºC,
%vol.
17.0
29.0
17.0
17.0
39.0
24.0
21.0
30.0
29.0
28.0
25.5
27.0
26.5
32.0
31.0
43.0
49.0
22.0
21.0
29.0
26.0
24.0
35.0
23.0
21.5
23.0
22.0
21.0
24.0
22.0
22.5
22.0
21.0
Up to
240ºC,
%vol.
23.0
37.0
18.5
18.0
46.0
30.0
25.0
37.0
36.0
35.0
32.5
35.0
34.0
41.0
38.0
51.0
60.0
27.0
27.0
37.0
34.0
30.0
40.0
31.0
28.0
29.5
28.5
27.5
32.0
30.0
29.0
30.0
30.0
Up to
250ºC,
%vol.
25.0
40.0
26.0
25.0
48.0
32.0
26.0
38.5
39.0
37.0
34.0
37.0
35.5
43.0
40.0
53.0
62.0
29.0
29.0
40.0
36.0
32.0
42.0
33.0
30.5
31.0
30.5
30.0
34.0
32.0
31.0
32.0
31.0
Up to
300ºC,
%vol.
39.0
50.0
35.0
36.0
58.5
41.0
34.0
48.0
48.0
45.0
43.0
48.0
45.0
54.0
50.0
65.0
74.0
38.0
39.0
50.0
46.0
42.0
53.0
44.0
42.0
43.0
43.5
41.0
44.0
43.0
42.5
43.0
43.0
283
Tunesian
Tuapse
Buzachinmski
Libyan1
Libyan2
Gulf of Suetz
Syrian
Light Iranian
Light Arabian
Heavy Iranian
Arabian AMCO
Light Syrian
Kuwaitian
Iraqi
Light Siberrian
Zaikinski
Tengiz
Heavy Ural
Ural + Oil Residue
Kumkol
Ural
REM
Light Azerski
REBCO 02.12.09
REBCO 30.11.09
REBCO 10.11.09
Average Blend Sept.
Average
Blend Oct.
2007
Average
Blend Apr.
2007
Average
Blend May
2006
Average
Blend June
2006
Average
Blend July
2006
Average
Blend Sept.
2006
2006
Crude Oil Sample
5%wt.,
ºC
92
74
115
105
45
85
83
72
81
61
79
75
75
54
56
36
44
97
102
50
82
90
62
91
93
93
88
87
91
89
88
84
95
10%wt,
ºC
138
112
165
155
79
131
132
113
122
103
122
116
118
91
95
64
70
146
153
84
126
135
99
136
137
136
133
131
137
135
133
129
140
30%wt,
ºC
267
222
302
290
187
264
279
233
237
235
249
238
245
207
217
157
150
286
295
189
255
262
207
262
261
255
260
257
265
263
261
258
262
50%wt,
ºC
380
319
416
406
293
383
416
341
337
362
362
347
360
320
335
248
221
409
419
290
371
373
305
372
368
357
371
366
376
376
374
373
366
Table 4 TBP distillation data (wt.%) of the crude oils under study
70%wt,
ºC
507
428
542
536
424
521
577
466
451
517
494
473
494
455
479
361
304
550
559
411
503
499
420
497
488
469
506
491
502
504
503
505
482
90%wt,
ºC
710
605
738
740
650
745
845
671
633
782
708
679
715
688
725
557
440
776
783
616
720
700
610
695
678
647
703
690
703
710
709
719
665
95%wt,
ºC
813
695
836
843
773
861
987
777
725
924
819
786
830
812
857
664
511
892
898
725
831
803
708
796
774
736
807
792
806
816
815
829
757
0.998
0.998
5
0.991
2
0.997
8
0.994
9
0.997
1
0.994
3
0.995
2
0.999
1
0.993
5
0.999
8
0.985
1
0.999
6
0.997
7
0.989
7
0.980
8
0.997
2
0.999
4
0.999
3
0.987
4
0.997
1
0.995
0
0.997
9
0.991
7
0.992
3
0.990
9
0.998
2
0.998
6
0.997
2
0.998
5
0.998
8
0.995
0
0.994
8
2
R²
6.255
4.345
9
8.822
7
7.715
7
2.844
3
5.700
0
5.804
5
4.513
3
4.974
9
4.066
0
5.098
2
4.708
6
4.849
2
3.393
7
3.617
4
2.190
3
2.115
7
6.889
4
7.487
1
2.987
2
5.394
8
5.977
6
3.636
9
6.065
9
6.165
2
6.047
4
5.812
5
5.724
2
6.128
0
5.969
7
5.858
2
5.554
3
6.362
0
8
AT
1.963
1.922
1
2.137
3
2.046
2
1.550
2
1.845
9
1.724
4
1.817
7
1.958
2
1.594
1
1.833
4
1.830
2
1.790
8
1.607
2
1.595
2
1.532
4
1.809
8
1.916
3
1.956
8
1.639
6
1.850
1
1.951
8
1.785
2
1.970
4
2.013
1
2.066
3
1.927
1
1.939
9
1.961
9
1.931
2
1.921
6
1.870
2
2.062
6
7
BT
0.836
0.849
0
0.891
0
0.893
0
0.815
0
0.872
0
0.907
0
0.851
0
0.856
0
0.863
0
0.871
0
0.840
0
0.868
0
0.840
0
0.843
2
0.792
5
0.793
0
0.892
0
0.872
7
0.820
4
0.855
7
0.870
0
0.842
0
0.874
8
0.871
5
0.869
0
0.866
0
0.863
6
0.865
8
0.868
0
0.867
0
0.867
8
0.867
8
8
SG
284
Crude Oil Sample
IBP, ºC
Tunesian
62.0
Tuapse
40.0
Buzachinmski
60.0
Libyan1
61.0
Libyan2
40.0
Gulf of Suetz
61.0
Syrian
55.0
Light Iranian
33.0
Light Arabian
30.0
Heavy Iranian
46.0
Arabian AMCO
51.0
Light Syrian
30.0
Kuwaitian
30.0
Iraqi
44.0
Light Siberrian
28.0
Zaikinski
40.0
Tengiz
35.0
Heavy Ural
50.0
Ural + Oil Residue
47.0
Kumkol
50.0
Ural
51.0
REM
47.0
Light Azerski
60.0
REBCO 02.12.09
53.0
REBCO 30.11.09
30.0
REBCO 10.11.09
25.0
Average Blend Sept. 2007
62.0
Average Blend Oct. 2007
60.0
Average Blend Apr. 2006
51.0
Average Blend May 2006
53.0
Average Blend June 2006
47.0
Average Blend July 2006
58.0
62.0
5%, ºC
125
74
113
118
79
96
88
74
88
80
85
86
77
80
78
82
77
89
85
79
81
93
71
100
99
86
106
108
98
91
91
100
106
10%, ºC 30%, ºC 50%, ºC 70%, ºC 90%, ºC 95%, ºC R²
AT
BT
159
266
367
488
694
804
0.9947
2.0310
1.6455
101
200
312
462
746
910
0.9986
1.5188
1.2577
151
288
436
630
991
1195
0.9751
2.2415
1.3242
156
283
414
579
875
1038
0.9872
2.2370
1.4355
107
205
310
447
698
839
0.9973
1.5987
1.3510
125
234
361
533
864
1058
0.9975
1.5365
1.2167
121
272
470
767
1394
1787
0.9982
1.8817
1.0249
103
205
313
453
709
854
0.9956
1.7393
1.3613
118
211
298
402
576
668
0.9962
1.9856
1.6909
107
210
329
489
797
976
0.9994
1.5258
1.2285
113
229
366
557
935
1159
0.9974
1.6233
1.1633
118
216
309
423
615
718
0.9995
2.0544
1.6252
108
218
332
478
741
888
0.9996
2.0048
1.3994
105
194
290
415
645
774
0.9984
1.3819
1.3464
107
200
291
401
590
693
0.9927
1.8311
1.5755
113
222
339
492
775
935
0.9970
1.8076
1.3342
108
226
357
533
864
1055
0.9985
1.9420
1.2711
123
260
425
656
1116
1391
0.9955
1.9658
1.1486
119
261
435
683
1182
1483
0.9937
2.0027
1.1188
104
202
317
477
791
977
0.9938
1.3566
1.1762
108
221
358
555
951
1190
0.9909
1.5198
1.1178
124
233
346
492
756
904
0.9985
1.8309
1.3926
86
165
285
482
947
1259
0.9897
0.8934
0.8740
131
234
340
474
712
844
0.9979
1.7322
1.4438
135
244
346
467
669
776
0.9970
2.6454
1.7065
122
239
354
495
739
871
0.9978
2.6001
1.5489
136
240
349
490
746
889
0.9969
1.6127
1.3837
139
248
360
502
758
900
0.9993
1.7620
1.4194
127
224
321
443
657
775
0.9929
1.6335
1.4850
123
246
389
585
967
1192
0.9928
1.7925
1.1992
124
244
376
551
877
1064
0.9924
1.9437
1.2987
130
240
359
515
805
969
0.9973
1.6822
1.3222
136
240
350
491
747
890
0.9966
1.6208
1.3864
Table 5 ASTM D-86 distillation data of the crude oils under study
285
Tunesian
Tuapse
Buzachinmski
Libyan1
Libyan2
Gulf of Suetz
Syrian
Light Iranian
Light Arabian
Heavy Iranian
Arabian AMCO
Light Syrian
Kuwaitian
Iraqi
Light Siberrian
Zaikinski
Tengiz
Heavy Ural
Ural + Oil Residue
Kumkol
Ural
REM
Light Azerski
REBCO 02.12.09
REBCO 30.11.09
REBCO 10.11.09
Crude Oil Sample
80
64
104
92
37
73
70
62
71
50
68
64
64
45
46
29
39
83
89
42
70
79
53
79
82
82
75
75
79
73
75
73
84
5%, ºC
123
100
152
139
67
115
114
100
110
88
108
103
103
78
81
55
64
129
136
73
111
121
87
122
124
123
117
117
122
115
116
114
126
10%, ºC
246
205
282
268
167
241
251
212
219
209
227
217
222
186
194
141
140
262
270
171
233
241
188
242
242
237
238
236
244
238
239
235
243
30%, ºC
356
298
391
381
267
356
380
316
316
329
336
322
333
292
305
227
209
380
390
267
344
349
281
348
346
336
347
342
352
351
349
344
345
50%, ºC
Table 6 TBP distillation data (vol.%) of the crude oils under study
482
406
513
509
392
490
534
439
427
477
464
446
464
422
443
335
290
518
527
383
474
472
392
470
463
447
472
465
475
482
477
472
459
70%, ºC
685
581
704
713
612
712
795
642
607
735
675
649
683
647
682
525
423
741
749
583
688
671
576
667
651
624
677
664
676
697
686
680
642
90%, ºC
790
671
799
817
732
827
933
748
699
875
786
756
798
769
812
629
492
857
863
691
800
773
673
768
748
713
783
767
779
810
794
789
434
95%, ºC
R²
1.0000
1.0000
0.9996
1.0000
1.0000
1.0000
0.9999
1.0000
1.0000
1.0000
1.0000
1.0000
1.0000
1.0000
1.0000
1.0000
0.9999
1.0000
1.0000
1.0000
1.0000
1.0000
0.9991
1.0000
1.0000
1.0000
1.0000
1.0000
1.0000
0.9991
0.9999
0.9999
1.0000
AT
5.1384
3.6644
7.4595
6.2917
2.3729
4.6798
4.7000
3.7380
4.1985
3.3067
4.2019
3.9014
3.9778
2.8213
2.9786
1.8672
1.8922
5.5911
6.0835
2.5227
4.4260
4.9609
3.0262
5.0154
5.1327
5.0744
4.7382
4.7031
5.0436
4.6220
4.7156
4.5539
5.2928
BT
1.8779
1.8525
2.0921
1.9608
1.4928
1.7734
1.6628
1.7434
1.8936
1.5298
1.7627
1.7581
1.7153
1.5506
1.5347
1.4815
1.7721
1.8392
1.8801
1.5818
1.7749
1.8808
1.7241
1.8950
1.9410
1.9924
1.8389
1.8570
1.8825
1.7879
1.8205
1.8064
1.9829
286
0 to 10%
10 to
D-86 ºF TBP ºF D-86 ºF
0.27
0.27
0.27
1.37
4.37
2.74
3.01
8.19
5.21
6.03
13.92
10.14
8.49
19.65
16.71
11.23
25.11
21.10
14.52
30.29
26.03
18.08
36.57
29.59
22.19
42.85
33.15
27.12
49.95
38.36
30.96
55.14
42.74
35.07
60.33
46.85
39.73
66.61
50.69
43.56
71.79
54.52
47.12
76.44
58.90
50.69
81.35
63.01
56.16
87.90
68.49
61.10
93.09
72.05
66.03
99.65
75.34
70.41
105.65 75.34
75.62
111.39 90.14
81.37
117.94 94.25
85.21
123.40 97.81
89.04
128.04 102.47
106.85
110.41
114.79
119.45
124.93
Segment of Destillation
30%
30 - 50%
TBP ºF D-86 ºF TBP ºF
0.55
0.27
0.27
4.64
1.99
4.89
11.74
5.78
13.05
20.74
10.45
18.21
31.93
13.75
23.92
38.76
18.70
30.44
46.13
22.55
36.69
51.04
27.22
42.94
56.50
31.62
48.10
62.24
36.02
53.81
66.61
40.14
58.70
72.07
44.53
63.04
75.90
48.93
67.12
80.26
55.52
73.91
84.09
60.47
78.79
88.19
65.14
83.41
92.29
69.81
87.49
95.84
74.48
91.83
98.57
80.25
96.99
98.84
85.47 102.42
111.68 91.24 106.77
115.23 95.36 110.84
117.42 103.60 118.17
122.06 108.54 122.52
125.62 114.59 127.95
128.90 120.63 133.38
132.45 127.23 139.90
137.09 131.35 143.43
141.74 137.12 149.68
Curve, Volume Percent
50 - 70%
70 D-86 ºF TBP ºF D-86 ºF
0.55
1.09
0.28
3.58
8.16
4.13
3.30
7.07
12.10
7.97
12.50
17.87
20.89
31.52
23.09
29.14
42.12
28.31
33.54
46.74
32.98
38.21
52.99
39.03
45.35
59.50
43.97
53.32
67.65
51.12
58.82
73.36
59.36
64.86
79.88
64.30
71.45
85.31
69.52
77.22
90.47
76.12
87.11
98.88
83.26
92.88 104.59 90.95
99.20 110.02 96.45
105.79 116.54 98.92
113.76 123.60 104.69
120.35 129.84 111.01
125.30 134.73 118.70
131.07 140.17 125.57
135.46 145.05 130.24
140.68 149.40 137.11
144.81 154.56 142.60
150.58 161.08 147.00
157.72 167.33 150.30
162.39 173.85 153.87
167.62 182.00 156.34
Table 7 Edmister conversion data for transforming of ASTM D-86 into TBP
D-86 50% to TBP 50%
90%
90 to 100%
D-86 50% ºF TBP 50% ºF
TBP ºF D-86 ºF TBP ºF
0.82
0.55
1.09
101.70
-9.87
7.34
6.32
7.61
141.50
-8.75
17.66
14.29
16.30
199.15
-7.62
25.00
22.26
26.08
258.17
-5.66
30.43
30.23
33.41
310.33
-4.26
36.95
36.00
39.66
359.75
-2.32
41.30
41.77
44.82
416.04
-0.10
48.09
46.16
50.25
464.10
2.11
54.07
51.11
54.87
501.18
4.05
61.40
55.23
60.31
553.37
7.35
69.00
59.08
63.84
595.95
10.37
73.08
65.12
70.90
631.67
13.38
78.51
69.52
75.24
685.26
18.31
85.30
73.37
81.50
725.13
22.96
91.27
78.04
88.83
755.39
27.33
98.88
82.99
96.44
787.03
32.51
102.68 85.74 101.88
818.68
38.23
105.94 89.32 108.40
847.60
44.50
111.10 92.34 114.38
869.64
49.67
117.35 94.82 119.82
897.23
58.37
124.68 97.02 125.80
131.47
135.81
143.96
148.85
153.47
156.73
160.80
163.79
287
Tunesian
Tuapse
Buzachinmski
Libyan1
Libyan2
Gulf of Suetz
Syrian
Light Iranian
Light Arabian
Heavy Iranian
Arabian AMCO
Light Syrian
Kuwaitian
Iraqi
Light Siberrian
Zaikinski
Tengiz
Heavy Ural
Ural + Oil Residue
Kumkol
Ural
REM
Light Azerski
REBCO 02.12.09
REBCO 30.11.09
REBCO 10.11.09
Abs. average deviation, 0C
Crude Oil Sample
10%, ºC
Δ abs
17
15
20
2
24
8
10
13
9
3
12
2
11
11
10
41
28
23
34
15
19
15
16
9
7
18
1
4
13
9
10
2
8
13
30%, ºC
Δ abs
11
14
3
6
29
16
12
16
17
8
7
10
13
1
3
72
77
11
18
22
21
17
32
17
7
7
7
3
29
1
4
4
12
16
50%, ºC
Δ abs
11
13
46
34
42
5
92
4
19
1
30
14
2
3
15
112
148
46
46
49
14
3
3
8
0
18
2
18
32
38
27
15
5
28
Table 10 ASTM D-86 to TBP volume fraction according to Riazi-Daubert Conversion Method
70%, ºC
Δ abs
13
62
130
81
61
52
252
20
21
19
103
18
21
2
38
164
252
152
171
101
91
27
97
11
10
55
25
45
27
114
84
51
39
73
90%, ºC
Δ abs
27
185
317
187
105
177
647
86
17
84
288
19
78
15
77
271
466
411
471
230
292
106
399
64
35
135
89
115
2
299
217
148
125
187
95%, ºC
Δ abs
65
300
483
293
161
305
1003
162
9
167
457
6
149
54
77
369
637
641
736
353
477
191
679
131
77
215
165
193
45
469
345
246
515
308
288
Tunesian
Tuapse
Buzachinmski
Libyan1
Libyan2
Gulf of Suetz
Syrian
Light Iranian
Light Arabian
Heavy Iranian
Arabian AMCO
Light Syrian
Kuwaitian
Iraqi
Light Siberrian
Zaikinski
Tengiz
Heavy Ural
Ural + Oil Residue
Kumkol
Ural
REM
Light Azerski
REBCO 02.12.09
REBCO 30.11.09
REBCO 10.11.09
Crude Oil Sample
10%, ºC
Δ abs
30
8
12
23
29
8
38
6
7
13
7
3
1
12
12
53
45
10
3
22
2
2
14
1
4
4
12
17
6
14
10
13
4
13
30%, ºC
Δ abs
25
2
23
27
40
2
52
4
9
6
13
1
1
8
5
87
95
18
14
35
2
3
20
4
6
8
7
18
18
21
15
12
2
18
50%, ºC
Δ abs
23
23
62
48
52
17
109
6
10
10
42
4
9
6
6
123
160
61
61
59
26
8
12
3
11
30
13
30
21
52
40
27
16
36
Table 11 ASTM D-86 to TBP volume fraction according to Daubert Conversion Method
70%, ºC
Δ abs
13
54
110
70
56
38
197
14
18
8
83
17
14
5
37
155
237
120
134
89
69
21
74
7
10
50
20
39
27
93
69
42
34
61
90%, ºC
Δ abs
43
66
144
59
6
26
277
16
69
51
105
81
28
70
138
152
314
167
198
92
96
1
162
26
33
40
12
14
77
112
68
24
24
85
95%, ºC
Δ abs
197
644
1009
617
406
795
2992
423
95
582
1115
121
414
257
41
690
1106
1628
1917
807
1233
461
2010
339
199
417
415
437
207
1130
791
584
765
753
289
Tunesian
Tuapse
Buzachinmski
Libyan1
Libyan2
Gulf of Suetz
Syrian
Light Iranian
Light Arabian
Heavy Iranian
Arabian AMCO
Light Syrian
Kuwaitian
Iraqi
Light Siberrian
Zaikinski
Tengiz
Heavy Ural
Ural + Oil Residue
Kumkol
Ural
REM
Light Azerski
REBCO 02.12.09
REBCO 30.11.09
REBCO 10.11.09
Crude Oil Sample
30%, ºC
Δ abs
32
11
35
4
37
23
220
10
2
10
31
4
9
9
10
74
62
99
138
22
47
10
42
5
9
0
4
14
14
33
17
1
1
32
10%, ºC
Δ abs
21
26
123
51
20
36
359
22
3
16
67
1
31
14
13
21
21
184
241
3
72
28
32
11
11
43
3
5
8
83
58
20
12
50
Δ abs
38
32
90
72
60
31
147
15
2
20
57
4
20
13
1
134
173
87
90
68
40
20
18
14
23
43
26
44
12
70
56
41
29
48
50%, ºC
Table 12 ASTM D-86 to TBP volume fraction according to Edmister Conversion Method
Δ abs
83
192
488
282
154
273
1846
121
18
186
427
33
141
64
6
307
492
808
1016
266
452
149
449
101
77
165
134
158
38
474
322
207
148
305
70%, ºC
Δ abs
341
1152
2646
1362
726
1852
14812
757
141
1374
2925
215
828
459
137
1241
2159
5584
7247
1599
3368
867
5436
586
327
719
767
797
347
3058
1831
1207
803
2051
90%, ºC
Δ abs
557
2135
4682
2311
1279
3554
31528
1384
246
2646
5677
375
1478
850
275
2130
3821
10944
14418
3083
6770
1545
13497
1035
527
1181
1364
1382
638
5848
3343
2171
1714
4072
95%, ºC
290

Boiling point distribution of crude oils based on TBP and ASTM D

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