Refining-Petrochemicals-Chemicals-Engineering
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PRINCIPLES PRINCIPLES OF INITIAL I NITIAL FRACTIONATION OF CRUDE OILS
INT INTRODUCTION ION.......................................................................................................................................1 I - TBP ANALYS LYSIS............................................................................................................................... 1 II - THE THE DIFFE DIFFER RENT ENT PETRO TROLEUM LEUMCUTS CUTS...... ............ ........... ........... ............ ............ ............ ............ ............ ............ ............ ............ ............ ............ ........... .....3 3 1 2 3 4 5 6 7
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Fuel Fuel gas gas cut.............................. cut............................................................... .................................................................. ............................................................ ........................................ .............4 4 Propa Propane ne and and butane butane cuts....................... cuts....................................................... ................................................................ ............................................................ ............................4 4 Gasolines asolines and and naphth naphtha a cuts cuts............................. ............................................................. ............................................................... ................................................. ..................4 4 Keros Kerosen ene e cut cut ................................................................ ............................................................................................... ............................................................... ....................................... .......6 6 Gas oils or middle middle distillates................... distillates................................................... ................................................................ ........................................................... ........................... 7 Vacu Vacuum um gas oils............................... oils ................................................................ .................................................................. .............................................................. ................................ ...8 8 Vacu Vacuum um residue residue................................ ................................................................. .................................................................. ............................................................. ............................... ...9 9
III - CRU CRUDE OIL FRA FRACTIO CTIONA NATIO TION N SCHE CHEME............... E..................... ............ ............ ............ ............ ........... ........... ............ ............ ............ ............ .........10 ...10 IV - YIELD YIELDS S AND AND MAIN CHAR CHARAC ACTE TERIS RISTIC TICS S OF CRUD CRUDE E OILS........ ILS........... ...... ...... ...... ...... ...... ...... ...... ...... ...... ...... ...... ...... ...... ...... ...12 12 AP APPENDICE ICES: Charac racteri teris stic tics of some crud rude oils ils Figure 1: Figure 2: Figure 3: Figure 4: Figure 5: Figure 6: Figure 7: Figure 8: Figure 9:
Middle East North Sea - France North North Africa - West Africa West Africa Africa Latin Ameri America ca - North Ameri America ca Far-East - Oceania Oceania - Russia Typical Typical crude oil characteristi characteristics cs Typical Typical atmospheric atmospheric residues characterist characteristics ics Typical vacuum residue characteristi characteri stics cs
RA FIB - 00007_C_A 00007_C_A - Rev. 14
08/12/2008
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INTRODUCTION The first treatment undergone by crude oils in the re finery units is fractionation especially especially by distillation. This produces approximately a dozen petroleum cuts which ha ve volatilities volatilities close to those o f commercial products. In some cases, these cuts may be directly marketed or or used for the manufacture of finished products. They generally require chemi chemical transforma transformations tions : – either to improve their quality and meet requirements concerning specifications. Petroleum cuts are thus converted into bases which are blended to obtain the finished products – or to convert them in order to quantitatively satisfy market demands. Conversion treatments are applied to heavy cuts to transform them into light cuts. Conversion operations often produce a large range of hydrocarbons which are relatively similar to a crude oil and must, also, be separated into cuts
Separation by distillation
CRUDE OILS
Refining processes
Petroleum cuts
Ba s e s
Blending
Pro du ct s
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The processing through the conversion units produces most of the time a large scale of hydrocarbons that looks like a crude oil. Thus it has to be fractionated into cuts. cuts . That is the reason why distillation is so often used all around the refinery. The yields obtained by fractionation of a crude oil or a cracked effluent can be determined by means of the TBP analysis.
I-
TBP ANALYSIS ANAL YSIS Every petroleum cut obtained by distillation corresponds to a volatility range that may be characterized simply by a series of normal boiling point temperatures, or by the number of carbon atoms of the hydrocarbons contained in the cut. For example:
Kerosene cut
180-230°C or C10-C13
The relationship between the boiling po int temperature temperature range and range and the yield of yield of a crude oil is obtained by the TBP (True Boiling Point) analysis. Point) analysis. This consists of a high separation distillation operation which produces all the petroleum components one after the other in function of their boiling point temperature at the top of the column. The result of the analysis is represented by the TBP curve of the crude i.e. the curve linking the boiling point temperatures at the top of the column to the distilled amounts. TBP TBP distillat distillation ion curve
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Boiling point temperatures temperatures versus distill distilled ed percentages. percentages.
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Boiling point of hydrocarbons at the top of the column
CONDENSER
Boiling temperature
T Measurement of the temperature
Reflux
l i o l d e i o r u c e " d v y r u a c " t H e h " g i L "
Receiver
t2
DISTILLATION TRAYS Measurement of distilled quantities
t1
Crude oil sample % Distilled HEATING DEVICE
0
Yield of cut t1 – t2
PRINCIPLE OF TBP DISTILLATION Separation of crude oil constituents in function of their boiling point
50
100 Yield of cut t1 – t2
TBP CURVE Boiling point temperature versus distilled amounts
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For two boiling point temperatures t 1 and t 2 characterizing a petroleum cut, the TBP curve shows the principle of yield determination and the result obtained for two different crude oils. At the same time, the comparison of the distilled amounts at a given temperature shows the yield variations between a "light" and a "heavy" crude oil.
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II -
THE DIFFERENT PETROLEUM CUTS
An other representation of the TBP distillation curve is obtained by associating the temperature scale and the distilled percentages as shown below. In this diagram, each rectangular area represents the yield of the different cuts from the crude. This makes it possible to situate the names and the corresponding temperatures limits or cut points of the petroleum cuts obtained in refineries.
O°C
80 – 90°C
C 1 C2 C3 C4 iC 5 C 5
Fuel gas Propane Butane
Gasoline and naphtha cuts
145°C 185°C
s t u c 3 o t 2
Light gasoline Heavy gasoline or Heavy naphtha
Kerosene cut
220°C to 240°C
C6 C7
Final boiling point
à C 10 C 11 C 9 C 11 à C 13 C 14
Final boiling point Freezing point
C 13 C 14 • Flash point
Light gasoil
Gasoil cuts
to Heavy gasoil
1 to 3 cuts
360°C to 380°C
C 20 C 25
Cloud point CFPP
C 20 C 25 Distillate cuts or VGO
Distillate 1
2 to 4 cuts
Distillate 2
Color Metal contents
550°C to 600°C
C 50 C 40 C 50 +
Vacuum residue C 6 6 0 D C P D
Normal Boiling Point (°C)
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The operation of the crude oil distillation leads to the following cuts:
1-
FUEL GAS CUT(C1-C2) This cut is generally used as internal fuel in the refinery furnaces.
2-
PROPANE AND BUTANE CUTS (C3 - C4) These two cuts are generally treated to remove the impurities as H 2S or mercaptans. Then they are included in the commercial products: propane, butane, automotive LPG. Butane can also be used in motor gasolines to adjust the Reid Vapor Pressure (RVP).
3-
GASOLINES AND NAPHTHA CUTS (C5 to C10 - C11) These cuts from C5 to C10 - C11 generally undergo further processing to improve their low octane number. We can distinguish: – LIGHT GASOLINES (C5 - C6 or from 0°C up to 80°C or 100°C). They can be used for different purposes: •
directly as motor-gasoline base with a poor octane number (RON between 60 and 80). Note that these gasolines were good bases for leaded products, since they have a very good response to lead incorporation.
•
it may be sold as petrochemical naphtha feedstock for a steam cracker . In this case, isopentane is generally first separated from the light gasoline by distillation and then mixed with motor gasolines (iC5: RON: 92.3; MON: 90.2). The petrochemical naphtha is then called deisopentanized naphtha.
isopentane
Light gasoline C5 - C 6
DEISOPENTANIZER
Deisopentanized naphtha
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it can be subjected to the isomerization process in order to improve the octane number. The process consists in converting the normal paraffins (low octane number) into isoparaffins with a medium or high octane number. This operation is especially useful for meeting requirements concerning the MON values of unleaded automotive gasolines. It produces a motor-gasoline base rich in isoparaffins called isomerate.
Light gasoline C5 - C6 RON 60 to 80
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ISOMERIZATION
Isomerate C5 - C6 RON 83-90 MON 82-88
HEAVY GASOLINE (C7 to C10 - C11 or 80 up to 180°C) with a low octane number (20 to 50) which will be used as a feedstock for catalytic reforming. The purpose of this unit is essentially to convert the paraffinic and naphthenic molecules to aromatic components with a high octane number. This operation provides a very good gasoline base called reformate.
Heavy gasoline C7 - C10 / C11 RON 20 to 50
CATALYTIC REFORMING
Reformate Gasoline with a high RON 100 ≅
This conversion is only possible on hydrocarbons with a minimum o f 6 carbon atoms and thus able to be easily changed into aromatics. However, in view of the recent specifications concerning the restriction of benzene content, refineries will have to run C7+ feeds. The corresponding initial cut point is around 80-100°C. Besides, the upper limit is chosen according to the gasoline final boiling point which must be lower th an 210°C. As a matter of fact, the final boiling point temperatures between the naphtha feedstock and the reformate increase by 20°C to 30°C during the reforming process. The result is that the naphtha cut is limited at around the upper temperature of 180-185°C. In practice, this upper limit is chosen between 140°C and 185°C according to the relative commercial requirements of gasolines and g as oil.
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KEROSENE CUT (C9-C10 to C13-C14) This cut is used as base material for: – jet fuels, mainly Jet A1 – diesel fuels and home-heating fuels The quality specifications in relationship with volatility and the cut points are mainly: – the flash point, especially when the cut point between heavy gasoline and kerose is low • for Jet A1, the specification is: flash point (ABEL) 38°C • for diesel fuels, flash point of the kerosene cut limits its incorporation rate – the final boiling point, which is related to the cold flow properties. The freezing point has to be lower th an – 47°C. From that point of view, the kerosene cut is an excellent base to be used to improve the cold flow properties of the gasoil Concerning the sulfur content, the following table compares the kerosene cut and the commercial products. KEROSENE CUT
JET A1 SPECIFICATIONS
• Sulfur content (% wt)
• Sulfur content 0.3% wt
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between 0.01 and 0.07 for • Mercaptans content 30 g/t cuts from BTS crude oils
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between 0.07 and 0.3 for • Copper strip and silver strip corrosion cuts from HTS crude oils
• Mercaptans content 10 to 300 g/t depending on the crude origin
DIESEL FUEL SPECIFICATIONS • Sulfur content 0.035% wt
On the basis of these figures, it is to be seen that desulfurization is generally not necessary when sending the kerosene cut to the Jet A1 pool. On the contrary, the presence of a too large amount of mercaptans imposes a sweetening process like MEROX, KEROX or SULFREX to get rid of these impurities. This unit transforms the mercaptans into non corrosive disulfide. The elimination of the mercaptans can also be achieved by hydrotreatments like HYDROSWEETENING.
Sweetening processes MEROX, SULFREX, ... Kerosene cut with mercaptans
Sweet cut to JET A1 pool
Hydrotreatment Hydrosweetening In view of the production of diesel fuels with less than 0.035% wt sulfur , or even less, the hydrodesulfurization of kerosene cuts will become necessary as soon as the sulfur content of the kerosene cut is larger than the specified value.
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GAS OILS OR MIDDLE DISTILLATES (C13-C14 to C20-C25) Gas oil fractions (US: distillates) are used for the production of diesel fuels or domestic fuel-oils. They must be desulfurized in proportion to the specification of sulfur content that become more and more stringent. This operation is carried out in a catalytic hydrogen-consuming unit called a gas oil hydrodesulfurisation unit.
Hydrogen
Gas oil cuts with high sulfur content
HYDRODESULFURIZATION
0.1 to 0.3% wt sulfur from LS crudes 0.3 to 2% wt sulfur from HS crudes
Desulfurized gas oil cut
Less than 0.005% wt sulfur for diesel oil pool Less than 0.1% wt sulfur for heating oil pool
Mainly in European countries, large quantities of such products are needed and the refiner tries to obtain the largest yields for these cuts. Cold flow properties - pour point and CFPP - limit the maximum yield possibilities (maximum end bo iling point at arou nd 350 - 380°C).
This temperature range of 350°C to 380°C can be considered as the maximum boiling temperature which separates the light and medium cuts from the heavy cuts. The light and medium cuts can be handled without heating and valorised as motor, engine, turbine fuels. The heavy cuts will remain warmed inside the refinery in order to avoid congealing and to allow normal flowing. Except in the case of special products (lube oils, bitumen), it is necessary to transform the heavy cuts into light and medium cuts by conversion
treatments . The complexity of these treatments is related to the characteristics of the heavy cuts obtained by distillation.
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VACUUM GAS OILS (C20-C25 to about C50) These cuts form the lighter fractions of the atmospheric residue (350 - 380°C+). Their components are vaporised during vacuum distillation: this is the origin of characterizing them as VACUUM GAS OIL (VGO). These heavy cuts are thus separated from the Vacuum Residue in order to contain few asphaltens and metal contaminents, and to be easily processed in catalytic conversion units. The refiners generally try to obtain the maximum yield of VGO/distillates , maximizing the final boilin g po int aroun d 550°C to 600°C. The conversion processes are generally: – catalytic cracking (F.C.C.) to produce mainly gasolines and olefins (propylene-butenes) – hydrocracking (HCK) which produces gasolines, kerosenes and gas oil fractions.
Gas - LPG (olefin rich) VGO / Distillates C20 - C50
F.C.C Fluid Catalytic Cracking
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Cracked gasoline ( 50%) ≅
Cracked gas oil (LCO) heavy cuts Hydrogen
Gasoline VGO / Distillates C20 - C50
H.C.K. Hydrocracking
Kerosene Gasoil
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At the same time, this VGO cuts might be used as feedstocks for light base lubricating oil and waxes manufacturing. The need for products with various viscosities requires the separation of three to four distillates in the atmospheric distillation column.
VGO / Distillates
LUBE OIL MANUFACTURING
Lube base oil
Waxes
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VACUUM RESIDUE It is the "non-vaporisable" fraction of the crude oil. It is often called "the bottom of the barrel". VACUUM RE SIDUES
(Yield in % volume)
Saharian crude
10 to 15%
Middle-East crude (Arabian light or Kuwait)
20 to 30%
Heavy crude oils (Boscan, Venezuela)
60 to 70%
This vacuum residue, which must be stored at m ore than 130°C, because of its high viscosity, concentrates the asphaltenes and petroleum resins, which contain the major part o f metal contaminants making catalytic conversions difficul t. According to the refinery type, different uses or treatments are applied to this cut.
Internal fuel oil (rare in Europe) Direct use
Base heavy fuel oil production
Lubricating oils
LUBE OIL PLANT
Base for bitumen manufacturing Heavy lube base oil Waxes Cracked cuts
VISBREAKER Vacuum Residue
Cracked cuts Thermal
COKER
conversion
Coke
Cracked cuts FLEXICOKER
Fuel gas (gasified coke) LMC residues
F.C.C.
Cracked cuts
Hydrotreatment or Hydroconversion
Cracked and hydrotreated cuts
Catalytic conversion LMC : Low Metal Content LMC: Low Metal Content
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III -
CRUDE OIL FRACTIONATION SCHEME The initial f ractionation of a crude oil into the different petroleum cuts described above can be summarized into three separate operations: -
atmospheric distillation of crude oil
-
vacuum distillation of the atmospheric residue
-
fractionation of gases and g asolines
The following figure gives the general and simplified scheme of the initial fractionation of crude oil. The successive steps are represented: -
preheating of the crude oil and heating in the furnace
-
desalting in order to set aside the mineral salts
-
fractionation into five cuts in a topping column. This atmospheric distillation column has quite a large size: about 50 m high and around 8 m diameter corresponding to a 1000 t/d capacity At the top, the mixture of gas and gasolines come out, then three side stream cuts called kerosene, light gasoil and heavy gasoil, and last the atmospheric residue at the bottom
-
-
separation of the light ends with four or five distillation columns: –
+
•
debutanizer separating the gas C4 and the gasolines C5
•
deethanizer separating the fuel gas C 2 and the LPG C3 and C4
•
depropanizer to separate the propane C3 from the butane C4
•
gasoline splitter separating the two gasolines, i.e. the light gasoline including C 5 and C6 and the heavy gasoline with C7 to C10/11
•
deisopentanizer to separate the isopentane (iC5) from the light gasoline
–
the vacuum distillation of the atmospheric residue in a column operating at a lower pressure from atmospheric pressure. The aim of using vacuum is to reduce the temperatures in the furnace and in the column to keep them compatible with the stability of the hydrocarbons (cracking threshold is 400-430°C). This column also has quite a large diameter and is connected to a vacuum system to suck the non condensable fraction at the top. It separates side stride streams called vacuum distillates (UK) or vacuum gasoil (US) and at the bottom, the vacuum residue.
In order to maximize the yield of vacuum distillates, which can be valued in conversion catalytic unit as FCC, one operates with a very high inlet temperature, and the lowest possible pressure. This causes a large vaporization of the column feed. Even if the aim of the different refineries in the same, numerous different schemes exist for the initial fractionation of the crude oils. The following scheme is only an example.
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CRUDE OIL INITIAL FRACTIONATION – Overview scheme – Fuel gas 26
C2-
Propane C3 17
DEETHANIZER Gas 11
C1 - C4 DEPROPANIZER
DEBUTANIZER
C3 - C4 CRUDE OILS STORAGE Water
Gas + gasoline Butane C4
C1 - C10/11 2.5
HEAT EXCHANGERS 1,5
C5 - C6
Gasoline
2.5
C5+
DESALTER
DEISOPENTANIZER GASOLINE SPLITTER
ATMOSPHERIC COLUMN
Water
Isopentane iC5
Light gasoline
Deisopentanized light gasoline
Water + salts
C7 - C10/11
Heavy gasoline naphtha Kerosene
STRIPPERS HEAT EXCHANGERS
Light gas oil
365
ATMOSPHERIC FURNACE
Medium gas oil
60 mbar
2.8
To vacuum system Heavy gas oil
VACUUM COLUMN
Atmospheric residue C20/25+
VGO/Distillate 1
VGO/Distillate 2 Pressure in bar abs Temperature in °C VACUUM FURNACE 00007_C_A
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400
80 mbar Vacuum residue
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YIELDS AND MAIN CHARACTERISTICS OF CRUDE OILS The yields in petroleum cuts strongly depend on the origin of the crude oil. The scheme below shows the yield structures in gas, gasolines, intermediate cuts (kerosenes, gas oils), heavy cuts (VGO, Vacuum Residue) obtained from several crude oils.
SAHARIAN CRUDE OIL (Algeria)
LIGHT ARABIAN CRUDE OIL (Saudi Arabia)
SAFANIYA CRUDE OIL (Saudi Arabia)
ATHABASKA (Canada)
BOSCAN (Venezuela)
0.806
0.855
0.893
1.000
0.995
44
34
27
10
10.7
0.2
1.7
2.8
4.27
5.27
0
GAS
10 GASOLINES
20 30 40 % t h g i e W
50 KEROSENE GASOLES
60 70 80 90
DISTILLATE R.S.V.
100 SPECIFIC GRAVITY ° API SULFUR CONTENT wt %
Comparison o f yields obtained from different crude oils
It can be noted the link between the specific gravity (Sp. gr. or °API) and the yields in light cuts. The specific gravity is an important criteria for crude oils which leads to the following classification:
Light crude oils : Sp. Gr. 0.800 to 0.830 - high yields in gasolines and intermediate distillates Medium crude oils : Sp. Gr. 0.830 to 0.890 Heavy crude oils : Sp. Gr. 0.890 to 1.000 In the same time, an other chief quality criteria is the sulfur content which can vary between 0.04% wt and 68% wt for the sulfur richest crude oils. Sulfur content drives the utilisation of desulfurization treatments in order to reach the specifications of the different petroleum products. It can be distinguished into:
Low sulfur content crude oils (< 0.6% wt of sulfur) for which the cuts easily meet the specifications
Medium and high sulfur content crude oils (> 0.6% wt of sulfur) which requires desulfurization treatments
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The other technical characteristics which can also be involved in the quality of crude oils are: – the viscosity , particularly as far as transportation in the pipelines is concerned – the pour point which is generally low enough so that the tanks have not to be heated. In some cases, and sometimes for light crude oils, high pour points are observed due to high paraffin contents. Some precautions, such as blending or preheating are to be taken to allow transportation – the asphaltene and metal content – the ability to produce base lube oils and bitumen
The following tables shows the main quality criteria of the crude oils coming from: – MIDDLE EAST crude oils (Figure 1) of variables quality have almost all a high sulfur content – NORTH SEA and NORTH AFRICA crude oils (Figure 2) are rather light and low sulfur – WEST AFRICA crude oils are generally LS crude oils (Figures 3 and 4). Their naphthenic character gives them a high specific gravity despite the fact that they generate good yields of light product and intermediates – LATIN AMERICA crude oils (Figure 5) are generally heavy and high sulfur – FAR EAST and RUSSIA crude oils (Figure 6) are of variable quality
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MAIN CHARACTERISTICS OF SOME CRUDE OILS
MIDDLE EAST Murban
Zakhum lower
Dubaï
Iranian light
Origin
Abu Dhabi
Abu Dhabi
Dubaï
Iran
Iran
Irak
Irak
°API
39,60
40,16
31,25
33,8
31,0
33,7
36,2
Sp. gr.
0,826
0,824
0,869
0,856
0,871
0,856
0,844
%S
0,73
1,01
2,07
1,35
1,65
2,00
1,95
Pour Point
– 12°C
– 12°C
– 30°C
– 29°C
– 21°C
– 26°C
– 30°C
Viscosity
5,9 cSt to 10°C
0
G
6 cSt to 10°C 16,2 cSt to 10°C 10,6 cSt to 10°C 17 cSt to 10°C
G
10 N
Iranian heavy Basrah light
G
G
G
N
N
N
N
20
150°C
15 cSt to 10°C 12,8 cSt to 10°C
G
G
N
N
150°C 150°C
150°C
165°C 150°C
165°C
30 K GO
40
50
K GO
Kirkuk
K GO
K GO
K GO
K GO
352°C 345°C
352°C
60
K GO
375°C 345°C
70
VGO
375°C 375°C
VGO 80
VGO
VGO
VGO
550°C
VGO
VGO
550°C
550°C
550°C
550°C
90
550°C 550°C
100
VR 1,6 % Sulfur
VR
VR
4,36 % Sulfur
3,2 % Sulfur
VR
VR
VR
4,7 % Sulfur
5,8 % Sulfur
VR 3,09 % Sulfur
3,4 % Sulfur
% volume
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MAIN CHARACTERISTICS OF SOME CRUDE OILS
MIDDLE EAST Qatar marine
North field condensate
Oman
Qatar
Qatar
31,4
33,34
32,50
55,72
37,7
33,9
28,0
24,1
Sp. gr.
0,869
0,858
0,862
0,755
0,836
0,855
0,888
0,909
%S
2,56
1,04
1,80
0,21
1,26
1,79
2,82
3,9
Pour pointt
– 15°C
– 24°C
– 15°C
—
– 34°C
– 43°C
– 34°C
– 30°C
Kuwait
Oman
Origin
Kuwait
°API
Viscosity
0
Arab extra light
Arab light
G
G
G G
N
Arab heavy Safaniya
Saudi Arabia Saudi Arabia Saudi Arabia
10 cSt to 38°C 34,3 cSt to 10°C 17 cSt to 10°C 1,29 cSt to 10°C 5,8 cSt to 21°C 10 cSt to 21°C
N 10
N
G
N
G
G
N
40
N
150°C
165°C
K GO
G
N
150°C
30
Syria
37 cSt to 21°C 150 cSt to 10°C
150°C
20
Souedie
165°C
N K GO
165°C
K GO
K GO
165°C
K GO
K GO
K GO
345°C
50
145°C
345°C
375°C
375°C 345°C
60
345°C
375°C
VGO
VGO 70
VGO VGO 550°C
80
550°C
K GO
VGO
550°C
90
VR
VGO
550°C
550°C
550°C
VR
550°C
VR 375°C
100
VGO
VR
VR
VR
5,9 % Sulfur
6,97 % Sulfur
VR
VGO
5,5 % Sulfur
2,32 % Sulfur
4,3 % Sulfur
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3,14 % Sulfur
4,03% Sulfur
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MAIN CHARACTERISTICS OF SOME CRUDE OILS
NORTH SEA
FRANCE
Sleipner condensate Chaunoy Seine et Norway marne
Brent
Forties
Flotta
Statfjord
Ekofisk
Origin
UK
UK
UK
UK-Norway
Norway
°API
38,08
44,54
35,7
39,1
37,47
59,8
37,2
Sp. gr.
0,834
0,803
0,846
0,829
0,837
0,739
0,839
%S
0,38
0,20
1,14
0,22
0,202
0,02
0,13
Pour point
– 3°C
– 15°C
– 6°C
+ 6°C
– 6°C
< – 45°C
—
Viscosity
0
7,1 cSt to 10°C 3,9 cSt to 10°C
G
31 cSt to 5°C
G
G
7,0 cSt to 10°C 9,8 cSt to 10°C 0,7 cSt to 20°C
G
G
G
N
N
10
N
N
N
N
N
20
150°C 150°C
150°C
30
150°C
165°C
K GO
150°C
40
50
—
K GO
K GO K GO
K GO
K GO
60 345°C
375°C
70 375°C
80
350°C 375°C
375°C
VGO
VGO
VGO
VGO
VGO
180°C
550°C
K GO
VGO 90
550°C
VR 100
1,25% Sufur
550°C
550°C
550°C
VR 1,06% Sufur
VR
VR
VR
2,23% Sufur
0,77% Sufur
0,63% Sufur
% volume
550°C
VR 375°C VGO
D 6 5 0 C P P D
© 2008 - IFP Training
— Figure 3 —
MAIN CHARACTERISTICS OF SOME CRUDE OILS
NORTH AFRICA
WEST AFRICA
Sahara blend
Zarzartine
Es Sider
Girassol
Palanca
Kole
Origin
Algeria
Algeria
Libya
Angola
Angola
Cameroon
°API
44,8
42,0
36,25
31,33
37,23
31,51
Sp. gr
0,803
0,816
0,843
0,867
0,838
0,868
%S
0,15
0,08
0,44
0,33
0,18
0,35
Pour point
– 29°C
– 12°C
+ 6°C
– 6°C
9°C
– 9°C
Viscosity
3 cSt to 21°C
6,9 cSt to 10°C
10 cSt to 10°C
36,9 cSt to 10°C
7,6 cSt to 10°C
14,5 cSt to 10°C
G
G
G
G
0
G
N
10
N
30
40
150°C
165°C
150°C
K GO
165°C
K GO
K GO 375°C
K GO
K GO K GO 375°C
375°C 345°C
375°C
70
VGO VGO
345°C
VGO
80
VGO
VGO 550°C
100
VR 0,51% Sulfur
550°C 550°C
550°C
VR
VR VR
VR 0,19% Sulfur
VGO
550°C 550°C
90
N
165°C
50
60
N 150°C
N 20
N
G
1,15% Sulfur
% volume
0,75% Sulfur
0,47% Sulfur
VR 0,90% Sulfur
E 9 5 0 C P P D
© 2008 - IFP Training
— Figure 4 — MAIN CHARACTERISTICS OF SOME CRUDE OILS
WEST AFRICA Djeno
Mandji
Bonny light
Forcados
Qua lboe
Oso condensate
Origin
Congo
Gabon
Nigeria
Nigeria
Nigeria
Nigeria
°API
27,36
29,54
35,36
30,43
36,4
47,40
Sp. gr.
0,890
0,870
0,848
0,873
0,843
0,791
%S
0,27
1,1
0,14
0,18
0,12
0,05
Pour point
0°C
+ 9°C
– 18°C
– 27°C
+ 7°C
+ 2°C
Viscosity
179 cSt to 20°C
72 cSt to 10°C
6,9 cSt to 10°C
17,4 cSt to 10°C
8,3cSt to 20°C
1,9 cSt to 20°C
G
G
0
G
G
G
N 10
N
N 150°C
N 150°C
20 K GO 30
150°C
N 165°C
K GO K GO
375°C
60
375°C
K GO
K GO
165°C
VGO VGO
70
N
150°C
40
50
G
345°C
K GO
VGO
345°C
375°C
550°C 375°C 550°C
80 VR 90
VGO VR
VGO 550°C
550°C
VGO 550°C
VR 100 0,39% Sulfur
2,33% Sulfur
VR 0,55% Sulfur
% volume © 2008 - IFP Training
0,56% Sulfur
VR 0,40% Sulfur
550°C VR F 9 5 0 C P P D
— Figure 5 —
SOME CHARACTERISTICS OF SOME CRUDE OILS
LATIN AMERICA
NORTH AMERICA
Tia juana light
Tia juana heavy
Bachaquero
Isthmus
Maya
Origin
Venezuela
Venezuela
Venezuela
Mexico
Mexico
°API
32,1
12,1
16,8
32,8
22
21,2
30,6
Sp. gr.
0,865
0,985
0,954
0,861
0,922
0,927
0,873
%S
1,1
2,7
2,4
1,51
3,32
3,69
1,01
Pour point
– 43°C
– 1°C
– 23°C
– 26°C
– 18°C
– 48°C
– 18°C
Viscosity
11 cSt to 39°C
3 cSt to 50°C
300 cSt to 38°C
6 cSt to 38°C
0
10
N
G
165°C
N
K GO 345°C
20
G
N
G
150°C
150°C 150°C
345°C
K GO
550°C
N
165°C
K GO
345°C
VGO
K GO
345°C
550°C
550°C
VGO
550°C
VR
VR
550°C
VR
550°C
VR
VR
2,64% Sulfur
VGO
VGO
550°C
100
345°C
VGO
VR
90
G
345°C
60
80
K GO
VGO
VGO
70
N
165°C
K GO
USA Alaska
150°C
30
50
G
G
N
K GO
North Slope
70 cSt to 38°C 177 cSt to 20°C 13 cSt to 20°C
N
375°C
40
Cold lake blend Alberta Canada
VR 3,77% Sulfur
3,3% Sulfur
3,62% Sulfur
% volume
5,81% Sulfur
2,21% Sulfur
2,53% Sulfur
D 8 5 0 C P P D
© 2008 - IFP Training
— Figure 6 — MAIN CHARACTERISTICS OF SOME CRUDE OILS
ASIA
OCEANIA
RUSSIA
AZERBAIJAN
Urals
Azeri light
Daquing
Shengli
Bekapai
Minas
Tapis
Gippsland
Origin
China
China
Indonesia
Indonesia
Malaysia
Australia
°API
33,3
24,2
43,2
35,3
45,5
48,7
31,8
34,8
Sp. gr.
0,859
0,909
0,809
0,848
0,799
0,785
0,866
0,851
%S
0,11
1,0
0,06
0,07
0,02
0,09
1,35
0,16
Pour point
+ 35°C
+ 21°C
– 29°C
+ 35°C
+ 16°C
– 12°C
– 18°C
– 7°C
Viscosity
132 cSt to 50°C
8 cSt to 50°C
0
G
G
10
165°C
20
K GO
2,9 cSt to 10°C 12,4 cSt to 50°C 3,18 cSt to 20°C 1,7 cSt to 20°C 17,9 cSt to 10°C 11,9 cSt to 20°C
G
N
N
G
G
G
N
165°C
30
345°C
N K GO 150°C
40
G
N
165°C
N
150°C
N K GO
165°C
345°C
50
G
N
165°C
K GO
Russia Azerbaijan
K GO
375°C 165°C
VGO
VGO
K GO 60 550°C
550°C
K GO
VGO
375°C 375°C
K GO
70 550°C
VGO
345°C
80
VGO
345°C
VR
550°C
VR 375°C
90
VR
VGO
VGO
550°C
VGO
VR VR
100
0,17% Sulfur
1,37% Sulfur
550°C
550°C
VR
VR
VR
0,17% Sulfur
0,84% Sulfur
0,45% Sulfur
0,17% Sulfur
% volume
550°C
2,78% Sulfur
0,43% Sulfur
D 0 7 0 C P P D
© 2008 - IFP Training
S C I T S I R E T C A R A H C L I O E D U R C L A C I P Y T
— 7 e r u g i F —
e d u a r e m E
2 0 6 1 0 . 4 1 0 6 1 6 . 6 . 3 3 . . 9 . 2 2 3 0 4 1 7 1 0
n a c s o B
9 9 9 . 0
e k a L d l o C
7 0 2 1 1 . 9 . 1 . 0 7 4 0 1 . 3 4 . 3 9 3 2 8 . 1 1 4 4 6 4 0
3 3 7 1 7
a y i n a f a S
1 0 7 9 3 5 3 . 9 8 9 8 . 0 8 . 0 8 7 . . . 6 7 8 8 . 2 4 2 4 1 3 0
8 1 7 5
k u k r i K
7 0 1 9 7 8 . 2 8 0 4 7 4 9 . 0 5 5 . . . . 2 8 3 . 3 7 1 1 1 1 0
1 1 9 2
5 7 4 9 8 0 . 8 5 5 . 4 9 7 5 8 3 . . . 8 0 9 3 . 3 1 1 1 0
. 4 . 5 0 4 2
t n e r B
3 1 6 7 9 . 6 3 8 2 2 8 . . . 8 . 3 5 1 0 0
9 7 6 8 . . 1 0
8 . 0
5 . 2
k s i f o k E
5 8 0 8 . 0
0 5 . 1
0 4 1 . 0
4 2 . 1
5 6 . 1
1 . 0
g n i h c a T
1 1 7 . 9 7 6 . 1 . 2 8 3 7 . 3 5 0
0 9 0 . 0
0 0 5 8 . 6 1 2
n a t i h b g a r i L A
1 . 0 1
4 . 3 4
0 0 0 0 6 1
5 2 . 4
0 2 2
0 5 . 5
0 6 3 6
0 0 9
9 . 4 1
0 . 2 1
9 0 . 0
0 5 5
0 0 2 1
0 5 1
1 . 1 . 3 0
t t m S p % p m p c S c % t % t t m w p w w p p
s c i t s i r e t c a r a h C
C ° y t 0 i 2 v t a r a g y t c i i f s i I o c c e P s p A i S ° V
C ° 0 0 1 t a y n t i e s r g o u o f c l r t s i u i V S N
n o b r a C n o s d a r n o C
s e l b u l o s n i 7 C
l e k c i N
m u i d a n a V
S C I T S I R E T C A R A H C S E U D I S E R C I R E H P S O M T A L A C I P Y T
— 8 e r u g i F —
e d u a r e m E
9 0 . 8 6
8 7 6 9 . 0
5 7 5 . 0
0 0 2 2
8 8 1
0 . 8 3 . 3 9 9 1
n a c s o B
0 3 . 5 8
2 7 2 0 . 1
9 8 . 5
0 0 4 6
0 5 7 1
1 . 7 3 8 . 1 6
0 8 5 1
e k a L d l o C
6 7 . 1 8
4 1 0 . 1
1 9 . 4
0 0 1 5
8 8 2
0 . 6 0 4 . 1 5
9 9 2
a y i n a f a S
2 8 . 9 5
4 1 8 9 . 0
0 3 . 4
0 5 2 2
4 9
2 . 9 5 3 . 1 3
5 2 1
k u k r i K
8 4 . 6 4
8 0 5 9 . 0
7 7 . 3
0 2 3 6 . 0 9 . 8 4 2 8 9 2 2
n a t i h b g a r i L A
9 7 . 3 4
5 4 5 9 . 0
4 1 . 3
0 6 0 4 . 8 6 . 0 4 2 5 7 1 1
t n e r B
3 0 . 2 4
2 2 2 9 . 0
8 6 6 . 0
0 9 5 5 . 2 . 9 . 9 1 1 3 1 7
k s i f o k E
5 8 . 3 3
0 4 2 9 . 0
6 6 3 . 0
0 5 9 6 . 7 5 . . 1 1 1 2 5 0 3
g n i h c a T
8 5 . 0 7
8 3 0 9 . 0
1 7 2 1 . 0
0 0 5 0 5 . . 3 1 . 3 2 4 0 4 2
% t w
d l e i y t u C
t % % S p p t m c t % t m w p w w p y t i v a r g n c i e f i r g c u o f e l r t p u i S S N
F ° 0 1 2 t a y t i s o c s i V
n o b r a C n o s d a r n o C
s e n e t l a h p s A
V + i N
S C I T S I R E T C A R A H C E U D I S E R M U U C A V L A C I P Y T
— 9 e r u g i F —
e d u a r e m E
8 3 . 1 4
9 0 0 5 2 . 9 7 8 0 6 . 6 5 6 . 9 8 2 0 . 2 2 1 2 1 0
n a c s o B
4 7 . 0 6
0 2 0 0 6 0 . 6 . 0 6 0 2 0 2 . 4 0 0 9 0 . 6 9 0 2 1 2 2 1 5
e k a L d l o C
2 5 . 6 4
5 0 0 0 1 0 . 5 . 6 2 0 . 6 2 6 7 6 6 7 6 2 0 0 5 . 1 9 1
a y i n a f a S
5 6 . 7 2
0 2 0 0 7 0 . 2 5 0 0 . 9 6 3 . 7 0 0 9 . 5 2 6 2 4 5 1
k u k r i K
4 2 . 6 1
9 0 0 9 2 . 8 6 1 . 0 1 . 1 5 6 6 3 5 0 7 2 2 . 4 4 0
n 4 a t 7 2 4 i h . 3 b g 7 2 . i a 4 . r L 1 0 1 A
0 6 9 2
0 3 1 . 9 9 5 4 0 . 5 1 2 5 1
t n e r B
1 0 . 1 1
8 0 8 8 6 8 . 0 9 2 9 8 1 . 5 . 0 4 3 9 5 1 2 . 7 4 0
k s i f o k E
4 2 . 1
3 5 7 9 . 0
8 9 5 . 0
0 8 6 4 . 7 . 9 8 0 4 . 1 4 1 1 3 1 6
g n i h c a T
5 6 . 1 3
8 1 4 9 . 0
8 7 1 . 0
0 0 1 9 0 5 2 9 . . 0 2 1 1 9 0 4
% t w
d l e i y t u C
t % % S p p t m c t % t m w p w w p y t i v a r g n c i e f i r g c u o f e l r t p u i S S N
F ° 0 1 2 t a y t i s o c s i V
n o b r a C n o s d a r n o C
s e n e t l a h p s A
V + i N
