Note: Descriptions are shown in the official language in which they were submitted.
41~
-- 2 --
BACKGROUND OF THE INVENTION
The procedure to handle heavy crude oils with a
high content of asphaltenes (over 7 weight ~; not soluble
in nC5), is characterized by removing contaminants by
means of an extraction stage by selective solvents in
order to obtain an extract whose properties are similar to
those of an atmospheric light residue (with less contents
of asphaltenes) and a stream where crude contaminants
known as bottGms are concentrated.
The growing worldwide demand for energy, together
with technology breakthroughs, have encouraged the
development of more and more complex procedures to
integrally recover distillates and residues derived from
crude oils.
Over the years, the oil industry needs have
undergone many changes; at present, it provides more heavy
crude oi~s.
A crude oil is a mixture mainly constituted by
several hydrocarbons and in a minor proportion, compounds
containing in their molecules elements such as sulfur,
nitrogen, oxygen, vanadium, nickel, --iron, and copper,
among others. Generally, a crude oil whose specific
gravity is high is known as a heavy crude oil, generally
signifying that in its composition the low boiling point
hydrocarbons are present in a lower proportion than in
those oils known as light crudes; however, when defining
thus a heavy crude oil, the chemical nature of its
compounds is not considered and consequently its quality
is not pin-p~i~ted even if in their analysis, data
normally determining the crude quality are included.
For the same specific gravity, i.e. API, quality
of a crude can vary greatly since the yield of products
may be quite different or the availability of some types
of products may substantially increase the costs of its
process or sometimes they may partially or totally impair
the normal refining procedure.
32
Crude oils present particular behaviors in their
various recovery stages, these behaviors depend on the
nature and physical and chemical properties of
hydrocarbons.
The main stages correspond to production,
handling, refining and marketing.
Traditionally, light and middle hydrocarbons have
been recovered, and recovery of heavier crudes makes it
necessary to develop new technologies for these reserves
to be commercia~ly exploitable. Also, light and middle
crudes are easily dehydrated and transported through
pipes. Heavy crude oils, on the contrary, due to their
high viscosity and specific weight are difficult to handle
and more costly transportation systems are required.
lS Heavy crude oils, especially those with high contents of
asphaltenes, will also require special processin~ plants.
Hence, marketing on a world wide basis of heavy crude oils
will also present particular characteristics.
As mentioned, standard techniques are based on
the recovery of light and middle consistency
hydrocarbons. The refin~ries to process these products
are adapted to a typical scheme in order to recoYer fuels
generally consistent of the following refining sequence:
atmospheric distillation, vacuum distillation of
atmospheric residues, upgrading of gasolines by catalytic
cracking of vacuum gas oils and viscosity breaking of
vacuum distillation residues.
Applicant has developed a processing scheme for
heavy crude oils with a high content of asphaltenes,
including the following stages: atmospheric distillation,
selective extraction with solvents, vacuum distillation
and viscosity breaking. In this process the feed for the
extraction unit is bituminous material which is a residue
having an initial boiling temperature of 300 to 470C,
derived from distilling heavy crude oil.
.
12~
4 --
SUMM~RY OF THE I~VE~TION
According to the me~hod of this invention, heavy
crude oils containing high levels of asphaltenes and a
paraffinic and naphthenic base are processed. The process
stages firstly comprise subjecting the crude to a primary
distillation under atmospheric pressure, obtaining thus a
residue at an initial boiling temperature of 300~-470C.
Immediately thereafter, the process is characterized by
the residue being subject to a selective extraction with
C4 - C7 aliphatic solvents or a mixture thereof,
recovering through the top an extract with properties
similar to those of a residue of light crude atmospheric
distillation. The extract derived is immediately subject
to refining stages such as vacuum distillation; catalytic
cracking, and viscosity breaking, coking, preparation of
asphalts and fuel oils from vacuum residues. Through the
bottom a stream is recovered where the crude contaminants
are concentrated.
Therefore, an object of this invention is a
method to process heavy crude oils with high contents of
asphaltenes allowing the provision of an extract whose
asphaltene and metal percentages are similar to those in a
light crude residue for further processing in the
conversion units, as mentioned.
Another purpose of this invention is to provide a
method to process heavy crude oils which allows a
comparatively increase in the distillate yields in
relation to the conventional heavy crude oil processing.
Another purpose is to provide a heavy crude oil
processing method allowing utilization of crude oil and
the refining of residues thereof in conventional, easy to
operate processing units.
One more purpose of this invention is to provide
a new technique to process heavy crude oils to take
advantage of the growing reserve of crudes with high
contents of asphaltenes and metals.
12~6~32
-- 5 --
The present invention resides in a method for
processing heavy crude oils, which comprises distilling a
100% heavy crude oil feedstock containing at least 7
weight percent n-pentane insolubles under atmospheric
pressure to obtain an atmospheric distillation residue;
contacting said atmospheric distillation residue with a
selective solvent comprising a C4 to C7 aliphatic
hydrocarbon or mixtures thereof in an extraction column to
extract asphaltenes, carbon, sulfur and metals from said
atmospheric distillation residue, said extraction column
having a top temperature of 50 - 250C, and a bottom
temperature of 40 - 230C while being operated under a
pressure of 3-40 kg/cm2 with a solvent-hydrocarbon
volume ratio of 2:1 to 1OD1; withdrawing an overhead
fraction and a residue fraction from said extraction
column, said overhead fraction having an API gravity of
10-18, an SSF viscosity at 50C of 100 to 3,500, 1.0-75
weight percent insolubles in n-pentane and 0.20-5.0 weight
percent insolubles in n-heptane, a Ramsbottom carbon of
4.0-12.0 weight percent, 2.0 to 5.0 weight percent sulfur
and 75 to 250 ppm metals comprising nickel and vanadium;
subjecting said overhead fraction to vacuum distillation
in a vacuum distillation column at a temperature of 300C
- 540C to recover a gas oil stream and a residue stream;
catalytically cracking said gas oil stream and feeding
said residue stream to a viscosity breaking unit; and
viscosity breaking the residue stream.
DETAILED DESCRIPTION OF THE INVENTION
_
The reserve of light crude oils at present has
been decreasing in several oil producing countries, while
the heavy crude oil reserve has increased. Refining these
crudes requires several techniques.
Classification of crudes - At present there are
several classes. From the commercial point of view, crude
oils have been classified according to their API gravity
in: light ( > 30 API); middle (20 to 30 API); heavy (10
r
~6~
to 20 API), and superheavy ( < 10 API). There are also
classifications that take into account the
characterization factor, the correlation index and the
viscosity gravity constant this latter defining the
prevailing chemica~ composition; within these
classifications, crudes with a paraffinic, mixed and
naphthenic base are included.
Classifications available so far, do not indicate
the use of distillates for each crude nor the degree of
refining to be applied for an economical process.
Consequently, an arbitrary classification given from the
process viewpoint may be that a heavy crude oil, is that
which generates vacuum residua requiring an antieconomical
dilution to become commercial fuel oil.
Heavy crude oils. According to the commercial
classification, heavy crude oils are those presenting
gravities lower than 20 API. Other characteristics
ascribable to heavy crude oils are: their high viscosity,
high contents of metals, mainly nickel and vanadium; high
contents of sulfur and abundant existence of carbon
residues consisting of asphaltenes and Ramsbottom or
Conradson carbon. It has been observed practically, that
all heavy crude oils generate amounts above 35 vol% of
fuel oils with a 500 SSF viscosity derived from vacuum
distillation residues.
In addition, it can be stated that a heavy crude
oil is that which necessarily requires its process scheme
to include a secondary refining process, such as
extraction using selective solvents to separate
asphaltenes and contaminants or catalytic processes to
isolate undesirable compounds such as carbon, sulfur and
metals.
Contaminants. The presence of these compounds
found in heavy crude oils, strongly affects the various
refining stages. Thus, sulfur in the primary distillation
process restrains the distillate recovery thoroughness due
;4~
-- 7 --
to the corrosion caused by some sulfur compounds at high
temperatures. In this case, special and expensive alloys
are required in process equipment . The presence of these
compounds in distillates makes it necessary to further
treat them for their isolation as otherwise they will not
meet quality specifications.
In the secondary refining system conventionally
applie~d to refineries in order to recover additional
gasoline volumes, the influence of these contaminants is
noticed. Their presence limits the recovery of feedstock,
which is to be recycled, since in most cases catalytic
agents are used which are easily poisoned and deactivated
by the presence of contaminants, especially metals.
Regarding heav~ industrial fuels normally
prepared from asphalt residues, the presence of noxious
compounds in heavy crude oils is also noticed to attack
normal equipment burning heavy fuels. Accelerated
corrosive effects are observed as well.
~s for hydrocarbons with a low hydrogen-carbon
ratio, it may be mentioned that an indirect measure of the
refining system's complexity and severeness to be applied
in processing heavy crude oils is given by the asphaltene
contents present in crude oils.
Thus, a heavy crude oil with low asphaltene
contents is easier to refine than a crude of equal API
gravity but with a high content of asphaltenes.
A behavior measure of crude in processes
involving heating in industrial processes, is made by the
value of Ramsbottom carbon which for practical purposes
may be interpreted as the trend towards carboni~ation.
This means that in spite of a crude having distillable
hydrocarbons, when the Ramsbottom carbon is high, many of
the above hydrocarbons are not to be derived from
distillation since by increasing the temperature to the
required level, carbonization will occur.
3~46~
-- 8 --
The values obtained when determining insolubles
in pentane and heptane are a measure of the asphaltene
contents, asphaltenes being compounds of a very high
molecular weight made of carbon, hydrogen, nitrogen,
oxygen, and metals. As already stated, asphaltenes in a
heavy crude oil cause many problems when refining the
latter.
Analysis of heavy crude oils furnishes various
values as to the asphaltene contents. This is repeated
also for Ramsbottom carbon. On the other hand, even
though atmospheric distillates from a typical heavy crude
oil are comparable to those in light oils insofar as their
characteristics related to their use as fuel, a great
difference in the vacuum gas oil chemical composition is
observed, however; the gas oil derived from heavy crude
oils, have a larger amount of aromatics and consequently a
higher carbon-hydrogen ratio.
This ratio shows also a trend to carbonization
and furthermore, as heavier fractions are analyzedt such
ratio continues to increase. This means that even prior
to considering asphaltenes, heavy gas oils from heavy
crude oils, because of their high carbon hydrogen ratio,
are potential products for carbonization presenting also
high viscosity since in their chemical composition there
is a high lèvel of polyaromatics.
Certain properties of heavy crude oils and their
distillates and residues resulting from their normal
processing are described below.
CRUDE OIL
A heavy crude oil with a 21.8 API gravity may be
considered as a heavy crude oil, intermediate between
paraffinic and naphthenic as shown by the characterization
factor observed (Kuop = 11.7~. With high contaminant
values such as sulfur (3.2 weight ~), Ramsbottom carbon
(10.~ weight %), metals Ni + V (350 ppm) and nC5
insolubles (14.7 weigh+ %). As to the recovery of
~!,' !
"~
lZ~6g~
g
atmospheric distillates (46 vol %) low yields may be
considered.
GASOLI~S
Gasolines recovered from crudes as stated above
have high sulfur values (280 to 2800 ppm).
TURBO FUELS
High values of sulfur (2900 to 3800 ppm) and
freezing point (-38 to -48C) are observed~ Flash point
is good (50 to 70C ) as is the aromatic compound
contents (18 to 21 vol %).
KEROSENÆS
These fractions present acceptable values of
sulfur ( 0.38 to 0.65 weight ~) and flash point (60 to
89C). Smoke index is low (14 to 15 mm).
DIESEL
High values of sulfur are observed (0.54 to 1.6
weight %) and normal pour point (-42 to 0C). In terms
of cetane index (47.5 to 51.5) and carbon residues (0.017
to 0~060 weight %) these fractions are of good quality.
HEAVY DISTILLATES
Metal contents is low (Ni + V = ppm) as opposed
to sulfur (2.2 to 2.9 weight %). Viscosity index (60 to
69) suggest the possibility to recover paraffinic lube
oils.
RESIDUES
Residues recovered from vacuum distillation have
high levels of sulfur (3.8 to 5.0 weight %), metals (~i +
V = 500 - 800 ppm), insolubles in pentane (20-33 weight %)
and viscosi~y at 98.9C (340 - 50,000 cs).
Based on the above, one comes to the conclusion
that a heav~ crude oil, due to its chemical
characteristics, is a crude oil with a tendency to
carbonization in industrial refining operations and
because of its high contents of metals, it will produce
vacuum gas oil with high concentrations thereof which will
affect the proper operation of catalytic cracking plants.
~Z~
-- 10 --
Consequentlyl the object of this lnvention is to provide a
method to eliminate the products mentioned from heavy
crude oils, i.e. those with high values of Ram~bottom
carbon, asphaltenes and metals so that the processes to
which the crude oil is subject during its refining, may
operate with a proper efficiency as will a typical light
crude oil.
The main characteristics of a heavy crude oil
subject to treatment under this invention are described
below:
CRUDE OIL ANALYSIS
Specific ~eight 0.918
API gravity 21.8
Sulfur, weight ~ 3.2
Viscosity at 37.8C, SSU 370
Ramsbottom Carbon, weiyht ~ 10.4
Asphaltenes, weight % 14.7
Vanadium, ppm 270
~ickel ppm 48
20 Kuop (characterization factor) 11.7
Processing a typical crude oil hereunder is carried out in
the following stages:
A 100% crude oil stream is treated by
distillation. A stream of gas and distillate fractions
with the following characteristics is obtained:
DEGREE OF FRACTIO~ YIELDAPI GRAVITY
VOL.%
Gas (IBT-5C) 1.0
Gasoline (50-210C) 19.5 57.7
30 Kerosene (210-290C) 10.5 38.8
- Diesel (290-400C) 15~5 27.5
Heavy gas oil (400-470C) 7.5 27.1
From atmospheric distillation bottoms a residue
with a yield of 53.5 volume ~ and a 400C IBT tInitial
Boiling Temperature) is obtained. The residue is composed
as follows:
ILZ~4~2
COMPOSITION
Ramsbottom carbon, weight % 19.7
Viscosity, SSF at 50C 70,000
Specific weight, 20/4C 1,026
API gravity 6.0
Metals, Fe, ppm 27
Metals, Cu ppm 2
The extract produced under these conditions has
the following characteristics:
EXTRACTEXTRACT
(1) (2)
API gravity 12.113.5
Viscosity, SSF at 50C 381 732
nC5 insolubles, weight % 2.2 3.2
nC7 insolubles, weight % 0.9 0.4
Ramsbottom Carbon, weight % 7.5 7.9
Sulfur, weight % 3.53.9
Metals (Ni ~ V), ppm 120 131
Yield, vol. % 65.4-67.3 63.0-69.6
The residues produced at 400C and 470C from the
extraction of bottoms after treatmant with solvents, has
the following characteristics:
BOTTOMSBOTTOMS
(1) (2)
Density (Beckman) 1.0711.13
Ramsbottom carbon, weight ~ 40.0 42.1
nC5 insolubles, weight % 70.2 77.2
nC7 insolubles, weight ~ 60.0 63.6
Qils, weight ~ 16.5 9.3
Resins, weight % 13.9013.6
Metals, (Ni + V), ppm 1574 1899
Sulfur, weight % 6.7 7.0
Carbon/Hydrogen, weight ~ 8~96 10.76
Gross Heat value (BTU/lb) 16,811 16,341
Melting point, C 153 160
Yield, vol. % 34.035.0
`:~
12~6~2
- 12 -
The extract derived from the extraction treatment
with solvents is immediately subject to conventional
vacuum distillation, catalytic cracking and viscosity
breaking stages.
During the vacuum distillation a gas oil fraction
with a 540C IBT (Initial Boiling Temperature) and a 40-41
volume ~ (1) and 36-38 volume ~ (2) yield is produced.
Comparative characteristics of a feedstock
(vacuum gas oil of catalytic cracking from a light crude,
with feedstock into catalytic cracking from a light crude,
with feedstock into catalytic cracking from heavy crude
oil extracts treated with this method) are described in
Table 1.
VACUUM GAS OIL
LIGHT CRUDE EXTRACT EXTRACT
(1) (2)
API gravity 25.5 19.6 18.9
Ramsbottom carbon, weight % 0.4 0.3 0.3
nC5 insolubles, weight % 0 0 0
Sulfur, weight % 2.0 2.5 2.7
Viscosity, SSU, 98.9C 36 52 55
Metals (Ni + V), ppm 0.6 1.4 1.5
Metal factor 3.0 4.2 5.4
Residue in the vacuum distillation unit with a
540C FBP (Final Boiling Point) has a 59-60 volume % (1)
and 62-64 volume % (2) yield.
According to the results shown on the above
table, it may be seen that extracts from vacuum
distillation produced by the technique to process heavy
crude oils under this invention, virtually exhibit the
same major characteristics of a vacuum extract derived
from light crude oils. Among these characteristics a
trend to carbonization is noticed in both cases with very
similar values, i.e.:
~t;4~3~
- 13 -
LIGHT CRUDEEXTRACT EXTRACT
(1) (2)
Ramsbottom carbon weight % 0.4 0.3 0.3
Likewise, it may be seen in the table that the
asphaltene contents is nil in both cases, that is:
LIGHT CRUDE EXTRACT EXTRACT
(1) (2)
nC5 insolubles, weight 0 0 0
In order to better illustrate the invention, in
the following examples the various modes to carry out the
heavy crude oil processing are described. Of course this
does not limit the scope of the invention.
EXAMPLE 1
A 100~ feedstock with heavy crude oil is
prepared. It has the following characteristics.
Specific weight, 20/4C 0.920
API gravity 22.6
Sulfur, weight ~ 3.1
Viscosity at 37.8~C, SSU 380
20 Ramsbottom carbon, weight % 10.7
Asphaltenes, weight % 14.7
Vanadium, ppm 283
Nickel, ppm 51
Kuop 11.7
This feedstock is immediately subject to
atmospheric distillation to obtain a stream with gas and
distillate fractions having the following characteristics:
DEGREE OF STRIPPING FRACTIONPRODUCT YIELD
VOL. %
30 Gas (IBT 50C) 1.0
Gasoline (50-210C) 19.5
Kerosene (210-290C) 10.5
Diesel (290-400C) 15.5
Heavy gas oil (400-470C) 7.5
Residuum ~70C + 46.0
;~
~.
6~32
- 14 -
With selective solvents comprising an isopentane
(iC5) and normal pentane (nC5) mixture, the resulting
residue is immediately trea~ed, to extract asphaltenes,
carbon, sulfur, and metals, under the following conditions:
Top temperature, C 138-142C
Bottom temperature, C 118-122C
Solvent/Hydrocarbon Ratio, vol/vol 4:1-7:1
Pressure, Kg/cm2 22-24
The results obtained and the feedstock and
product properties in this extraction stage are listed
below:
FEEDSTOCK RESIDUE EXTRACT BOTTOMS
IBT:470C
Yield, vol. % 100.0 64.0 36.0
API gravity 4.92 12.9 __
Specific weight, 20/4C 1.0342 0.977 1.130
Viscosity SSF C 504 x 105 828 --
82.2 8,850 100 --
98.9 1,980 -- --
Total sulfur, weight % 4.7 4.2 6.7
Ramsbotton carbon, weight % 19.9 7.9 39.3
Water and sediment, Vol. % 0.3 0.2 -~
nC5 insolubles, weight % 28.3 1.1 76.3
nC7 insolubles, weight % 20.9 0.4 60.0
2~ Oils, weight % 42.0 64.9 10.3
Resins, weight % 29.7 34.0 13.4
Metals, ppm Fe 45 16.2 --
Cu 1.0 0.3 --
Ni 108 14.2 275
V 642 100 1600
Ductility, cm 150
Softening point, C 50 -- 150
Penetration 100/5/25, 0.1 mm 0
Pour point, C -- +12 --
Carbon, weight % 82.2 83.1 82.2
Hydrogen, weight % 9.3 10.2 9.5
~r
~Z46~
- 15
~itrogen, weight % 1.0 0.5 0.5
Basic nitrogen, ppm 1600 987 2473
Benzene insolubles, weight % 0.0 0.0 0.0
Polars, weight ~ 29.7 34O0 13.4
Saturates, weight ~ 13.6 19.6 2.8
Aromatics, weight ~ 28.3 45.2 7.5
Fixed carbon, weight %10.5 0.30 28.9
Ash, weight % 0.10 0.04 0.20
Gross heat value, BTU/lb 17,41618,584 16,175
Cal/g 9,68210,331 8,992
Thereafter, the extract obtained continues its
refining processing in vacuum distillation, catalytic
cracking, and viscosity breaking units, and the coking,
asphalt preparation and fuel oil units.
Vacuum Distillatio~. In this stage a gas oil is
pro~uced (FBT-540C) with a 37.8 v~l. yield and a 62.9
vol. % residue (IBT-540C).
Following below are the major characteristics of
gas oils and residues derived from this stage.
470C
TYPE OF FEEDSTOCKGAS OIL RESIDUE
CHARACTERISTICS
API gravity 18.58 7.2
Specific weight 20/4C0.938 1.0173
Viscosity, 37.8Cgoo,ooo
Viscosity, 98.9C 55 7,950
Total sulfur, weight % 2.7 4.5
Ramsbottom carbon, weight ~ 0.3 15.3
nCs insolubles, weight % 0.0 8.6
Metals, ppm Fe 0.8 1.7
Cu 0.05 9.8
~i 10~3 36
V 1.2 199
lZ9~4~;~
- 16 -
Flash point, C 204 ~~
Aniline point, C 72 --
Benzene insolubles, weight % -- 0-07
Ash, weight ~ 0.06 0.07
EXAMPLE 2
Following the same technique as in example 1, the
resultant atmospheric residue is treated with a different
aliphatic hydrocarbon, such as normal pentane to extract
asphaltenes, carbon, sulfur and metals and the following
results are obtained:
c5
TYPE OF SOLVENTFEEDSTOCKEXTRACT BOTTOMS
Yield t vol. ~ 100~0 71.3 28.7
API gravity 4.92 11.8 --
Specific weight, 20/4C 1.0342 0.985 1.150
Viscosity, SSF C 504 x 105 -- --
82.2 8,850 --- --
98.g 1,980 -- --
Total sulfur, Weight % 4.7 4.4 6.8
Ramsbottom carbon,
weight ~ 19.9 10.6 40.6
Water and sediments,
vol. % 0.3 0.1 --
nCs insolubles,
weight ~ 28.3 7.7 79.4
nC7 insolubles,
weight % 20.9 4.3 62.1
Oils, weight ~ 42.0 59.1 9.4
Resins, weight ~29.7 33.2 11.2
Metals, ppm Fe 45 7.5 --
~t;4~;~Z
- 17 -
Cu 1.0 0.5 --
Ni 108 25 300
~ 642 130 1900
Ductility, cm 150 -- --
Softening point 50 -- MI
Penetration 100/5/25,
0.1 mm 380
10 Pour point, C -- +12 __
Carbon, weight % 82.2 81.0 81.9
Hydrogen, weight % 9.3 10.3 10.3
Nitrogen, weight % 1.0 0.5 0.5
Basic nitrogen, ppm1600 1077 2550
Benzene insolubles,
weight % o.o o.o o.o
Polars, weight % 29.7 33.2 11.2
Saturates, weight %13.6 17.5 3.6
Aromatics, weight ~28.3 41.6 5.8
Fixed carbon, weight %10.5 0.7 34.4
Ash, weight % 0.10 0.03 0.30
Gross heat value, BTU/lb 17,416 18,450 17,244
CAL/g 9,682 10,257 9,586
The extract derived continues being processed
into the following stages of vacuum distillation,
catalytic cracking, viscosity breaking, coking, asphalt
preparation, and fuel oils..
EXAMPLE 3
Following the same techniques as in example 1,
the atmospheric residue is treated with an aliphatic
solvent such as normal hexane, nC5 with the following
results:
~2~69182
- 18 -
TYPE OF SOLVENTFEEDSTOCK EXTRACT BOTTOMS
Yield, vol.% 100.0 74.9 25.1
API gravity 4.92 11.2 --
Specific weight,
20/4C 1,0342 0.989 l.l70
Viscosity, SSF, C 504 x 105 2370 --
82.28,850 234 --
98.91,980 --
Total sulfur, weight ~4.7 4.45 6.9
Ramsbottom carbon,
weight % 19.9 11.4 42.4
Water and sediments,
~ol. % 0.3 0.1 --
nCs insolubles,
weight % 28.3 10.3 82.0
nC7 insolubles,
20 weight % 20.9 6.0 65.4
Oils, weight ~ 42.0 56.4 8.9
Resins, weight % 29.7 33.3 9.1
Metals, ppm Fe 45 6.0 --
Cu 1.0 1.3 __
Ni 108 31 330
V 642 160 2080
Ductility, cm 150 -- --
30 Softening point, C 50 -~ --
Penetration l00/5/25,
0.1 mm 380 -- --
Pour point, C -- +15 --
35 Carbon, weight % 82.2 82.8 81.8
`i~
- 19 ~Z46~8~
Hydrogen, weight %9.3 10,2 9 0
~itrogen, weight %loO 0~5 0~5
Basic nitrogen, ppm1600 1255 2689
Benzene insolubles,
weight ~ 0.0 0.0 0.0
Polars, weight % 29~7 33~3 9~1
Saturates, weight %13~6 15~2 3~3
Aromatics, weight ~28~3 41~4 5~6
Fixed carbon, weight % 10~5 2~1 36~8
Ash, weight % 0.10 0. 04 0~37
Gross heat value, BTU/lb 17~416 18~154 16~905
CAL/g 9, 682 10,092 9~398
Extract continues its processing into the
following stages: vacuum distillation, catalytic
cracking, and viscosity breaking.
EXAMPLE 4
The same technique as in example 2~ The
atmospheric residuum is treated with an aliphatic solvent,
such as a normal heptane nC7 with the following results:
TYPE OF SOLVENTFEEDSTOCK EXTRACT BOTTOMS
Yield, vol. % 100.0 78~6 21~4
API gravity 4~92 10.5 ~~
Specific weight, 20/4C 1~0342 0~994 1~182
Viscosity, SSF C 504 x 105 3270
82~28~850 285 ~~
98~91,980 118 ~~
Total sulfur, weight % 4~7 4~5 7~0
Ramsbottom carbon weight ~ 19.9 11. 8 44~3
64~2
- 20 -
Water and sediments, vol.~ 0.3 0.1 ~~
nCs insolubles, weight % 28.3 12.1 87.8
nC7 insolubles, weight % 20 9 6.7 72.4
Oils, weight % 42.0 55.7 6.7
Resins, weight % 29.7 32.2 5.5
Metals, ppm Fe 45 11.0 --
Cu 1.0 0.5 --
Ni 108 37 360
V 642 175 2300
Ductility, cm 150
Softening point, C 50 -- --
Penetration 100/5/25,
0.1 mm 380 -- --
Pour point, C -- ~21 --
Carbon, weight % 82.2 83.3 83.7
20 Hydrogen, weight % 9.3 10.8 9.3
Nitrogen, weight ~ 1.0 0.5 0.5
Basic nitrogen, ppm1600 1343 2700
Benzene insolubles,
25 weight % 0 0 0 0 0 0
Polars, weight % 29.7 -- --
Saturates, weight %13.6 -- 2.7
Aromatics, weight %28.3 -- 4.1
30 Fixed carbon, weight %10.5 -- --
Ash, weight % 0.10 0.03 0.4
Gross heat value BTU/lb 17,416 18,148 16,984
CAL/g 9,682 10,089 9,442
~ ~.
~6~3Z
- 21 -
Extract produced continues its processing into
the following stages; vacuum distillation, catalytic
cracking and viscosity breaking.
" , . ,~
.
