DE3444721A1 - Process for treating heavy crude oils - Google Patents

Abstract

A process for treating heavy crude oils by atmospheric distillation, vacuum distillation and catalytic cracking is described, in which the residue from atmospheric distillation is treated in a separate step with aliphatic solvents for selective extraction of asphalts, carbon, sulphur and metals. After removal of the impurities, the process is continued in the following stages: the extract is fed to a normal vacuum distillation unit; the vacuum gas oil stream is fed to a catalytic cracking unit, and the residue from the vacuum distillation is used for reducing viscosity, for coking, for asphalt production and for fuel oil.

Description

INSTITUTO MEXICANO DEL PETROLEO Mexico o773o, D.F., Mexico

Process for processing heavy crude oils

The invention relates to a method for processing heavy crude oils by atmospheric Distillation, vacuum distillation and catalytic cracking. The procedure is through a special Stage characterized in which a residue of atmospheric distillation, which is essentially Contains asphaltenes, sulfur and metals such as iron, copper, nickel and vanadium in one Unit for selective solvent extraction and removal of the impurities is fed. After removing the impurities, the procedure is carried out according to the following stages: The extract obtained is fed into a normal vacuum distillation unit; the gas oil flow from the vacuum distillation is fed into a catalytic cracking unit and the residue becomes further processed, e.g. B. by viscosity reduction, coking and production of asphalt and Heating oil.

0227-199 652-K-Bk

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The process for processing heavy crude oils with a high content of asphaltenes (over 7% by weight ; insoluble in nC ^ hydrocarbons) is characterized by the removal of impurities in a stage of selective solvent extraction, whereby an extract whose properties correspond to those of a light crude oil residue from atmospheric distillation (with a lower content of asphaltenes), and a stream can be obtained in which the impurities of the crude oil are concentrated in the sump.

The world's increasing demand for energy and some breakthroughs in technology have been developing encouraged by increasingly complex processes in which distillates derived from crude oils and residues are completely recovered.

The needs of the oil industry have changed in many ways over the years; there are currently greater ones Amounts of heavy crude oils present.

A crude oil is a mixture that has as its main component some hydrocarbons and a minor one Contains compounds that have elements such as sulfur, nitrogen, oxygen, Contains vanadium, nickel, iron and copper. In general, a crude oil with a high specific gravity called heavy crude, which means that the existing low-boiling point Hydrocarbons are present in lesser amounts than in oils known as light crude oils are. In defining such a heavy crude, however, the chemical nature of its

34ΑΪ721

ties are not taken into account and consequently its quality is not precisely defined, even then, when the analysis includes data that would normally determine the quality of the crude oil.

With the same specific weight or the same API density, the quality of a Crude oil can vary widely as product yields can vary greatly or the presence of some Product types add materially to the cost of processing and occasionally the normal refining process partially or fully affect.

Crude oils show at their various stages of recovery special behavior on; these depend on the type and the physicochemical properties of hydrocarbons.

The main stages in the processing of crude oils are manufacture, processing, refining and marketing.

Traditionally, light and medium hydrocarbons have been recovered; the recovery of heavier crude oils required the development of new technologies to make these reserves commercially available to be able to exploit. Light and medium crude oils can be easily dewatered and transported through pipes will. In contrast, heavy crude oils are popular because of their high viscosity and specific gravity difficult to handle and require expensive transportation systems. They are also used for heavy crude oils, in particular for those with a high content of asphaltenes, special processing systems are necessary. That's why indicates the global marketing of heavy crude oils

special properties.

As stated above, the standard processes are based on the extraction of light and medium-bodied liquids Hydrocarbons. The refineries for processing these products are typical geared towards the production of fuels and consist of the following refining processes: Atmospheric distillation, vacuum distillation of residues from atmospheric distillation, Upgrading gasoline by catalytic cracking of vacuum gas oils and reducing the viscosity of the Vacuum distillation residues.

The object of the invention was to provide a method for processing heavy crude oils with a high asphaltene content, which is carried out according to the following stages: atmospheric distillation, selective extraction with solvents, vacuum distillation and viscosity reduction, ^and in which it is possible to obtain an extract whose asphaltene and metal content corresponds to that of a light crude oil residue from atmospheric distillation. In addition, in the process according to the invention, the yields of distillate should be increased compared to conventional processes for processing heavy crude oil.

The object was achieved according to the invention.

The invention thus relates to a method for processing heavy crude oils atmospheric distillation, vacuum distillation and catalytic cracking, with the starting

Starting material 100% heavy crude oil with a content of insoluble in n-Cr hydrocarbons compounds of at least 7 % is fed, which is characterized in that the residue from the atmospheric distillation is immediately mixed with aliphatic solvents for the selective extraction of asphaltenes, carbon, sulfur and metals is treated under the following conditions:

Head temperature: 50 to 250 ⁰ C,
Temperature at the column foot: 40 to 230 ⁰ C, volume ratio of solvent to hydrocarbon: 2: 1 to 10: 1,
Pressure: 3 to 40 kg / cm ² ,

where over the top of the column an extract with the following properties:

API density: 10 to 18 °;

SSF viscosity at 50 ⁰ C: 100 to 3500, in n-Cr-hydrocarbon insoluble compounds: 1.0 to 75 parts by weight I,

Compounds insoluble in n-CL hydrocarbons: 0.20 to 5.0% by weight,

Ramsbottom carbon: 4.0 to 12.0% by weight, sulfur: 2.0 to 5.0% by weight ?,
Metals (Ni, V): 75 to 250 ppm,

and a residue with the following properties is obtained at the foot of the column:

Density: 0.9 to 1.4,

Ramsbottom carbon: 30 to 50% by weight, compounds insoluble in n-Cr hydrocarbons:

60 to 90 wt. ° s,

Compounds insoluble in n-C hydrocarbons:

50 to 80% by weight,

Metals (Ni, V): 750 to 3000 ppm, sulfur: 5 to 8% by weight,
Melting point: 120 to 200 ⁰ C,

the extract obtained from the solvent extraction is subjected to a normal vacuum distillation, in this unit at an initial temperature of 300 ⁰ C and an end temperature of 540 ⁰ C a gas oil stream, which is fed into the catalytic cracking columns, and at the foot of the column at eiixer Temperature of 540 ⁰ C a residue is obtained, which is fed to the viscosity reduction.

In the process according to the invention, heavy crude oils with a high content of asphaltenes are processed on a paraffinic or naphthenic basis. In the first stage of the process, the crude oil is subjected to distillation under atmospheric pressure, a residue with an initial boiling ^{temperature of 300 to 470 °} C. being obtained. Immediately thereafter, the residue is subjected to a selective extraction with C 1-4 aliphatic solvents or one of their mixtures, an extract being obtained overhead whose properties correspond to those of a residue from an atmospheric distillation of a light crude oil. The extract obtained from the solvent extraction is immediately fed to further refining stages, such as vacuum distillation and catalytic cracking. The residues from vacuum distillation are fed into units for viscosity reduction, coking and for the production of asphalt and heating oils. At the foot of the extraction column, a stream is obtained in which the

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impure of the crude oil are concentrated.

The method according to the invention allows to process crude oil in conventional, easy-to-handle process units and to add residues refine and in this way the growing reserves of crude oils with a high content of Exploit asphaltenes and metals. The reserves of light crude oils take in various oil-producing Countries, whereas the reserves of heavy crude oil are increasing. Refining this Crude oils are made by various processes.

At the moment the crude oils are divided into different classes. From a commercial point of view The crude oils were classified according to their API density in light C> 30 ° API), medium (20 - 30 ° API), heavy (10 - 20 ° API and super heavy (<10 ° API) crude oils are divided. But there are also classifications, the characterization factor, the correlation index and the viscosity-density constant, which indicates the chemical composition. In these classifications Also includes paraffinic, mixed and naphthenic based crude oils.

The classifications available up to now give neither the distillates for each crude oil nor the one to be used Degree of refinement for an economical process. Hence, an arbitrary classification from a procedural point of view could indicate that a heavy crude oil is present when vacuum residues arise that are necessary for the production of commercially available Heating oil is an uneconomical dilution

to necessitate. According to the commercial classification, heavy crude oils have a density below 20 ° API on. Other properties for heavy crude oils are: their high viscosity, their high content of metals and especially of nickel and vanadium, their sulfur content and abundance of carbon residues consisting of asphaltenes and Ramsbottom or Conradson carbon. It was found that from the vacuum distillation residues of all heavy crude oils amounts of over 35 volume-I of heating oils with a SSF viscosity of 500 SSF can be obtained (SSF; Saybolt-Furfurol seconds).

In addition, a heavy crude can be said to exist when its processing is secondary to refining required, such as extraction with selective solvents to remove asphaltenes and impurities or catalytic processes to separate undesired compounds, like carbon, sulfur and metals.

The presence of impurities in heavy crude oils severely affects the various stages of refining. For example, sulfur deteriorates because of the effects of some sulfur compounds at high temperatures Corrosion caused complete recovery of the distillate from the first distillation. In this In this case, special and expensive alloys are necessary for the process equipment. Distillates that contain these compounds must be treated further to remove them, otherwise the Not meeting quality requirements.

The influence of these impurities makes itself felt

at the secondary refining stages, which are conventional are used in refineries to recover additional quantities of gasoline. your attendance limits the recovery of the feed material to be recycled, since in most cases catalysts are used, which are easily poisoned by the impurities and especially by metals and deactivated.

For heavy industrial heating oils, which are usually made from asphalt residues, makes The presence of harmful compounds in heavy crude oils is noticeable in that of normal equipments to burn heavy fuel oils. There will also be accelerated corrosion established.

For hydrocarbons with a low ratio from hydrogen to carbon, the asphaltene content of crude oils is an indirect measure of the complexity of the refining system and the stringent processing conditions to be applied of heavy crude oils.

In other words, a heavy crude oil with a low asphaltene content is easier to refine than a crude oil with the same API density, but which has a higher asphaltene content.

A measure of the behavior of crude oils when processed in large-scale processes that include a Include heating, is the value of the Ramsbottom carbon, which for practical purposes as the

can be specified for carbonization. This means, that with a high Ramsbottom carbon number, many of the hydrocarbons of a crude oil with distillable hydrocarbons are not obtained by distillation as carbonization occurs when the temperature is increased to the necessary value.

Asphaltenes have very high molecular weight compounds made of carbon, hydrogen, nitrogen and oxygen and metals, their content can be determined by determining the compounds insoluble in pentane and heptane can be specified. As stated above, asphaltenes in a heavy crude cause upon refining many problems.

The analysis of heavy crude oils gives different values for the asphaltene content. this also applies to the Ramsbottom carbon value. Although, on the other hand, distillates from the atmospheric Distillation of a typical heavy crude oil is comparable to the distillates of light oils, as regards its properties in relation to its usefulness as a fuel, there is big difference in chemical composition of vacuum gas oil. The gas oil made from heavy crude oil contains more aromatic compounds and consequently has a higher ratio of carbon to hydrogen on.

This ratio indicates the tendency to carbonization and this increases with heavier fractions Ratio continues. One can conclude from this, without taking into account the asphaltene content, that heavy gas oils from heavy crude oils, because of theirs

high carbon to hydrogen ratios tend to carbonize; they also have a high viscosity because they contain a large amount of polyaromatics.

Some properties of heavy crude oils and theirs resulting from normal processing Distillates and residues are described below:

Crude oil :

A heavy crude with an API gravity of 21.8 ° can be viewed as a heavy crude between a paraffinic and a naphthenic. This is shown by the characterization _{factor (K U (} -.p = 11.7). The content of impurities is high, e.g. sulfur (3.2% by weight), Ramsbottom carbon (10.4% by weight), metals such as nickel and vanadium (350 ppm) and compounds which are insoluble in nC “-carbons (14.7% by weight). Low yields are to be expected when obtaining atmospheric distillates (46% by volume!).

Petrol:

Gasolines made from the crude oils listed above have a high sulfur content (280 to 2800 ppm).

Turbine fuels:

High sulfur values (2900 to 3800 ppm) and freezing points (-38 to -4 8 ^° C.) are observed. The flash point (50 to 70 ⁰ C) and the content of aromatic compounds (18 to 21 vol- ume!) Are good.

Kerosene:

These fractions have acceptable sulfur levels (from 0.38 to 0.65 wt!) And flash points (60 and 89 ⁰ C). The smoke index is low (14 to 15 mm).

Diesel:

High sulfur values (0.54 to 1.6 wt. S) and a normal pour point (-42 to 0 ° C) are observed. What den_.Cetaneindex (47.5 to 51.5) and the carbon residues (0.017 to 0.060 wt. for that matter, these fractions are of good quality.

Heavy distillates:

The metal content is low (Ni + V = 1 ppm), in contrast to the sulfur content (2.2 to 2.9% by weight!) The viscosity index (60 to 69) indicates the possibility of obtaining paraffinic lubricating oils.

Residues:

The residues obtained from vacuum distillation have a high content of sulfur (3.8 to 5.0% by weight!), Metals (Ni + V = 500 to 800 ppm) and compounds insoluble in pentane (20 to 33% by weight!) !) The viscosity at 98.9 ⁰ C from 340 to 50,000 mm ~ ² / s (340 to 50,000 cS).

From this nian can conclude that a heavy crude oil because of its chemical properties in industrial Refining process tends to carbonize. Because of its high metal content, of vacuum distillation gas oil with high metal

concentrations that affect the operation of catalytic crackers. In the invention Process it is now possible to remove these products from heavy crude oils, i.e. from oils with high Ramsbottom carbon values and high levels of asphaltenes and metals, so that the processes

to which the crude oil is subjected during its refining can work so economically, as is the case with a typical light crude.

The main characteristics of one in the invention Methods of processing heavy crude oil are given below:

Crude Oil Analysis

Specific gravity 0.918

API density., ° 21.8 sulfur, weight I 3.2

Viscosity at 37.8 ⁰ C, SUS 370

Ramsbottom carbon, by weight! 10.4

Asphaltenes, wt. S 14.7

Vanadium, ppm 270

Nickel, ppm 48 Kuop (characterization factor) 11.7.

The processing of a typical crude oil is carried out in the following stages:

A stream of 100 % crude oil is subjected to distillation to give a gas stream and distillate fractions having the following properties:

"3U4721

19.5 57.7 10.5 38.8 15.5 27.5 7.5 27.1

Degree of fractionation Yield API density

CVoI.-ξ) (°)

Gas (initial boiling .. _Q

temperature 5 ⁰ C) '

Petrol (50 - 210 ⁰ C) kerosene (210 - 290 ⁰ C) diesel (290 - 400 ⁰ C) heavy gas oil (400-470 ⁰ C)

From the bottom of the atmospheric distillation, a residue with a yield of 53.5 volume I and an initial boiling ^{temperature of 400 0} C is obtained, the composition of which is as follows:

composition

Ramsbottom carbon, wt% 19.7

Viscosity, SSF at 50 ⁰ C 70,000 specific weight, 20/4 ⁰ C 1.026

API density, 6.0

Metals, iron, ppm 27

Copper, ppm 2.

The extract obtained under these conditions has the following properties:

O ⁰ C extract
(1) extract
(2) API density, SSF at 50 12.1 13.5 Viscosity, 381 732

Compounds insoluble in n-C5 hydrocarbons, weight I ''

insoluble in n-Cy hydrocarbons Compounds, Weight I 0.9 0.4

Ramsbottom carbon, weight I 7.5 7.9

34U721

Sulfur, I wt. Metals (Ni + V), ppm yield (vol.-2)

extract
(1) extract
(2) 3.5 3.9 120 131 65.4-67.3 63.0-69.6

The residues, which were obtained at 400 ^° C. and 470 ^° C. by extraction of the sumps after the treatment with solvents, have the following properties:

Residue
(D Residue
(2) 1, 071 1, 13 40.0 42.1

7 7?

Density (Beckman) Ramsbottom carbon, wt. -% compounds insoluble in n-Cr hydrocarbons, wt. % compounds insoluble in n-Cy hydrocarbons, wt. -% 60.0 oils, I weight resins, ξ weight metals (Ni + V), ppm sulfur (I weight)

Carbon / hydrogen, wt

Combustion value, J / g (BTU / lb)

Melting point, ⁰ C yield, % by volume

The extract from the solvent extraction is immediately subjected to conventional vacuum distillation, a subjected to catalytic cracking and viscosity reduction.

: .-% 60.0 63.6 16.5 9.3 .13.90 13.6 1574 1899 6.7 7.0 8.96 10.76 39,148
(16,811) 38.051
(16,341) 153 160 34.0 35.0

During the vacuum distillation is I by volume (1) and 36 to 38 obtain a gas oil fraction having an initial boiling point of 540 ⁰ C, in a yield from 40 to 41 vol I (2).

This gas oil fraction, according to the invention by Extraction of heavy crude oil is obtained using a vacuum gas oil fraction from light crude oil compared. Both gas oils serve as feed material for the catalytic cracking:

Vacuum gas oil

light crude extract extract oil (1) (2)

API density, ° 25.5 19.6 18.9 Ramsbottorn coals
fabric, weight ξ 0.4 0.3 0.3 in n-Cr hydrocarbons
unsolvable substances
connections,
Weight I ° 0 0 Sulfur by weight! 2.0 2.5 2.7 Viscosity at
98.9 ⁰ C, SUS 36 52 55 Metals (Ni + V),
ppm 0.6 1.4 1.5 Metal factor 3.0 4.2 5.4

In the vacuum distillation, a residue with a final boiling point of 540 ⁰ C, in a yield from 59 to 60 vol ° s (1) and 62 to 64 vol ° s (2) is obtained.

From the tables given above it can be seen that the extracts from vacuum distillation, which are im Process according to the invention obtained from heavy crude oils will have practically the same essential properties as a vacuum extract of light weight Has crude oils. In both cases, there is a tendency towards carbonization with very similar ones Values:

light extract extract crude oil (1) (2)

Ramsbottom coal _Λ . _n , _{n 7} fabric, weight I ^ü ' ^{4 ü} > ^{6 U} ' ³

Accordingly, the table shows that no asphaltenes are present in either case:

light extract extract crude oil (1) (2)

in n-Cr hydrocarbon

Substancesü insoluble 0 0 0.

Connections (weight!)

The following examples illustrate the invention.

example 1

The feed material is 100-ply heavy Crude oil used with the following properties:

Specific gravity, 20/4 ⁰ C 0.920

API density, ° 22.6 sulfur, weight S 3.1

Viscosity at 37.8 ⁰ C, SUS 380

Ramsbottom carbon, wt -5 10.7

Asphaltenes, weight I 14.7

Vanadium, ppm 283 nickel, ppm 51

Kuop 11.7.

This feed material is immediately subjected to atmospheric distillation with a gas stream and distillate fractions with the following properties are obtained:

Fractionation degree product yield

Gas (initial boiling ^{temperature 50 °} C.) 1.0

Petrol (50 - 210 ⁰ C) 19.5

Kerosine (210-290 ⁰ C) 10.5

Diesel (290 - 400 ⁰ C) 15.5 Heavy gas oil (400 - 470 ⁰ C) 7.5

Residue (above 470 ^° C.) 46.0.

The resulting residue is immediately treated with a mixture of isopentane (1-C ₅ ) and n-pentane (n-Cr) to extract the asphaltenes, carbon, sulfur and metals under the following conditions:

Head temperature, C 138-142

Temperature at the bottom of the column, ⁰ C 118-122

Volume ratio of solvent to hydrocarbon 4: 1 - 7: 1

Pressure, kg / cm 22-24.

The properties of the material fed in, as well as the products obtained after extraction are given below:

Residue
Initial boil
temperature
470 ° C Yield, vol-I 100.0 extract , 0 swamp API density, ⁰ 4.92 64 , 9 36.0 Specific weight,
20/4 ⁰ C 1.0342 12th , 977 - Viscosity, SSF at
50 ⁰ C 4 χ 10 ⁵ 0 1, 130 82.2 ⁰ C 8,850 828 _ - 98.9 ⁰ C 1, SLSO 100 - Total sulfur, weight-2 4.7 __ , 2 - Ramsbottorn carbon,
Weight! 19.9 4th , 9 6.7 Water and sediment,
Vol.-! 0.3 7th , 2 39.3 in n-C - hydrocarbon 0 _ _ substances insoluble 28.3 ,1 1 76.3

bindings, wt

Compound insoluble in n-C_ hydrocarbons gen, wt!

Oils by weight! Resins by weight! Metals, ppm, Fe

Cu

Ni

Extensibility, cm softening point, ⁰ C

Penetration 100/5/25, 0.1 mm

Pour point, ⁰ C carbon, weight-! Hydrogen, weight!

0.4

60.0

42, 0 64, 9 1 10.3 29 7th 34, 0 13.4 45 16, 2 - 1, 0 O, 3 - 108 14, 2 275 642 100 600 150 - - 50 - 150 0 - - - + 12 - 82 , 2 83 ,1 82.2 9 , 3 10 , 2 9.5

Residue
Start you
detempera
temperature 470 ⁰ C .-! 29.7 extract swamp Nitrogen, weight! 1.0 13.6 0.5 0.5 Basic nitrogen, ppm 1600 28.3 987 2473 Compound insoluble in benzene
dungen, by weight! 0.0 10.5 0.0 0.0 Polar compounds, wt 0.10 34.0 13.4 Saturated compounds,
Weight! 40,538
(17,416) 19.6 2.8 Aromatic compounds
Weight! (9,682) 45.2 7.5 Bound carbon,
Weight! 0.30 28.9 Ashes, weight! 0.04 0.20 Combustion value, J / g
(BTU / lb) 43,255
(18,584) 37,650
(16,175) cal / g (10,331) (8,992)

The extract obtained is further refined by vacuum distillation, catalytic cracking, Viscosity reduction, coking, asphalt and heating oil production.

Vacuum distillation: In this stage, a gas oil with a final boiling temperature of 540 ⁰ C in a yield of 37.8 vol.! and a residue with an initial ^{boiling temperature of 540 0} C in a yield of 62.9 vol.! which have the following properties:

470 ⁰ C gas oil residue

API density; ³

Specific weight 20/4 ⁰ C, viscosity at 37.8 ⁰ C, viscosity at 98.9 ⁰ C, total sulfur, I weight Ramsbottom carbon, I weight in n-Cr hydrocarbons

insoluble compounds, wt. -% ^{0> 0 8} ' ⁶

18th , 58 900 , 7 7th 000 7th , 2 0 , 938 .3 1 4th , 0173 15th 55 .950 2 , 5 0 .3

Metals, ppm, Fe O.
. 0 Ver 0.8 1 , 7 Cu 0.05 9 ,8th Ni 10.3 36 V Be 1.2 199 Flash point, ⁰ C 204 - Aniline point, ° C. 72 - insoluble in benzene bindings, wt - 0 , 07 Ash, wt -.% 0.06 0 , 07. game 2

Following the procedure of Example 1, the residue from the atmospheric distillation is with another aliphatic hydrocarbon, namely n-pentane, for the extraction of asphaltenes, carbon, Sulfur and metals. The following results are obtained:

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Residue
Initial boil
temperature
470 ⁰ C. , Extract swamp Yield, Vo 1.-2 100.0 71.3 28.7 API density, ⁰ 4.92 11, 8 - Specific
20/4 ⁰ C Weight, 1.0342 0.985 1 .150 Viscosity,
50 ⁰ C SSF at
4 χ 10 ^b _ _ _ _ 82.2 ⁰ C 8,850 - - 98.9 ⁰ C 1Γ98Ο _ _

Total sulfur, wt. I 4.7 4.4 6.8

Ramsbottom carbon,

Weight -! 19.9 10.6 40.6

Water and sediment,

Vol.- ° a 0.3 0.1

compounds insoluble in n-CL hydrocarbons, Weight! 28.3 7.7 79.4

in n-Cy hydrocarbon

have insoluble bonds % 100/5/25, Weight-5 20.9 4.3 62.1 gen, Gew.-I , Fe Weight - ° s 42.0 59.1 9.4 oils, by weight! Cu C. 29.7 33.2 11, 2 Resins by weight Ni 45 7.5 - Metals, ppm V 1.0 0.5 - cm 108 25th 300 Softening point, ⁰ C 642 130 1900 penetration 150 - - Extensibility, 0.1 mm 50 - MI Pour point, ° Carbon, 380 - - Hydrogen, - + 12 - 82.2 81, 0 81, 9 9.3 10.3 10.3

Residue
Start you
detempera
temperature 470 ⁰ C 13.6 10.5 extract swamp Nitrogen, weight! 1.0 Aromatic compounds,
Weight! 28.3 0.10 0.5 0.5 Basic nitrogen, ppm 1600 Bound carbon,
Weight! 40,538
) (17,416) 1077 2550 Compound insoluble in benzene
dungen, by weight! 0.0 Ashes, weight! (9,682) 0.0 0.0 Polar connections, by weight! 29.7 Combustion value, J / g
(BTU / lb; 33.2 11, 2 Saturated compounds.
Weight! cal / g 17.5 3.6 41, 6 5.8 0.7 34.4 0.03 0.30 42,946
(18,450) 40.136
(17,244) (10,257) (9,586)

The extract obtained is further processed in the following stages, namely in the vacuum distillation, catalytic cracking, viscosity reduction, coking, asphalt and heating oil production.

Example 5

According to Example 1, the residue from the atmospheric distillation with an aliphatic solvent, like η-hexane, treated with the following results:

Residue
Initial boil
temperature
470 ⁰ C 00.0 extract swamp 6.9 Yield, vol-I 1 4.92 74.9 25.1 42.4 API density _t ° 1.0342 11, 2 Specific weight,
20/4 ⁰ C 4 x 10 ⁵ 0.989 1, 170 Viscosity, SSF at
50 ⁰ C 8,850 2370 82.2 ⁰ C 1,980 234 - 98.9 ⁰ C 4.7 - _ - Total sulfur, wt 19.9 4.45 Ramsbottom carbon,
Weight! 0.3 11.4 Water and sediment,
Vol.- ° s 0.1

Insoluble compounds 28.3 in n-Cr hydrocarbons bindings, wt

in n-Cy hydrocarbon

10.3

82.0

with insoluble compounds: '■ 42.0 6.0 65.4 gen, Gew.-I 29.7 oils, wt 45 56.4 8.9 Resins by weight! 1.0 33.3 9.1 Metals, ppm, Fe 108 6.0 Cu 642 1.3 Ni 150 31 330 V 50 160 2080 Extensibility, cm 380 - - «- Softening point, ⁰ C - Penetration 100/5/25, - _ _ 0.1 mm 82.2 Pour point, ⁰ C 9.3 + 15 __ Carbon, weight! 82.8 81, 8 Hydrogen, weight! 10.2 9.0

Residue
Initial boiling temperature ^{470 0 C}

Extract swamp

Nitrogen, weight! 1.0 0.5 0.5

Basic nitrogen, ppm 1600 1255 2689

compounds insoluble in benzene, weight-! 0.0 x 0.0 0.0

Polar connections, by weight! 29.7 33.3 9.1

Saturated compounds,

Weight! 1-3.6 15.2 3.3

Aromatic compounds,

Weight! 28.3 4 ^ 4 5 ^

Bound carbon,

Weight! 10.5 2.1 36.8

Ashes, weight! 0.10 0.04 0.37

Combustion value, J / g 40,538 42,255 39,349

(BTU / lb) (17,416) (18,154) (16,905)

(cal / g) (9.682) (10.092) (9,398)

The extract obtained is further processed in the following stages: vacuum distillation, catalytic Cracking and viscosity reduction.

Example 4

The procedure is as in Example 2, the residue from the atmospheric distillation is with a aliphatic solvent, namely n-heptane, with the following results:

Residue
Initial boil
temperature
470 ⁰ C I. at 100.0 extract swamp Yield, vol. 4.92 78.6 21, 4 API density, ⁰ Specific weight,
20/4 ⁰ C 1.0342 10.5 - Viscosity, SSF
50 ⁰ C Weight I 4 χ 10 ⁵ 0.994 1, 182 82.2 ⁰ C Ramsbottom carbon,
Weight - ° a 8,850 3270 ._ 98.9 ⁰ C Water and sediment,
VoL- ⁰ S 1, 980 285 - Total sulfur, 4.7 118 - 19.9 4.5 7.0 0.3 11, 8 44.3 0.1 __

compounds in n-C_-insoluble hydrocarbons encryption 28.3 wt -.%

in n-C_ hydrocarbon

12.1

87.8

form insoluble compounds 20.9 42.0 6.7 72.4 gen, Gew.-I 29.7 oils, wt 45 55.7 6.7 Resins, wt 1.0 32.2 5.5 Metals, ppm, Fe 108 ' 11, 0 __ Cu 642 0.5 - Ni 150 37 360 V 50 175 2300 Extensibility, cm 380 - - Softening point, ⁰ C - - - Penetration 100/5/25,
0.1 mm 82.2 - - Pour point, ⁰ C 9.3 + 21 - Carbon, wt 83.3 83.7 Hydrogen, wt 10.8 9.3

Arrears initial boiling temperature ^{470 0 C}

Extract swamp

Nitrogen, weight I 1.0

Basic nitrogen, ppm 1600 compounds insoluble in benzene, weight I

0.0

Polar compounds, wt. I 29.7

13.6 28.3

Saturated compounds, weight ξ ^

Aromatic compounds, weight-1

Bound carbon,

Weight -I 10.5

Ash, wt. ⁰ S 0.10

Combustion value, J / g 40,538

(BTU / lb) (17,416)

cal / g C 9.682)

0.5
1343

0.0

0.03

0.5 2700

0.0

2.7 4.1

0.4

42,242 39,533 (18,148) (16,984)

(10,089) (9,442)

The extract obtained is further processed in the following stages:

Vacuum distillation, catalytic cracking and viscosity reduction.

Claims (7)

Expectations Process for the processing of heavy crude oils by atmospheric distillation, vacuum distillation and catalytic cracking, whereby 100% heavy crude oil with a content of compounds insoluble in n-CL hydrocarbons of at least 7 % is fed in, characterized in that the residue from the atmospheric distillation immediately with aliphatic solvents for selective Extraction of asphaltenes, carbon, sulfur and metals treated under the following conditions will: Head temperature: 50 to 250 ⁰ C;
Temperature at the column foot: 40 to 230 ⁰ C; Volume ratio of solvent to hydrocarbons: 2: 1 to 10: 1; 2
Pressure: 3 to 40 kg / cm, where over the top of the column an extract with the following properties: API density: 10 to 18 °; SSF viscosity at 50 ^° C.: 100 to 3500; Compounds insoluble in n-Cr hydrocarbons: 1.0 to 7.5 wt%; 0227-199 652-K-Bk Compounds insoluble in n-C, hydrocarbons 0.20 to 5.0 wt. !; Ramsbottom carbon: 4.0 to 12.0 weight percent; Sulfur: 2.0 to 5.0% by weight;
Metals (Ni, V): 75 to 250 ppm, and a residue with the following properties is obtained at the foot of the column: Density: 0.9 to 1.4;
Ramsbottom carbon: 30 to 50% by weight !; Compounds insoluble in n-Cr hydrocarbons: 60 to 90% by weight !; Compounds insoluble in n-C ~ hydrocarbons: 50 to 80% by weight !; Metals (Ni, V): 750 to 3000 ppm; Sulfur: 5 to 8% by weight;
Melting point: 120 to 2 00 ⁰ C, the extract obtained from the solvent extraction is subjected to a normal vacuum distillation, with ^{a gas oil stream at the top at an initial boiling temperature of 300 0} C and an end boiling temperature of 540 ⁰ C, which is fed into the catalytic cracking columns, and at the bottom of the column at a temperature of 540 ⁰ C a residue is obtained, which is fed to the viscosity reduction. 2. The method according to claim 1, characterized in that the selective aliphatic solvent can be selected from aliphatic hydrocarbons or one of their mixtures. 3AAA721 3. The method according to claim 1 and 2, characterized in that the selective aliphatic solvent is preferably can be selected from aliphatic hydrocarbons such as pentanes, hexanes and / or heptanes. 4. The method according to any one of the preceding claims, characterized in that the extraction of asphaltenes, carbon, sulfur and metals preferably at a head temperature of 50 to 250 ⁰ C and a temperature at the column foot of 40 to 230 ⁰ C, a volume ratio of solvent to Hydrocarbon of 2: 1 to 10: 1 and a pressure of 3 to 40 kg / cm is carried out. 5. The method according to any one of the preceding claims, characterized in that an extract with a minimum content of asphaltenes and metals in a yield of 60 to 90% by volume, based on the Feed material, is obtained. 6. The method according to any one of the preceding claims, characterized in that an asphaltene-free gas oil and a gas oil that is practically free of metal impurities such as iron, copper, nickel and vanadium, can be obtained. 7. The method according to any one of the preceding claims, characterized in that the extraction of asphaltenes, carbon, sulfur and metals at a head temperature of 138 to 142 ⁰ C and a temperature at the column foot of 118 to 122 ⁰ C, a volume ratio of solvent to hydrocarbon from 4: 1 to 7: 1 and a pressure of 22 to 24 kg / cm.