FR2503734A1 - Crude or other heavy oil converted to lighter crude mixt. - by integrated distn., solvent deasphalting and coking - Google Patents

Abstract

Process is claimed for prodn. from a hydrocarbon mixt., e.g. a crude oil, of a synthetic crude oil, having lower density and lower concns. of sulphur, asphaltenes, and metals than the feed. The process comprises: (i) opt. fractionation of the feed to remove any considerable light fraction: (ii) solvent deasphalting of the feed or of the heavy fraction from (i); (iii) coking of the bituminous phase from (ii) after opt. removing solvent by distn., and (iv) fractionation of the liq. prod. from coking. The synthetic crude comprises (a) the oil phase from (ii),after removing solvent: (b) the low-volatile fraction from (iv) ; and opt. (c) part of the light fraction from (i). A heavy crude oil can be converted, e.g. near the well, to a a more valuable mixt., which is easier to refine.

Description

 The present invention relates to a process for obtaining a liquid product, hereinafter referred to as "synthetic crude oil", from a hydrocarbon product having a higher density.

 "Hydrocarbon product" means a product consisting essentially of hydrocarbons, but which may also contain other chemical compounds which, in addition to carbon and hydrogen atoms, may have heteroatoms, such as oxygen, nitrogen, sulfur, or metals such as vanadium and nickel.

 The term "synthetic crude oil" as employed above is a commonly used term, but does not mean that the synthetic crude oil is derived from a crude oil proper, and may also be derived from, for example, heavy oils having a higher 1500 density. at about 0.93 g / ml, oil shale, oil sands or even coal.

 The current trend in the international oil market is a growing demand for light crude oils of relatively low density. On the one hand, light crudes often contain less troublesome products for their refining such as sulfur or metals such as vanadium and nickel, on the other hand, in the coming years, the sale of light products such as fuels will increase relatively more. quickly than heavy products such as fuels-oils.

 The demand for light crudes therefore increases and their price rises faster than that of heavy crudes.

 It is thus more interesting to transform the heavy crude on the fields of production in light crude before transporting it.

 The heaviest part of the crude oil, which is the residue of the distillation of oil, is composed of a mixture of oil and bituminous compounds.

The oily part and the bituminous part are separated by the so-called deasphalting process, which consists in extracting the oily part from the residue using a solvent. This solvent may be chosen from the group consisting of:
saturated or unsaturated aliphatic hydrocarbons having from 2 to 8 carbon atoms, alone or as a mixture,
- Hydrocarbon mixtures, called distillates, obtained by distillation of crude oil, and having molecular weights similar to those of hydrocarbons having 2 to 8 carbon atoms,
the mixtures of all the hydrocarbons mentioned above.

 The Applicant has devised a means of obtaining synthetic crude oil by a method incorporating a deasphalting step.

 The purpose of the present invention is therefore to obtain synthetic crude oil of lower density from heavier products.

To this end, the subject of the invention is a process for obtaining synthetic crude oil from a hydrocarbon feed having a higher density, said process being characterized in that it comprises the following steps:
a) the possible fractionation of the hydrocarbon feedstock em at least two fractions:
at least one light fraction, containing most of the compounds having the lowest boiling points,
a heavy fraction, containing most of the compounds having the highest boiling points,
b) Solvent treatment ::
or the hydrocarbon feedstock, when the fractionation of the step has not been carried out,
- the heavy fraction when the fractionation of the charge takes place,
said treatment leading to obtaining:
- on the one hand, an oily part,
- on the other hand, a bituminous part,
c) the coking of the bituminous part obtained at "b", leading to obtaining:
- on the one hand, coke,
- on the other hand, from an effluent that is fractionated to give
(1) a first mixture containing hydrogen, hydrogen sulfide and low molecular weight hydrocarbons,
(2) a second mixture of higher molecular weight hydrocarbons than those contained in the first mixture,
d) adding to the oily portion obtained in step "b" at least the second hydrocarbon mixture obtained in step "c" and optionally at least a portion of at least one light fraction obtained in step "a", when the splitting of the charge takes place,
said addition leading to the production of synthetic crude oil.

In the process according to the invention, the deasphalting solvent used, the nature of which has been described previously, can come from:
- from a source external to the unit,
at least in part, at least one light fraction obtained in step "a",
or at least in part, the fractionation of the first mixture obtained from the coker effluent of step "c".

 The invention will be better understood from the following description of Figures 1 and 2 of the accompanying drawings which show, without limitation, two types of units implementing the method according to the invention.

With reference to FIG. 1, a hydrocarbon feedstock arrives in the unit via the line lo
Prior to any treatment, the load may, and even must, in the case where this feed is in particular crude oil, have been treated in a desalter 2, into which it is introduced via line 1, in order to eliminate the salts which contains.

 For this purpose, water is added to the feedstock in line 1 through line 3 in order to dissolve the salts contained in the feedstock. In the desalter, the mixture separates into two phases, an aqueous phase 4 and a hydrocarbon phase 5.

 In the case of fillers having a high density greater than 0.96 g / ml at 150 ° C., it is preferable to dilute the feed by introducing a lighter hydrocarbon diluent via line 6 so as to lower the density of the feedstock. charge and improve the contact between water and the load and promote the dissolution of salts in lteåu and, therefore, their separation. The nature of the diluent as well as the rate of diluent with respect to the feed should be chosen so as to avoid the precipitation of asphaltenes.

 The aqueous phase is removed via line 7 and the line 8 recovering the hydrocarbon feedstock to be treated by the process according to the invention.

The charge of line 8 can then be treated in two different ways, according to its nature:
1) the charge can be sent directly into a liquid-deasphalting liquid extractor 10 via line 9,
2) the charge can be fractionated in a fractionation tower 12 where it is conducted by line 13.

this is particularly the case when the load of line 8 contains light products that is useless return to the deasphalting extractor.

This last case meets
- for very heavy products requiring diluted beech,
- for crude oils not "stabilized" on the production field, that is to say still containing light hydrocarbons.

 Fractionation can be envisaged in two fractions, as shown in FIG. 1, or fractionation in addition to two fractions.

 The operating conditions of this column 12 depend on the nature of the feed of the line 13, as well as the degree of separation that it is desired to obtain using this column, but, of course, these operating conditions are chosen so that to minimize, in the light fraction collected by line 14, at the top of the column, the presence of heavy compounds contained in the oily and bituminous parts, which will be separated later.

The light fraction is conducted in a fractionation tower 15, the function of which will be explained later.

 At the bottom of column 12, line 16 is collected the heavy fraction which is conducted in the liquid-liquid deasphalting extractor 10.

 The subsequent processing of the flows of lines 9 or 16 is identical.

 In the extractor 10, the oily part is extracted from the feedstock supplied via lines 9 or 16 by a solvent which is introduced into the extractor via line 17. This solvent may be a saturated or saturated aliphatic hydrocarbon, having 2 to 8 carbon atoms, preferably 3 to 5 carbon atoms, or hydrocarbon mixtures, known as distillates, obtained by distillation of crude oil and having molecular weights similar to those of hydrocarbons having from 2 to 8 carbon atoms, or the mixtures of all the above-mentioned hydrocarbons.

 The solvent for starting the unit comes from a source external to the unit via line 41. The solvent losses can be compensated either by products from the unit, as will be explained later. or by an external support brought by the line 41.

The pressure inside the extractor 10 can be between 1 and 100 bar absolute, the temperature - 6
solvent between 15 and 300 C, the mass ratio being between 0.1 and 10;
At the top of the extender 10, line 18, the oily portion in solution in the solvent is collected. This mixture is conducted via line 18 in a fractionation assembly 19. For the sake of simplification, this assembly has not been shown in detail, but it generally comprises a regulator controlling a pressure drop, evaporators and a steam distillation column.

 At the outlet of the assembly 19, on the one hand, by the line 20, of the sol.vant, which is recycled to the extractor 10 via the line 17, and on the other hand, by line 21, the oily portion, which is conducted in the mixer 22.

 The precipitated bituminous part and the solvent are recovered at the bottom of the extractor 10 and this mixture is conducted via line 23 in a fractionation unit 24, which generally comprises an oven and an evaporator.

 At the overall outlet 24, on the one hand, via the line 25, solvent is collected, which is recycled to the tractor 10 via the line 17, and, on the other hand, via the line 26, the bituminous part, which is conducted in a coker unit 27.

 This coking unit can be of various kinds, but in the case of an installation using the process according to the invention and located on the field of production of the load, it is more interesting that this unit provides little coke which can be easily used as fuel. This is the case of coking units in a fluidized bed, where the coke produced can be easily handled or even gasified.

 In Figure 1, the coke produced is withdrawn through line 28 and is optionally gasified.

 Effluent, drawn off line 29 and containing hydrogen, hydrogen sulfide and hydrocarbons, is conducted in the middle part of a fractionation tower 34.

 At the top of column 34, line 35 is collected a first mixture containing hydrogen sulfide hydrogen and low molecular weight hydrocarbons.

 A second mixture consisting of hydrocarbons of higher molecular weight than those contained in the first mixture is collected at the bottom of column 34, via line 36.

 The flow of the line 36 is led to the mixer 22 to form the synthetic crude, after a possible hydrogenation when this stream contains too many unsaturated products.

The operating conditions (pressure, temperature) of the column 34 are chosen so that the flow of the line 36 contains few hydrocarbons of 1 to 4 carbon atoms, so that the synthetic crude has a low vapor pressure.
The stream collected by the line 35 can be discharged out of the unit. This is the case, in particular, when the operating conditions (pressure, temperature) of the column 34 are such that the flow of the line 35 is composed of hydrogen, hydrogen sulphide and hydrocarbons with 1 or 2 carbon atoms. After removal of hydrogen sulfide, the rest of the stream can be burned in an oven.

 It is also possible, as shown in the figure, to adjust the operating conditions of the column 34 so that the flow of the line 35 contains heavier hydrocarbons, which can serve as deasphalting solvent, as explained below .

 For this purpose, the flow of the line 35 is conducted in the fractionation column 15, where the content of the line 14 is also fractionated, when the fractionation tower 12 exists.

 In this column 15, the hydrogen sulfide, hydrogen and light hydrocarbons are collected at the top of the column by line 37 and undergo the same treatment as that indicated above.

 The heavier fraction may be conducted at least in part to mixer 22 via lines 38 and 40.

 In this case, the synthetic crude will be composed of the products brought by lines 40, 36 and 21.

 The synthetic crude obtained has a lower density than the starting material and contains less troublesome products, such as sulfur, and especially much less metals like nickel and vanadium, which is very interesting for the subsequent processing of the crude.

 A portion of the products contained in the line 38 can be conducted via the line 39 to the extractor 10, via the line 17, as a deasphalting solvent.

 A portion of the products contained in the line 38 can also be conducted via the line 33, line 6 as diluent of the feed to be desalinated, a possible supplement diluent from the outside of the unit by the line 42.

 With reference to FIG. 2, the hydrocarbon feedstock is a feedstock which, having a high density, must therefore always be added with diluent before entering the desalter.

In this FIG. 2, the elements identical to those represented in FIG. 1 have been identified by the same numbers, assigned the index I,
The beginning of the treatment is the same. it changes at the level of the deasphalting extractor 101.

 The oily portion dissolved in the solvent collected at the top of the 10X extractor is conducted through the line 18t in a fractionation assembly 19 '.

 At the outlet of the assembly 19s, by the line 50, is collected the solvent, which is conducted in a fractionation tower 51, where the fraction collected at the top of the tower 12t is also conducted by the lines 14 '. , when splitting is done. The function of the tower 51 will be explained later.

 At the outlet of the assembly 19, line 211 is collected, the oily portion, which is conducted in a mixer 52.

 The precipitated bituminous part and the solvent are collected at the bottom of the extractor 10 ', through the line 23'. This mixture is conducted via line 23 'directly into a coking unit 53. This form of implementation is advantageous because the bituminous phase is difficult to transfer, in the absence of solvent, from the extractor 10' to the coker unit.

 The coke produced in unit 53 is withdrawn via line 54 and optionally gasified.

 The effluent withdrawn via line 56 and containing hydrogen, hydrogen sulphide and hydrocarbons, is conducted in a fractionation column 57, whose operating conditions are chosen according to the degree of fractionation desired.

 The treatment of this effluent is identical to that made with reference to FIG. 1, with the difference that the mixture collected at the top of column 57 via line 59 is always conducted in a fractionation column 51.

 In this column 51, hydrogen, hydrogen sulfide and light hydrocarbons having from one to two carbon atoms are collected at the top of the column via line 60 and undergo the same treatment as that indicated previously in FIG. .

 The heaviest fraction is collected by line 61.

 Part of this fraction can be conducted to the mixer 52 via line 62.

 Another portion serves as a diluent to the hydrocarbon feedstock and is conducted via line 63 to line 6 '.

 Still another portion serves as a deasphalting solvent and is conducted via line 64 to line 17 'at the entrance to column 10'.

 The stream collected by line 58 at the bottom of column 57, composed of hydrocarbons of higher molecular weight than those contained in line 59, is fed to mixer 22 to form at least part of the synthetic crude, after a possible hydrogenation. when this stream contains too many unsaturated products.

 The line 41 'allows the solvent supply of the extractor 10 at the start of the unit. It can also be used to compensate for solvent losses if the additions from the unit prove to be insufficient.

 Line 42 'allows the supply of diluent at the start of the unit and when the rate of the line 6 is insufficient.

 The synthetic crude consists of the products of lines 211, 62 and 58 and is collected by line 65.

 The following examples are intended to illustrate the invention in a non-limiting manner.

EXAMPLE 1
This example relates to the treatment, by the process according to the invention, of a crude oil, stabilized on the field of production, that is to say containing only about 2% of hydrocarbons having from 4 to carbon, and whose main characteristics are given in Table I below.

TABLE I

<tb> Mass <SEP> volume <SEP> to <SEP> 15 C <SEP> in <SEP> g / ml <SEP> 0.884
<tb>% <SEP> in <SEP> weight <SEP> of <SEP> sulfur <SEP> 2,8
<tb>% <SEP> in <SEP> weight <SEP> of asphaltenes <SEP> (1) <SEP> 3.8
<tb> Residue <SEP>"Conradson"<SEP> in <SEP>% <SEP> in <SEP> weight <SEP> (2) <SEP> 7,9
<tb> Content <SEP> in <SEP> nickel <SEP> in <SEP> ppm <SEP> 16
<tb> Content <SEP> in <SEP> vanadium <SEP> in <SEP> ppm <SEP> 55
<tb> (1) measured according to standard AFNOR T 60 - 115 (2) measured according to standard AFNOR T 60 - 116
The process described in Figure 1 was simulated in a laboratory facility.

 In this test, the crude oil was not fractionated and was deasphalted directly into an autoclave.

 The deasphalting is carried out at a temperature of 850 ° C. at a pressure of 40 bar and with a solvent mass ratio of 1 2 crude oil of 1.27.

The solvent used has the composition which is given in Table II below:

<tb><SEP> TABLE <SEP> II <SEP> Percentage <SEP> molar
<tb> Ethane <SEP> 1.53
<tb> Propane <SEP> 94.71
<tb> Isobutane <SEP> 3.40
<tb> Butane <SEP> normal <SEP> 0.36
<Tb>
An oily part and a bituminous part were thus separated.

 85% by weight of oily part and 15% by weight of bituminous part were obtained.

Their main characteristics are given in Table III below:
TABLE III

<tb><SEP> Part <SEP> Part
<tb><SEP> Oily <SEP> Oily
<tb> Mass <SEP> volume <SEP> to <SEP> 15 C <SEP> in <SEP> g / ml <SEP> 0.857 <SEP> 1.087
<tb>% <SEP> in <SEP> weight <SEP> of <SEP> sulfur <SEP> 2.26 <SEP> 6.47
<tb>% <SEP> in <SEP> weight <SEP> of asphaltenes <SEP> 0.13 <SEP> 31.2
<tb><SEP> Residue <SEP> Conradson <SEP> in <SEP>% <SEP> in <SEP> Weight <SEP> 2.7 <SEP> 34
<tb> Content <SEP> in <SEP> nickel <SEP> in <SEP> ppm <SEP> 2 <SEP> 81
<tb><SEP> Content <SEP> in <SEP> vanadium <SEP> in <SEP> ppm <SEP> 5 <SEP> 287
<Tb>
Coking in a fluidized bed of the bituminous part makes it possible respectively to obtain
- 12% by weight of gaseous effluent: hydrogen, hydrogen sulphide, hydrocarbons of 1 to 4 carbon atoms,
45% by weight of liquid effluent,
43% by weight of coke, which can be gasified.

The main characteristics of liquid effluent are given in Table IV below:
TABLE IV

<tb> Nasse <SEP> volume <SEP> to <SEP> 15 C <SEP> in <SEP> g / ml <SEP>: <SEP><SEP> 0.920
<tb> in <SEP> weight <SEP> of <SEP> sulfur <SEP>: <SEP><SEP> 4,4
<tb> Residue <SEP> Conradson <SEP> in <SEP>% <SEP> in <SEP> Weight <SEP>: <SEP> 3,3
<tb>: Content <SEP> at <SEP> nickel <SEP> at <SEP> ppm <SEP>: <SEP><SEP> traces
<tb> Content <SEP> in <SEP> vanadium <SEP> in <SEP> ppm <SEP> traces
<Tb>
This liquid effluent was then mixed with the oily part and a synthetic crude oil was obtained, the characteristics of which are given in FIG.
Table V below:
TABLE V

<tb> Mass <SEP> volume <SEP> to <SEP> 15 C <SEP> in <SEP> g / ml <SEP> 0.860
<tb>% <SEP> in <SEP> weight <SEP> of <SEP> sulfur <SEP> 2,4
<tb>% <SEP> in <SEP> weight <SEP> of asphaltenes <SEP><0.15
<tb> Residue <SEP> Conradson <SEP> in <SEP>% <SEP> in <SEP> Weight <SEP> 2,75
<tb> Content <SEP> in <SEP> nickel <SEP> in <SEP> ppm <SEP> 2
<tb> Content <SEP> in <SEP> vanadium <SEP> in <SEP> ppm <SEP> 5
<Tb>
The yield of zew weight of synthetic crude oil relative to the unit charge is 91.7%.

 It may be noted that the product obtained has a lower density than that of the starting material, contains less sulfur and substantially more nickel or vanadium.

EXAMPLE 2
This example relates to the treatment, by the method according to the invention, of a crude oil. This oil was obtained from the deposit by steam extraction. The product thus obtained contains about 25% by weight of water, which is removed.

A hydrocarbon product is thus obtained, the characteristics of which are shown in Table VI below:
TABLE VI

<tb> Mass <SEP> volume <SEP> to <SEP> 15 C <SEP> in <SEP> g / ml <SEP> 0.996
<tb> Sulfur <SEP> in <SEP>% <SEP> in <SEP> weight <SEP> 3,5
<tb> Asphaltenes <SEP> in <SEP>% <SEP> in <SEP> Weight <SEP> 7.8
<tb><SEP> Content <SEP> in <SEP> nickel <SEP> in <SEP> ppm <SEP> 57
<tb><SEP> Content <SEP> in <SEP> vanadium <SEP> in <SEP> ppm <SEP> 121
<Tb>
This product is then processed in a laboratory installation according to the block diagram of Figure 1, to which reference is made.

 The charge of line 13 is fractionated in column 12 at atmospheric pressure.

 A fraction n 1, whose boiling point range is between 150 and 3500C, and a fraction n 2, boiling above 3500C, are collected.

The yields in% by weight are as follows:
- fraction No 1: 16%
fraction n 2: 84%.

The characteristics of the two fractions are given in Table VII below:
TABLE VII

<tb> Characteristics <SEP> Fraction <SEP> n <SEP> 1 <SEP> Fraction <SEP> n <SEP> 2
<tb> Mass <SEP> volume <SEP> at <SEP> 150C <SEP> at <SEP>: <SEP><SEP> 0.893 <SEP>: <SEP><SEP> 1.036
<tb><SEP> g / ml
<tb> Sulfur <SEP> in <SEP>% <SEP> in <SEP> Weight <SEP> 1.13 <SEP> 4.17
<tb>: <SEP> Asphaltenes <SEP> in <SEP>% <SEP> in <SEP> weight <SEP>: <SEP> traces <SEP><SEP>:<SEP> 15s4 <SEP>
<tb><SEP> Residue <SEP> Conradson <SEP> in <SEP>% <SEP> in <SEP>: <SEP> no <SEP> measured <SEP>: <SEP> 20.2
<tb><SEP> weight
<tb><SEP> Content <SEP> at <SEP> nickel <SEP> at <SEP> ppm <SEP>: <SEP><<SEP> 2 <SEP>: <SEP> 70
<tb> Content <SEP> in <SEP> vanadium <SEP> in <SEP> ppm <SEP>: <SEP><2<SEP>:<SEP> 146
<Tb>
Subsequently, fraction no. 2 is subjected to different deasphalting tests in an autoclave.

The conditions of the different tests carried out are shown in Table VIII below:
TABLE VIII

<tb> Test <SEP> Solvent <SEP> Temperature <SEP> Pressure <SEP> Mass <SEP> Rate
<tb> used <SEP> in <SEP> C <SEP> in <SEP> bars <SEP> Solvent
<tb> Charge
<tb> A <SEP> Butane <SEP> 70 <SEP> 40 <SEP> 2.04
<tb> B <SEP> Butane <SEP> 70 <SEP> 40 <SEP> 3.74
<tb> C <SEP> Pentane <SEP> 140 <SEP> 30 <SEP> 1.96
<tb> D <SEP> Pentane <SEP> 140 <SEP> 30 <SEP> 3.07
<Tb>
The compositions of the solvents used are shown in Table IX below:
TABLE IX

<tb> Solvents <SEP> Constituents <SEP>% <SEP> Molar
<tb> Methane <SEP> 0.06
<tb><SEP> Ethane <SEP> 0.03
<tb><SEP> Propane <SEP> 5.3
<tb><SEP> Isobutane <SEP> 21.25
<tb> Butane <SEP> Normal <SEP> Butane <SEP> 72.67
<tb><SEP> Butenes <SEP> 0.39
<tb><SEP> Isopentane <SEP> 0.27
<tb><SEP> Normal <SEP> Pentane <SEP> 0.03
<tb><SEP> Isopentane <SEP> 13.06
<tb> Pentane <SEP> Normal <SEP> Pentane <SEP> 85.53
<tb><SEP> Isohexane <SEP> 1.41
<Tb>
The results of the tests are shown in Table X below:
PAINTINGS

<tb><SEP> Yield <SEP> in <SEP> part <SEP> Yield <SEP> in
<tb> Oil <SEP><SEP> assay in <SEP>% <SEP> in <SEP><SEP> bitumen <SEP> weight in <SEP>% <SEP> in
<tb><SEP> weight
<tb>: <SEP> A <SEP>: <SEP> 59.2 <SEP>: <SEP> 40.8
<tb>: ~ :: <SEP>:
<tb>: <SEP> B <SEP>: <SEP> 68.4 <SEP>: <SEP> 31.6
<tb>: ~~~~ <SEP> ::
<tb>: <SEP> C <SEP>: <SEP> 86.2 <SEP>: <SEP> 13.8
<tb>: --------------: ---------------------: --------- ----------:
<tb>: <SEP> D <SEP>: <SEP> 81.9 <SEP>: <SEP> 18.1
<Tb>
The main characteristics of the oily and bituminous fractions obtained are summarized in Table XI below:
TABLE XI

<tb> Character <SEP>. <SEP><SEP> Part <SEP> oily <SEP> :: <SEP> Part <SEP> Bituminous
<tb><SEP> risks <SEP> part <SEP> @ulleuse <SEP> Part @ e <SEP> @ itum @ neuse
<tb><SEP> Assay <SEP> Assay <SEP> Assay <SEP> Assay <SEP> Assay <SEP> Assay <SEP> Assay <SEP> Assay
<tb> A <SEP> B <SEP> C <SEP> D <SEP> A <SEP> B <SEP> C <SEP> D
<tb> Mass <SEP> 0.967 <SEP> 0.966 <SEP> 0.991 <SEP> 0.981 <SEP> 1.093 <SEP> 1.098 <SEP> 1.122 <SEP> 1.112
<tb> volumic
<tb> to <SEP> 150C <SEP>: <SEP>: <SEP>: <SEP>: <SEP>: <SEP>: <SEP>: <SEP>: <SEP>:
<tb> zen <SEP> g / ml <SEP>: <SEP>: <SEP>: <SEP>: <SEP> :: <SEP>: <SEP>: <SEP>: <SEP>: <SEP>
<tb> in <SEP> in <SEP>: <SEP> 3.01: <SEP> 2.84: <SEP> 3.62: <SEP> 3.50 :: <SEP> 5.8 <SEP> : <SEP> 5.76: <SEP> 5.56: <SEP> 6.03: <SEP>
<tb>: <SEP> weight of <SEP>: <SEP>: <SEP>
<tb> sulfur
<tb> :::::::::::
<tb>:% <SEP> in <SEP>: <SEQ> 1.82: <SEP> 0.26: <SEP> 3.8 <SEP>: <SEP> 2.58 :: 39.3 <SEP >: 38.1 <SEP>: 69 <SEP>: 68.1
<tb> weight
<tb> asphal
<tb> tènes
<tb> Residue <SEP>: <SEP> 4.2 <SEP>: <SEP> 3.1 <SEP>: <SEP> 9.3 <SEP>: <SEP> 8.3 <SEP> :: 31 , 3 <SEP> 31.5 <SEP>: 38.5 <SEP>: 40.4
<tb> Conradson
<tb> in <SEP>%
<tb> in <SEP> weight
<tb> Content <SEP> at: <SEP> 8 <SEP>: <SEP> 4 <SEP>: 33 <SEP>: 23 <SEP> :: 155 <SEP>: 151 <SEP>: 240 <SEP> 229
<tb> nickel
<tb> in <SEP> ppm
<tb>: Content <SEP> at: 15 <SEP>: <SEP> 8 <SEP>: 71 <SEP>: 47 <SEP> :: 304 <SEP>: 313 <SEP>: 459 <SEP>: 450
<tb> vanadium <SEP>: <SEP>: <SEP>: <SEP>: <SEP> :: <SEP>: <SEP>: <SEP>: <SEP>:
<tb> in <SEP> ppm
<tb>: <SEP> ::: + <SEP>: <SEP> :: <SEP>: <SEP>: <SEP> ::
<tb> Point <SEP> of <SEP> 105 <SEP> 105 <SEP> 137.5 <SEP> 150
<tb>: soften-: <SEP>: <SEP> s <SEP>: <SEP>: <SEP> s <SEP> :: <SEP>
<tb> sement <SEP> in
<tb>: 0C <SEP> (3): <SEP>: <SEP>: <SEP>: <SEP> s <SEP>: <SEP>
<Tb>
(3) Measured according to AFNOR T 66-008
The oily portion is conducted in the mixer 22.

 The bituminous part is subjected to coking.

The yields in% by weight of the various products collected are shown in Table XII below:
TABLE XII

<tb><SEP> Test <SEP> Effluent <SEP> Effluent <SEP> Coke
<tb><SEP> gas <SEP> (1) <SEP> liquid <SEP> (2)
<tb><SEP>: -------------------: ------------: ---------- -:
<tb>: <SEP> A <SEP>: <SEP><SEP> 13.8 <SEP>: <SEP> 45.6 <SEP>: <SEP><SEP> 40.6
<tb>: -------------------: ------------: ------------: -----------
<tb>: <SEP> B <SEP>: <SEP><SEP> 13.8 <SEP>: <SEP> 45.3 <SEP>: <SEP> 40.9
<tb>: -------------------: ------------: ------------:
<tb>: <SEP> C <SEP>: <SEP> 15.8 <SEP>: <SEP><SEP> 33.6 <SEP>: <SEP> 50.6
<tb>: -------------------: ------------: ------------: -----------
<tb>: <SEP> D <SEP>: <SEP><SEP> 16.3 <SEP>: <SEP><SEP> 30.4 <SEP>: <SEP> 53.3
<tb> (1) Gaseous effluent: effluent containing hydrogen,
sulphide, hydrocarbons of 1 to 4 carbon atoms.

(2) Liquid effluent: effluent containing hydrocarbons
at 5 and more than 5 carbon atoms.

The characteristics of the liquid effluent are given in Table XIII below:
TABLE XIII

<tb><SEP> Characteristics <SEP> Assay <SEP> Assay <SEP><SEP>B; Assay <SEP> C-Assay <SEP> D. <SEP>
<Tb>

:::: <SEP> ::
<tb> Mass <SEP> volume <SEP> to <SEP> 150C <SEP>: <SEP> 0.892 <SEP>: <SEP> 0.892 <SEP>: <SEP> 0.892 <SEP>: <SEP> 0.892
<tb> in <SEP> g / ml
<tb> Sulfur <SEP> in <SEP>% <SEP> in <SEP> Weight <SEP> 4.3 <SEP> 4.3 <SEP> 3.9 <SEP> 4.2
<tb> Residue <SEP> Conradson <SEP> in <SEP>% <SEP>: <SEQ> 4.9 <SEP>: <SEP> 4.9 <SEP>: <SEP> 5.6 <SEP>: <SEP> 5.7
<tb>: in <SEP> weight
<tb> :: <SEP> ::::
<tb>: Content <SEP> at <SEP> nickel <SEP> at <SEP>: <SEP> 2 <SEP>: <SEP> 1 <SEP>: <SEP> 1 <SEP>: <SEP> 1 <September>
<tb>: ppm
<tb> Content <SEP> in <SEP> vanadium <SEP> 4 <SEP> 4 <SEP> 2 <SEP> 2
<tb> in <SEP> ppm
<Tb>
the liquid effluent from the coker is mixed at 22 with the oily part from the deasphalting and with the fraction n 1 from column 12, whose boiling range is between 150 and 3500C.

At the outlet of mixer 22, line 32, is collected a synthetic crude whose characteristics are given in Table XIV below:
TABLE XIV

<tb><SEP> Characteristics <SEP> Assay <SEP> A <SEP> Assay <SEP> B <SEP> Assay <SEP> C <SEP> Assay <SEP> D
<tb> Mass <SEP> volume <SEP> at <SEP> 150C <SEP>: <SEP> 0.937 <SEP>: <SEP> 0.942 <SEP>: <SEP> 0.968 <SEP>: <SEP> 0.959 <SEP >:
<tb> in <SEP> g / ml
<tb> in <SEP> in <SEP> weight <SEP> of <SEP> sulfur <SEP>: <SEP> 2.9 <SEP>: <SEP> 2.7 <SEP>: <SEP> 3,2 <SEP>: <SEP> 3.1
<tb>: --------------------------: -------: -------: --- ----:
<tb> Residue <SEP> Conradson <SEP> in <SEP>: <SEP> 3,5 <SEP> s <SEP> 2,8 <SEP>: <SEP> 7,5 <SEP>: <SEP> 6 7
<tb> in <SEP> in <SEP> weight <SEP>: <SEP>
<tb>: --------------------------: -------: -------: --- ---- ------
<tb> sTeneur <SEP> in <SEP> nickel <SEP>: <SEP> 5 <SEP>: <SEP> 3 <SEP>: <SEP> 26 <SEP> 18
<tb> in <SEP> ppm
<tb> Content <SEP> in <SEP> Vanadium <SEP> 10 <SEP> 6 <SEP> 56 <SEP> 36
<tb> in <SEP> ppm
<tb> Yield <SEP> in <SEP>% <SEP> in <SEP> weight <SEP>: <SEP> 81.3 <SEP>: <SEP> 88.5 <SEP>: <SEP> 92.3 <SEP>: <SEP> 89.4
<tb> of <SEP> crude oil <SEP>
<tb>: synthetic <SEP> by <SEP> report <SEP>: <SEP>
<tb>: at <SEP> the <SEP> load <SEP>: <SEP>
<Tb>
The synthetic crude oil obtained has a lower density than that of the starting material and contains much less nickel and vanadium and less sulfur, which shows the interest of the process according to the invention.

Claims (6)

 1. A process for obtaining synthetic crude oil from a hydrocarbon feed having a higher density, said process being characterized in that it comprises the following steps:  a) The possible fractionation of the hydrocarbon feedstock in at least two fractions:  at least one light fraction, containing most of the compounds having the lowest boiling points.  - on the other hand, a bituminous part.  - on the one hand, an oily part,  or the heavy fraction obtained, when the fractionation of step "b" is carried out, said treatment leading to the production of:  either of the hydrocarbon feed, when the fractionation of step "a" is not carried out,  b) Solvent treatment:  a heavy fraction, containing most of the compounds having the highest boiling points;  (2) a second mixture of higher molecular weight hydrocarbons than those contained in the first mixture.  (1) a first mixture, containing hydrogen, hydrogen sulfide and low molecular weight hydrocarbons,  - on the other hand, an effluent that is fractionated to give:  - on the one hand, coke,  (c) The coking of the bituminous part leading to the production of:  Said addition leading to the production of synthetic crude oil.  d) The addition to the oily part obtained in stage "b" of at least the second hydrocarbon mixture obtained in step "c" and, optionally, d-at least a portion of at least one light fraction obtained in step a when the splitting of the charge takes place,  2. A process according to claim 1, characterized in that at least a portion of the hydrocarbons contained in the first mixture obtained in step "c" is used as a solvent for the treatment of step "b".  3. A process according to one of claims 1 and 2, characterized in that at least a portion of the hydrocarbons contained in the first mixture obtained in step "c" is added to the synthetic oil.  4. Method according to one of claims 1 to 3, characterized in that at least a portion of at least one light fraction obtained in step "a", when the fractionation of the charge takes place, is used as a solvent in the treatment of step "b".  5. A process according to one of claims 1 to 4, characterized in that the hydrocarbon feedstock is subjected to a desalting operation and in that, prior to this desalting, the feedstock is added at least a portion of the hydrocarbons contained in the first mixture obtained in step "c".  6. A process according to one of claims 1 to 5, characterized in that the hydrocarbon feedstock is subjected to a desalting operation and in that, prior to this desalting, the feedstock is added with at least a portion of at least a light fraction obtained in step "a", when the fractionation of the charge takes place.