DE1470633A1 - Process for the removal of asphaltenes and ash-forming constituents from petroleum residue fractions - Google Patents

Description

SHELL INTERNATIONAL kESBAkCH MAATSCHAPPIJ N.V., The Hague,

Netherlands

Procedure for removing asphaltenes and ash-forming Components from petroleum residue fractions.

(Priority: November 28, 1960 / Netherlands)

The invention relates to a method for removing asphaltenes and constituents which form them before from petroleum residues by precipitating the same with the aid of a precipitant and separating the precipitated components from the oil.

It is well known that almost all crude oils have some metal compound content, mainly vanadium and sodium compounds. In the usual boil distillation these compounds enriched in the residue fractions, which causes serious difficulties in further applications of these oils.

co ten can occur. If the residue fractions e.g. ale ο

«Ο When heating oil is used, a vanadium and sodium form co

^ Containing ash in the combustion chamber, which is deposited on the cooler _> places, such as water pipes, where they connect with the

* - the oxide film present on the metal with the formation of a

bond with a lower melting point is converted. as

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As a result, the protective film is attacked, whereupon the Corrosion progresses faster. A similar phenomenon of corrosion occurs in gas turbines where the use of this type of residual oil does serious damage in a short period of time on the turbine blades and other JLtall parts can. In addition, a build-up of the ash components greatly reduces the efficiency of the turbine.

It has already been proposed to use ash-forming ingredients remove from residual oils. For example, British patent 634-135 suggests the use of vanadium-containing material from Petroleum residue fractions by adding C, - to C, -, - Paraf-

3 /

to separate finen and remove the oil-insoluble phase thus formed. Removal according to this working method is possible, because the Jiet al! compounds in the '3l are mainly in the form of porphyrin-like structure in the peptized state are present. When the paraffins are added, the above-mentioned second phase is formed, which is the metal compounds as well as other high molecular components, e.g. asphaltenes, contains.

In this context it is observed that the single. ixen. C, - to CU paraffins do not feel the same .Resultaten with regard to the nature and the quantity of the second phase formed. Propane and butane thus form an oily phase. On the one hand, this is an advantage because this phase - for example in a continuous countercurrent process - can be removed from the apparatus as a liquid stream. On the other hand, however, it is a disadvantage because the yield of deasphalted oil is

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is relatively big while there are few (if any) There are possible uses for the relatively large amounts of the sulfur-containing material.

Pent an, hexane and heptane can provide a high yield of ϋΐ because these hydrocarbons fill the asphaltenes and the asehe-forming constituents selectively, so that as a result the second phase formed is almost oil-free. Although these precipitants in principle allow a simple procedure for the selective removal of asphaltenes and ash-forming constituents from residual oils, carrying out the process on an industrial scale leads to almost insurmountable difficulties. These difficulties arise when separating the precipitated material, which - contrary to the phase precipitated with propane and butane - is not oily, but consists of very fine, solid asphalt particles which, according to some researchers, have a particle size that has a molecular weight of - - correspond to 90 ooo, which suggests a particle diameter of 65 8 or less. (Pfeiffer "The Properties of asphaltic bitumen ¹ · (1950) 8.36-37.)

Although these particles can be separated by filtration (e.g. for analytical purposes), the application in technical criteria for a clogged filter, so that a technically and economically viable process not carried out who can ae.

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Contrary to expectations it has now been found that a very simple separation of the precipitated solid particles becomes possible if the oil-containing mixture is passed through one or more hydro cyclones and / or liultizyklone.

The invention is therefore a method for Removal of asphaltenes and ashes forming components from petroleum residue fractions by precipitating the same with a precipitant and separating the precipitated components from the oil. The symbol of the method according to the invention consists in the complete or partial separation the precipitated components from the oil by passing it through of the oil-containing mixture is effected by one or more hydro cyclones and / or iäultiz.y clones.

It has also been found that the separation of the asphaltenes can be made much easier by using the 31 containing the freshly precipitated components for some time Movement keeps. This could be explained by the assumption that an agglomeration of elementary asphalt particles takes place, whereby larger units are formed. By the Moving the oil is mainly felt as an improved contact between the elemental asphalt particles favors the formation of larger units.

In order to separate the asphaltenes and ash-forming constituents, the oil mixture is converted into one or more hydrocyclones passed through.

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A hydrocyclone is understood here to mean a vessel which is closed and smooth on the inside The surface of revolution is limited to the one near one end with a tangential inlet opening or with a strainer correspondingly directed tangential inlet openings and is provided with a central outlet opening. This outlet opening is hereinafter also referred to as the overflow opening. There is a second drain opening at the other end of the vessel. rIf the latter end tapers conically, the drainage opening is made at the apex of the cone.

The entrance to the opening is at the furthest part of the hydrocyclone attached, which is preferably cylindrical. The overflow opening is preferably formed by a vortex tube, which protrudes axially into the hydrocyclone.

The extremely small size of the particles to be separated requires hydrocyclone, the (largest) internal diameter of which is generally between 0.5 and 4 cm and preferably between 1 and 3 cm. If such cyclones are used, a satisfactory separation of the oil mixture to be treated can be carried out at moderate feed pressures, which as a rule are between 3 and 10 ata .

Preferably, 75 ^ ⁸ 95% of the total amount of the oil mixture outside the hydrocyclone (or the cyclones) are fed through the overflow opening so that the asphalt content of the oil flowing out (after removal of Pentane usrwv> lower ■■■ * than 1% by weight and preferably lower than 0.5% by weight

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Hydrocyclones are used for this purpose Diameter of the inlet opening, overflow opening and opening at the apex of the cone a ratio of 1.5: 3: 1 to 2.5 * 3: 2 have good results with hydrocyclones reached, the cylindrical part has a diameter of 10 mm, while the inlet opening, the overflow opening and the opening at the apex of the conical part has a diameter of 2 mm, 3 mm or 1.5 μ.

A particularly surprising fact is that, despite the extraordinarily high shear stresses, which In hydro cyclones with a diameter between 0.5 and 4 cm, hardly (if any) disintegration can occur the agglomerated particles to form elementary asphalt particles occurs «In view of the fact that hardly any disintegration occurs On the other hand, it is surprising that this takes place Agglomerate under the influence of strong centrifugal forces not thrown as a sticky pale against the wall of the cyclone will cause what fcd-i the narrow opening becomes clogged in the conical part. Because although the asphalt particles precipitated with Pent an etc. are dry and hard in themselves they occur in the oil-pen tan medium in the form of sticky ones Particles on.

Ub to increase throughput, several hydrocyclones can of the type described before are connected in parallel, which can be achieved very easily by using the so-called / Mtflticyclones, under which Designation construction units are understood that

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contain a larger number of hydro cyclones, and in the Eegel are provided with a single inlet opening and two discharge lines.

The effectiveness of the separation can be increased by using hydrocyclones and / or multi-cyclones, which in Are connected in series * These cyclones can be used for the separation of asphalt particles from the oil phase passed through the overflow opening with pasture, as also for further enrichment of the asphalt suspension, which flows out of the opening at the apex of the conical part.

Starting from a petroleum residue fraction, one can in this way on the one hand produce an oil that is completely or is essentially asphaltene-free, and on the other hand pure or essentially pure, i.e. oil-free asphaltenes, which which may contain ash-forming constituents. The 81-free Asphaltenes can then be obtained in the form of a powder.

The asphalt suspension is preferably used after dilution concentrated with precipitants. For example, an oily pentane solution can be obtained via the overflow opening the yield of deasphalted oil is increased. The oil-containing one containing the precipitant Solution can also be returned to the process and together with or instead of the pure precipitant - for Precipitation and separation of the asphaltenes in the base oil can be used.

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Suitable precipitants for precipitating asphaltenes and ash-forming constituents are hydrocarbons with 4 to 9 carbon atoms in the molecule (with or without substituted polar groups) and with a surface tension against air of less than 24 D _t yn per cm (at 25). Faiaffins can be mentioned as examples, for example pentane, hexane, heptane and isooctane, as well as methylcyclohexane, as well as dimethylcyclopentan, diethyl ether and ethyl acetate or geaieche of such compounds. For economic reasons, paraffins are usually used in the form of technical mixtures, for example in the direct distillation of coal oil, and which are therefore available in large quantities in almost every refinery. In particular, pentane-containing fractions are used because the components of these fractions have relatively low boiling points, so that they can be removed very easily and completely from the deasphalted oil and from the asphaltene concentrate by means of vaporization. It should also be noted that the presence of unsaturated compounds, such as alkanes, in these fractions does not interfere with the process.

For the precipitation of asphaltenes and ache-forming components are usually 3 to 6 parts by volume and preferably 4 to 5 parts by volume of precipitant to 1 part by volume Used oil.

The precipitation can either be carried out in individual batches or continuously be performed. However, the continuous procedure is preferred. The residual oil that is used for

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Reduction of its viscosity, preferably first mixed with precipitant, is for this purpose either continuously fed into a pipeline with turbulent flow or into a boiler in which the oil mixture is stirred. The average residence time in the presence of the precipitant is preferably 0.5 to 10 minutes in both cases. If no precipitating agent has previously been added, a sufficient amount of the precipitating agent is now added. Even if the oil stream introduced into the drilling line or the mixing vessel already contained precipitant, a further amount of the precipitant can be added if necessary. The mixture with the agglomerated asphalt particles is then pressed through one or more HydroCyclones and / or MultiCyclones. The oil phase obtained from the overflow opening and the asphaltene suspension obtained from the opening at the apex of the conical part are collected separately and, if desired, freed from the precipitant by evaporation or in some other way. The recovered precipitant can be returned to the process.

The precipitation is usually carried out at a somewhat elevated temperature, because this reduces the viscosity of the mixture and promotes the agglomeration of precipitated particles. Temperatures between 3Ο ^ό and 70 ° are preferably used.

Ia general it is recommended to use the starting oil before the precipitation of the asphaltenes, because the in the Ifef-

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Residual oils produced in the production process usually contain a small amount of solid impurities, which can clog the narrow inlet and outlet openings in the Hydrocyclones. To make filtering easier, becomes the viscosity of the base oil by adding a certain amount of the precipitant or another Diluent reduced, so that little (if any) separation of asphaltenes takes place.

Petroleum residue fractions obtained by direct distillation of crude oils come into consideration as starting materials and contain asphaltenes and / or ash-forming constituents, as well as residues caused by thermal or catalytic cleavage processes have been obtained. In the In cases where the crude oil contains only a small percentage of volatile constituents, the crude oil itself can be classified as Starting material can be used, i.e. after distilling off only the most volatile components. In general, however Fractions with an initial boiling point of 340 ° to 360 ° (ASTM) used. One can also start from fractions with a higher initial boiling point, e.g. 390 ° at 30 mm Hg. An advantage of the The latter material consists in that the amount of material passed through the cyclone is considerably less.

You invention is based on the in Figures 1 and 2 The apparatus shown here is explained in more detail. This is not supposed to Limitation of the invention to be expressed rather, only working methods should be explained according to which the invention can be carried out. Fig. 1 explains

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a one-step process and FIG. 2 is an embodiment a two-stage process in which the asphaltenes are obtained in powder form.

Lines for heat exchangers, pumps and Hegel valves are not shown in the figures.

According to FIG. 1, a starting oil from a feed line 1 is diluted with a precipitant from a feed line 2, either by mixing in the feed lines or by mixing the two streams in a container 3 which is preferably provided with a stirring device (not shown) . The diluted oil is kept in the mixing container (or a mixing line) and at such a temperature that a precipitation of at least about 85% by weight of the asphaltenes originally contained in the starting oil takes place. The mixture, which contains precipitating agent, precipitated asphaltenes and oil in the precipitating agent, is then passed through a line 4 into the cyclone 5, which is usually a multicyclone, ie an arrangement of a large number of cyclone units connected in parallel . The asphaltenes leave the cyclone or cyclones via the junction attached to the apex of the conical part and the subsequent line 6, which leads to a stripping column 7, in which the remaining precipitant evaporates and is returned through line 8 to the outlet line 2 for the precipitant while the asphaltenes freed from the precipitant are withdrawn through line 13.

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According to another embodiment of the invention the cyclone operated in such a way that the asphalt sludge contained both precipitated asphaltenes and a separate one Contains phase of the precipitant, in which part of the oily constituents of the supplied starting oil is present. It can therefore enter the asphaltene scraper before it enters Settling tank (not shown) are used to dispose of a predominant part of the oily solution of the precipitant to separate from the precipitated asphaltenes before they are passed into the asphaltene scraper (7). The oily one Solution of the precipitant can then either go to the precipitant feed point or it can be stripped to remove the precipitant to remove from the '31. You can then of course combine any part of the asphaltene with any part of the Oil from the latter source or from the main supply Mix a portion of the 3ls to get the products you want either with the character of a residual oil or an asphalt.

The main amount of the precipitant leaves the overflow section of the cyclone 5 via an overflow line 9. Usually the oil solution is then fed to the oil scraper 10, in which the precipitant is evaporated and returned through the line 11 to the delivery line 2 for the precipitant is, while the deasphalted Jl is withdrawn via the line. In some cases, however, you can get this oily Solution of the precipitant without stripping for the precipitation of asphaltenes from other parts of the starting oil

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use. As a result, any part of the oily solution of the precipitant, which the overflow line 9 leaves, can be returned via line 12 for the purpose of mixing with the starting oil.

A special embodiment of the process according to the invention is shown in FIG. 2, which relates to the continuous and simultaneous production of asphalt-free or essentially asphalt-free oils and of pure or essentially pure - ie, oil-free - asphaltenes. For this purpose, a petroleum residue fraction from a source 15 is mixed for some time with a precipitant from a source 16 in a line 17, whereupon the mixture is passed through a first cyclone 18. A product is drawn off through the overflow line 19 of this hydro cyclone, which consists of a solution of essentially deasphalted oil in the precipitant. The flow which is discharged into the line 25 through the opening in the conical part of the cyclone 18 is a product which consists of a suspension of solid asphalt parts in the precipitant together with a relatively small amount of oil. The asphaltene concentrate discharged through line 25 is then mixed in line 26 with pure or substantially pure filler, which is supplied through line 24, and the concentrate is then passed through a second cyclone 27. It should be noted that the precipitant, with which the asphaltene concentrate from the first hydrocyclone 18 is mixed, from the recovery system 21, for example from a distillation column, in which the overflow line 19 from the first hydro-

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cyclone 18 withdrawn deasphalted oil is worked up, and / or from the drain recovery system 29 of the second hydrocyclone 27 - which will be mentioned below - originates.

Through the overflow line 16 of the second hydrocyclone 27, a product is obtained which consists of a solution of a relatively small amount of the essentially deasphalted UIs in the precipitating agent. This solution is mixed with the base oil in order to bring about the precipitation and separation of asphaltenes and as-forming components in the first hydrocyclone see below. A suspension of solid asphalt particles in the precipitant is drawn off through the line 28 of the second hydrocyclone 27 connected to the opening in the conical part. The product of the first hydrocyclone 18 discharged through the overflow line 19 is passed into a recovery system 21 in which, on the one hand, oil essentially freed of asphaltenes (through line 22) and, on the other hand, pure or essentially pure precipitant (through line 23) is obtained will. The product discharged through line 28 in the conical part of the second hydrocyclone 27 is introduced into a recovery device 29, where on the one hand pure or essentially pure asphaltenes (through line 31) and on the other hand pure or essentially pure precipitating agent (through line 30) are obtained , whereby the precipitant, as mentioned above, is returned to the process.

The pure asphaltenes obtained from line 31 can, for example, be mixed with a suitable diluent oil,

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which is fed through the line 32 so as to produce a synthetic asphaltic bitumen, which through the Line 33 is withdrawn.

In all cases in which those described above Working methods a hydrocyclone has been used, a multi-cyclone can also be used.

The (largest) inside diameter of the cyclones according to the present invention can vary within very wide limits. In general, a diameter between 0.5 and 4 cm is preferred; but it can also cyclones _t ^ rößeren diameters, for example up to 10 cm can be used.

example 1

16.8 l of a residue fraction which has been obtained by direct distillation of a Venezuelan HohoIs with an initial boiling point of 350 ° (ASTM), a vanadium content of 520 parts per million parts and an N trium content from 61 parts to 1 million parts and a viscosity of 30,000 cS at 37 * 8 ° were mixed with 82 liters of n-pentane in a pressure vessel while stirring. Then came the roar continued at a temperature of 35 ° for a further 10 minutes. The oil-pentane mixture old the precipitated asphaltenes and ash-forming constituents was then through a Hydrocyclone run at a nitrogen pressure of 4 atmospheres

The dimensions of the Z clone were as follows:

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1470 633 10 mm 6th mm 55 mm 2 camouflage. 3 mm 1. 5 mm 4th mm

Diameter of the cylindrical part Height of the cylindrical part
Height of the conical part
Diameter of the inlet opening Diameter of the overflow opening Diameter of the opening in the conical part length of the vortex tube

Under these conditions, the starting mix was with a speed of 150 1 ^ h through the cyclone.

A total of 80.8 l of the oil-pentane mixture was obtained through the overflow opening and 18 l of a pentane-containing asphalt concentrate were obtained through the opening in the conical part. After evaporation of the pentam, 12.7 liters of enta remained; Phosphated oil and 4.1 l of asphalt concentrate, which contained 0.4 and 40% by weight, respectively, of precipitated constituents, receded. The viscosity of the asphaltene-free oil was 8500 cS at 37 »8 °. The vanadium content of the Gis was content to 200 parts per 1 million parts and N sodium had dropped to 6 parts per 1 üäillion parts.

Example 2

A fraction with an initial boiling point of 350 ° (ASTM) a VanaSf'um content of 52 parts per million parts and a sodium content of also 52 parts per 1 million parts produced by direct distillation of a Middle East oil was used as the starting material. The viscosity of the base oil was 1618 cS at 37.8 °.

In continuous operation, 20 l / h of the ßück stock fraction and 130 l / h n-pentane at the same time in one

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container with a usable capacity of 25 1 pumped · The Jl-j. ^J entan-Geiaisch with the precipitated asphaltenes and aach-forming constituents, which remained under the Aibeitsbedin ^ ungen during an average residence time of 10 minutes in the ία container, was continuously through the cyclone described in Example 1 at a pressure of 4 · at and with a Pumped speed which corresponded to the feed rate of the oil-pentane mixture.

130 l / h of a Jl-Pentane-Ge Through the opening in the conical part, 20 l / h of a pentane-containing asphaltene concentrate were obtained. After evaporation of the pentane, de-asphalted oil remained an asphaltene concentrate back which precipitated 0.3 or 28 wt. ifc Ingredients contained. The viscosity of the deasphalted Oil was 833 cS at 37.0 °. The vanadium content of the Jls was at 23 parts per million parts and the sodium content had dropped to 2.4 parts per million parts.

Example ^

The asphaltenic concentrate obtained according to Example 2 was once again through a hydrocyclone for the purpose of further enrichment passed through. For this purpose, a hydrocyclone with the same dimensions in the previous examples used.

19 «9 l of the asphaltene concentrate were used for this purpose first diluted with 69 1 n-pentane and then through the hydrocyclone passed through at a pressure of 4 at · Via the

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Overflow openings were 70.4 1 x-entane-oil mixture and through the opening in the conical part 18.5 1 pentah-containing asphaltene concentrate were separated. After evaporation of pentane dee 1.96 1 1.44 1 oil and asphalt concentrate with an asphalt contains from 66 percent · -% was obtained.

Example 4

The same residue fraction as mentioned in Example 2 was used as starting material for the simultaneous production of deasphalted oil and asphaltenes, which contained ash-forming constituents, in the -E ¹ Ig. 2 used apparatus *

In a continuous flow, 1000 kg / h of the aforementioned Residue fraction - heated to 100 ° - fed through line 15 and at 5000 kg / h of a precipitant. heated to 52 ° - mixed, which consists of a solution of a relatively small amount of ent asphalted oil in n-JPentane existed and via the overflow line 16 of the MultizySklönB was withdrawn. The mixture thus obtained, which is now a temperature of 60 °, was guided in a turbulent flow through line 17 into a multicyclone 18, which from 10 parallel switched cyclones · Each of the cyclones had the dimensions given below:

Diameter of the cylindrical part 25 mm

Diameter of the inlet opening 7 mm

Diameter of the overflow opening 8.5 mm

Diameter of the opening in the conical part 4

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The length of the line 17 was such that the residence time of the mixture in the same 1 minute was sufficient to precipitate the asphaltenes contained in the BaBie oil and to bring about the desired agglomeration of the primarily precipitated asphalt particles into larger units. Above the overflow opening of the cyclone 18 was 5557 kg / h of oil solution discharged through line 19, which were then heated in furnace 20 and passed into a distillation column 21. At the bottom At the end of this column, 950 kg / h of deasphalted oil were also transferred An asphaltene content of 0.5% by weight is discharged through line 22. The vanadium content of the deasphalted 3l was up 23 parts per million and the sodium level had dropped to 2.4 parts per million. Bas through line 23 at the top of the distillation column in an amount Clay 4607 kg / h discharged pentane was through line 24 returned to the process at a temperature of 20 ° and mixed in line 26 with the asphaltene concentrate (60), through the line 25 from the opening in the conical part of the cyclone 18 was withdrawn in an amount of 442 kg / h. The mixture of pentane and asphaltene concentrate, which had a temperature of 23 °, was in a turbulent flow the line 26 is introduced into the multicyclone 27, which - similar to the first-mentioned multicyclone 18 - from FIG. 10 in parallel switched cyclones, each of which had the same dimensions as the first cyclone. Through the overflow line 16 of this cyclone 27 were 5000 kg / n of pentane an oil of 1.2% by weight, which is used as a precipitating agent for the base oil supplied through line 15

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det vurde. Asphaltene concentrate was fed through line 28 to the recovery system 29 in an amount of 442 kg / h, from which pentane was withdrawn in an amount of 400 kg / h through line 30, and then together with that through line 23 from the distillation column 21 pentane removed to be mixed via line 24 with the asphaltene concentrate which was withdrawn from the opening in the conical part through line 25 of the cyclone 18. Through line 31, asphaltenes were in powder form with a Ol ^ ehalt of 10 wt .-% in an amount of ^ O kg / h obtained.

Example 5

About the effect of temperature on asphaltene removal To study, comparative tests were carried out under two different combinations of working conditions. In a series of experiments, contact was made in a tube and in the other a container was used while drilling the contents. The temperatures were in each of this test series varies according to the information given in the table below. In every case they were Asphaltenes after the specified residence time under the relevant contact conditions and with the various Separated specified temperatures, with the residue oil with 5 parts by volume of n-pentane per part by volume of the residual oils had been diluted ",

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Continuous paving of a long Kuwait residue Residence time Type of temperature Asphaltene

mixture o «concentration;

. * __________. apparatus or ___ »« »_» __ »_ ft ⁱⁿ overflow

2o seconds tubular 25 2

40 1.5

60 1

66 0.8

Stirred for 4 minutes in 32 1.0

Boiler 40 0.8

56 0.1

It can be seen that asphalt particles, "oak one Allow separation with the aid of hydrocyclones, earth formed more quickly at the higher temperatures.

Taking a summary of some of the benefits provided by the application The advantages achieved according to the present invention can be said: The process enables the economic separation of the asphaltenes from the oily components in petroleum residues and, at the same time, a substantial reduction of ash components such as vanadium and sodium, these being enriched in the asphaltenes. The Ul has significantly improved properties as far as its later usefulness comes into play, namely with regard to on the reduced ash content and the resulting reduced corrosiveness. It has also been found that as a result of Reduction of these special ash constituents makes the catalytic treatment of oils obtained in this way more effective iet, as the decrease in catalyst activity takes place much more slowly than when treating the untreated petroleum return «

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Stand. This is particularly noteworthy for hydrogenation treatments including hydrodesulfurization treatment.

The asphalts isolated by the process of the invention are very desirable constituents in asphalt mixes and they can be combined with a number of oils known in the art, such as aromatic extracts or heavies Distillates, for the purpose of obtaining asphalt compositions, which have the same properties as blown asphalt. It it can thus be seen that the use of such asphaltenes reduces or reduces the need for blowing such mixtures even eliminated without having to forego the properties of blown asphalt.

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Claims (13)

«23- U70633 Patent claims 1.1 Process for the removal of asphaltenes and ash- constituents forming from petroleum residue fractions by precipitating the same with a precipitant and separating the precipitated constituents from the oil, characterized in that the complete or partial separation of the precipitated constituents from the oil takes place in that the oil-containing mixture is passed through one or more hydrocyclones and / or multicyclones. 2. The method according to claim 1, characterized in that pentane and / or heptane or hydrocarbon frestions containing these precipitants are used as precipitants. 3. The method according to claim 1 or 2, characterized in that that the oil together with the precipitated constituents 0.5 kept moving for 10 minutes before moving into the Cyclone is dismantled. 4. The method according to claim 3 «characterized in that the oil with the precipitated constituents is stirred at a temperature between 30 ° and 70 °. 5. The method according to any one of claims 1 to 4, characterized in that the separation takes place in one or more hydro-cyclones whose (largest) inner diameter between 0.5 and 4 approx and preferably between 1 and 3 cm, and that the oil mixture to be broken down at a pressure between 3 and 809813/1043 -24- U70633 10 at is supplied. 6. The method according to any one of claims 1 to 5 »characterized in that 75 to 95 vol .-% r <it supplied oil mixture from the hydrocyclone (the cyclones) are discharged through the overflow opening, so that the asphalt content of the withdrawn oil (after Removal of the precipitant) is less than 1% by weight and preferably less than 5% by weight. 7 · A method according to any one of claims 1 to 6, characterized in that hydrocyclones applied grazing, in which the diameter _o of Eintrittsöffηun, the overflow opening and the opening in the conical part the ratio of 1.5: 3: 1 to 2.5: 3: 2 exhibit. 8. The method according to any one of claims 1 to 7 »characterized in that that the oil to be deasphalted through the hydrocyclone (s) in a dilution corresponding to 3 to 6 parts by volume and preferably 4 to 5 parts by volume of the Precipitant on 1 part by volume of the oil carried wild. 9. Method according to one of Claims 1 to 8, characterized in that that the 9lphase obtained via the overflow opening and / or the asphaltene suspension of a first hydrocyclone or multicyclone obtained via the opening in the ionic part is passed through another or several series-connected hydrocyclones. 10. Process for the simultaneous extraction of deasphalted $ 1 and of asphaltenes, which asehe-forming constituents 8098 1 3/1043 -β * «- Η70633 may contain parts, due to the precipitation of asphaltenes and ash-forming components from a petroleum residue fraction by means of a precipitation agent and separating the precipitated Components of the oil according to claim 9 »characterized in that the through the opening in the conical part preserved asphalt ens uapensi on of the first hydro cyclone or Multicyclones through a second hydrocyclone or multicyclone after it has been diluted with further precipitant 11. The method according to claim 10, characterized in that the oil-containing precipitant, which is drawn off via the overflow opening of the second hydrocyclone or multicyclone was used to precipitate and separate the asphaltenes in the first hydrocyclone or multicyclone. 12. The method according to any one of claims 1 to 11, characterized in that the residue oil, preferably mixed with precipitant, continuously in a pipe u & d / or a mixing vessel is introduced in which the oil mixture, with or without further addition of precipitant, in the presence of precipitant during an average residence time from 0.5 to 10 minutes, whereupon the mixture containing agglomerated asphalt particles passes through one or more hydrocyclones and / or multicyclones passed through and that it will be obtained from the overflow opening " oil phase and that obtained from the opening in the conical part As ^ holdeuspeneion obtained separately and, if desired, from Pällungsaittel are freed (»wake-up by evaporation). 809813/10 ^ 3 13. The method according to claim 10 to 12, characterized in that that the petroleum residue fiction with a precipitant is mixed so that the mixture is passed through a first hydrocyclone or multicyclone to obtain an overproduct which consists of a solution of precipitant and essentially deasphalted oil, while the one below Product withdrawn from the cyclone consists of a suspension of solid asphalt particles in the precipitant and contains only a relatively small amount of oil that the Product withdrawn below from the first hydrocyclone or multicyclone is mixed with pure or essentially pure precipitating agent, which is wholly or partially composed of a Recovery system for the upper discharge of the first hydrocyclone or MultiZyklons and / or for the lower drain of the second hydrocyclone or multi-cyclone has been obtained that the mixture of the product running down below first hydro cyclone or multi cyclone and the pure or essentially pure precipitant through a second hydro cyclone or multicyclone is felt, whereby an overflow product is obtained, which consists of a precipitant and a relative small amount of essentially ent asphalt! he tem oil consists, while a product drawn off at the bottom consists essentially of a suspension of solid asphalt particles in precipitating agents is that the overflow product of the second hydrocyclone or multi cyclones for precipitation and separation is used by Aephaltenen in the first hydrocyclone or multicyclone, and that the overflow product of the first hydrocyclone or multi cyclones in a recovery system 8098 13/1043 leads is in which practically deasphalted oil and pure or otherwise pure precipitating agent is obtained, and that the product withdrawn below of the second hydrocyclone or multicyclone in a second V.iociergevinnungssystGm ^ is carried out "in which pure or we sent pure asphalt ene as well as reinea or im. essential pure precipitant obtained will. 14 · method n---.ch one of claims 1 to 13 »thereby apply, draws, dcisü the precipitated components canz or partly as a component in asphalt; be used· 809813 / 10Ü3