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It is known that one can decompose residues of oils, tars or pressure hydrogenation or Exitraktionsprodukte of coal or oils in high-boiling, useful for the lube oil production oils and asphalt when they are mixed with low-boiling aliphatic, z , B. treated with liquefied, gaseous at ordinary temperature, hydrocarbons. However, a satisfactory separation is achieved only if the residues still contain sufficient amounts of heavy oil. If this is not the case, z. For example, if all of the oils, which are undecidably distilled in vacuo, are removed therefrom, it is necessary to dilute the residue with an oil before treating it with low boiling hydrocarbons. As a diluent oil has for this purpose z. B. heavy fuel or luminescent oil proposed. However, this procedure is cumbersome, since the phalt separated from As oil, before z. B. with the aid of liquid selective solvents for cyclic carbon compounds, eg. As phenol, further cleans, must be rid of the diluent again.

It has now been found that it is possible to carry out the decomposition and purification of the said residues in a much simpler manner while saving a considerable part of the device costs, if the residues freed from the hydrocarbons which can be distilled without decomposition under reduced pressure are admixed with about 5 to 30% by volume of phenols, treated the mixture with low-boiling aliphatic hydrocarbons and refining the asphalt-free oils in a conventional manner with larger amounts of phenols.

Since the amount of phenols required to dilute the residue is relatively small, the apparatus for treating the low-boiling point hydrocarbon residue may be smaller than in the known process in which virtually all of the oil above the medium oil leaves boiling oils in the residue for satisfactory disintegration become. Compared to the processing of residues, which were freed of all without decomposition distillable constituents in vacuo and then diluted with heavy gasoline or luminescent oil, the operation according to the invention has the advantage that'the distillation column needed there for separating the dilution oil from the asphalt-free 01 before Cleaning with the help of further amounts of phenols is saved.

Despite this significantly simplified operation is achieved according to the invention, a clean separation in asphalt and pure, useful as saturated steam and hot steam cylinder oils oils. In addition, it also achieves even higher yields of lubricating oil, as less Asphaltstoff6, namely only thief for lubricating oil extraction unusable ingredients are precipitated while the processable on lubricating oil asphalt-like materials remain in solution. Refining with phenols before, during or after treatment with low-boiling aliphatic hydrocarbons in amounts customary for this purpose of about 100% by volume or more (based on residue) can not achieve this selective asphalt precipitation. Rather, the beneficial effect is achieved only if the amount of phenol is limited to 5 to 301 / o and if the phenols are added to the residue to be separated prior to treatment with the low-boiling aliphatic hydrocarbons.

As low-boiling aliphatic hydrocarbons both liquid and particularly liquefied, gaseous at ordinary temperature hydrocarbons, eg. Ethane or propane or mixtures thereof. These are allowed in quantities that are a multiple 'z. B. from 4 to 10 times the residues to be decomposed, at temperatures of about 30 to 100 or higher, at ordinary or elevated pressure, expediently in the usual extraction columns, act on the residues.

Phenols are to be understood as meaning those oils which consist entirely or mainly of phenols, eg. As phenol itself, crude phenols or crude cresols.

For further purification of the deasphalted oils it is expedient to use the same phenols which were added initially in amounts of about 300% by volume, based on deasphalted oil.

Example i From German petroleum, all components which can be distilled without undue decomposition in a vacuum are distilled off. The residue remaining in an amount of 30% of crude oil is diluted with 10% by volume of phenol and then treated with 8 times the amount of Vo-inine liquefied propane at 30 ° under pressure, 6.5 parts being obtained, based on crude oil 1 / o asphalt off.

The propane-depleted, deasphalted oil (2o l / o based on crude oil) is added without distilling off the diluent with enough phenol that the total amount, including that added as diluent, is three times that of the deasphalted oil. After removal of the phenol remain, based on crude oil, i4: 2% "after deposition of the paraffin 12.1 '/ 0 refined oil with the viscosity index go.

If the residue is not diluted with phenol before the propane treatment, all other conditions are equal to 10%. Asphalt and only 1/2 refined dewaxed oil of the same composition.

If the same amount of luminescent oil is used as diluent instead of phenol, it is necessary to distil off the luminescent oil before further purification of the deasphalted oil with phenol.

Subjecting a obtained from the same crude oil in a quantity of 55 Oh residue, which still contains a large part of the undecomposable in the vacuum components, the treatment with propane, so you need this much more extensive device than when working according to the invention. In addition, this gives about 7% less refined, dewaxed 01. EXAMPLE 2 A solid residue which has been separated from a pressurized hydrogenation product obtained by treating lignite with hydrogen under a pressure of 6oo at high pressure in the presence of strong hydrogenating catalysts after removal of the solids is diluted with 10% by volume of phenol and then at 50 °. treated under pressure with 4 times the amount of liquefied propane. The resulting raffinate in an amount of 55 kg is purified without separation of the diluent with i8ol / o phenol at 45 to 5o '. In addition to 33.5 kg of extract, 2.1 lbs. Of refined O1 are decomposed into 7.5 kg of paraffin and 14 kg of lubricating oil with the viscosity 13.5 'E / 5c "and the viscosity index 48.

Treating the same pressure hydrogenation residue without prior dilution with phenol with propane under the same conditions, gives only 5o kg of raffinate, and this results in the treatment with 2oo 1 / o PhenChl 2o kg of purified oil, atis idem after separation of <paraffins 12.5 kg of Schinieröl with the Visio # sity 1.2 'E / 500 and the viscosity index 5o be obtained.

By previously diluting the residue with phenol, more i2% of shortening oil is obtained than in the usual way of working without phenol dilution.