RU2762672C1 - Method for producing a hydrocarbon base of drilling fluids - Google Patents

Abstract

FIELD: petroleum industry.

SUBSTANCE: invention relates to the field of refining petroleum and low-value weighted fractions of primary and secondary petroleum refining processes and producing a special hydrocarbon base for drilling fluids used in the petroleum and gas industry in the technological process of drilling gas and petroleum boreholes. In the method for producing a hydrocarbon base for drilling solutions, mixtures of weighted middle-distillate fractions of primary and secondary petroleum refining processes, boiling in the temperature range from 155 to 455°C or vacuum gas oil produced in distillation of petroleum residue boiling in the temperature range from 280 to 460°C, are subjected to a process of deep hydrogenation: said mixtures of weighted middle-distillate fractions at a temperature of 325 to 420°C and a pressure of 20.0 to 31.0 MPa on a nickel-tungsten-sulphide catalyst, adding aluminium oxide, or on a catalyst containing hydrogenating components - nickel, molybdenum in the oxide form, and said vacuum gas oil at a temperature of 350 to 420°C and a pressure of 23.0 to 32.0 MPa on a catalyst containing hydrogenating components - nickel, molybdenum in the oxide form on an alumina carrier, adding silicon oxide. The hydrogenation product produced in the process of deep hydrogenation is additionally treated with an aqueous alkali solution and subjected to fractionation, extracting the target fraction of a hydrocarbon base for drilling fluids, boiling in the range of 195 to 320°C, exhibiting the following quality characteristics: the content of aromatic compounds no more than 3 wt.%, total sulphur no more than 0.001 wt.%, pour point not higher than minus 40°C, flash point in a closed crucible not lower than 80°C.

EFFECT: expansion of the raw material base and scope of technological solutions for producing a hydrocarbon base for drilling fluids while simultaneously reducing the production cost thereof, fire safety, environmental safety of the hydrocarbon base for drilling fluids, possibility of storage and operation of the liquid hydrocarbon base in cold climatic zones, allowing for a drilling process with minimum possible power consumption.

1 cl, 2 dwg, 12 tbl, 4 ex

Description

The technical field to which the invention relates

The invention relates to the field of oil refining and low-value weighted fractions of the processes of primary and secondary oil refining (fuel oil components) and the production of special petroleum products, in particular to the production of a hydrocarbon base for obtaining drilling fluids used in the oil and gas industry in the technological process of drilling gas and oil wells ...

State of the art

In most cases, drilling fluids are complex colloidal systems that perform many different functions in the process of drilling wells, from removing cuttings from the bottom of the well and cooling the bit to maintaining the stability of the wellbore walls and protecting drilling equipment from corrosion and abrasive destruction.

Depending on the geological conditions and requirements of the drilling process, various agents can be used as the basis for creating a continuous phase of drilling fluids. Most often, water or aqueous brines are used for these purposes, as well as hydrocarbon liquids.

The hydrocarbon base for drilling fluids, as a rule, is used when drilling easily swellable and prone to collapse clay rocks, salt deposits, as well as productive formations with low reservoir properties. In this case, the hydrocarbon base can be used either in pure form, or in a mixture with water or with an aqueous solution in the composition of emulsions, where the hydrocarbon liquid forms a continuous phase.

Oil, gas condensate, base oils, vegetable oils, diesel fuel, poly- and alpha-olefins are traditionally used as a hydrocarbon medium for the preparation of drilling fluids. Moreover, these hydrocarbon bases have both positive and negative performance characteristics. At present, the requirements for the quality of hydrocarbon bases for drilling fluids are becoming more stringent in terms of ensuring operational, environmental and fire safety properties. Bases for drilling fluids should be low in sulfur and aromatics, high flash points, and low viscosities and pour points. Table 1 shows the requirements of the STO of PJSC "NK" Rosneft "to the hydrocarbon base for drilling fluids Rosneft Drilltec В 2, produced by OJSC" Slavneft-YANOS ".

Many of the previously used hydrocarbon bases for drilling fluids did not meet these requirements. Ensuring these characteristics of the hydrocarbon base for drilling fluids is possible only through the use of special technologies, taking into account the selection of certain raw materials, the use of catalytic processes and the use of highly efficient rectification to isolate target products. A number of products and methods for their preparation are known, which allow the production of hydrocarbon bases for drilling fluids of the required quality.

In drilling practice, synthetic liquid paraffins can be used. So there are inventions [US patent 5096883; US patent 518902, patent RU 2547653], which mentions a method for producing liquid paraffins of a branched structure for use in compositions of oil-based drilling fluids, which consists in the synthesis of low molecular weight alpha-olefins by oligomerization processes to obtain paraffinic hydrocarbons. The resulting liquid paraffins are non-toxic to the environment due to the absence of aromatic and sulfur-containing compounds in them. Moreover, they have a low pour point (below minus 40 ° C) and a high flash point (over 90 ° C). The latter property is important from the point of view of fire safety during storage and operation of drilling fluids. However, a significant disadvantage of this method of obtaining a hydrocarbon base for drilling fluids is the technological complexity of their production, the scarcity and high cost of raw materials, and, as a consequence, the high cost of the resulting product relative to other analogues, which can limit their use in drilling practice.

Vegetable oils can also be used as a hydrocarbon base for drilling fluids. There is an invention [US patent 463136], proposing to use for these purposes peanut, rapeseed, soybean, sunflower, corn, castor, palm oil or mixtures thereof with each other. These oils, which contain C ₁₂ -C ₁₄ carboxylic acids, are biodegradable, which makes them safe for the environment. However, due to the higher cost of these fluids relative to refined and petrochemical products, such oils have not found wide application in drilling practice. In addition, their disadvantages include relatively high pour point values (over minus 20 ° C), which limits their use in cold climatic zones.

From the patent of the Russian Federation No. 2346020 known a method of obtaining a base for oil emulsol, which is liquid hydrocarbons, which can be used as a base for drilling fluids. The basis for oil emulsol is a paraffin-naphthenic fraction obtained by rectification of hydrocracking kerosene, a product with a freezing point of 55-65 ° C and a boiling point of 210-230 ° C. In the method for producing said base, hydrocracking kerosene is subjected to rectification, the process is carried out at reduced or atmospheric pressure.

The common features of this patent and the proposed invention are:

- use as a raw material for the production of a hydrocarbon base for drilling fluids obtained during oil refining, a weighted component of the raw material - vacuum gas oil, which is formed during vacuum distillation of straight-run fuel oil;

- obtaining as a result of a hydrocarbon base for drilling fluids with a low content of sulfur and aromatic hydrocarbons, a high flash point and low viscosity and pour point.

The disadvantages of this patent are:

- the yield of the product for the feedstock of the hydrocracking process is several times lower (less than 10% for the feedstock of the hydrocracking process, since the yield of the product for the hydrocracking kerosene is 45-65%, and the yield of the hydrocracking kerosene itself for the feedstock is usually no more than 10%) than the product yield according to our proposed method for hydrogenation raw materials (according to two options 45.7-72.8%, according to the third - more than 20%);

- limited resources of raw materials - hydrocracking kerosene, because the hydrocracking process, as you know, is aimed at the production of diesel fuel or improved oils, and kerosene is a low-tonnage by-product;

- high prime cost of the resulting base for emulsol due to low resources of raw materials and its high cost.

From RF patent No. 2699419 (analogue) there is a known method for producing a component for drilling fluids from oil, which includes the distillation of oil with the release of a fraction of diesel fuel, fuel oil, catalytic hydrotreating of a fraction of diesel fuel, and the hydrotreated fraction of diesel fuel is sent to isodewaxing carried out at a pressure of 41- 43 ati, the resulting technological product is sent to fractionation and a fraction is taken, boiling in the range of 160-360 ° C.

The common features of the analogue and the proposed invention are:

- use as a raw material for the production of a hydrocarbon base for drilling muds of oil and raw materials obtained during its processing;

- increased yield of the target product for the feedstock up to 43.6% (at the output of the component for drilling fluids at the stage of isodewaxing and fractionation of hydrotreated diesel fuel up to 80% - table 2 of the description of the invention);

- obtaining as a result of a hydrocarbon base for drilling fluids with a high flash point and low viscosity and pour point.

The disadvantages of the analog are:

- the complexity and high costs of the proposed technology, since a two-stage catalytic process is used, carried out at rather high pressures and temperatures, while in our proposed method, a one-stage catalytic process is used;

- the use of high-value raw materials - straight-run diesel fuel obtained during atmospheric distillation of oil (typical boiling range 160-360 °), the cost of which is much higher than that of weighted middle distillate fractions obtained during atmospheric-vacuum distillation of oil and fuel oil and in the processes of secondary oil refining (coking and catalytic cracking), vacuum gas oil. At the same time, the use of straight-run diesel fuel as a raw material for the production of a base for drilling fluids will lead to a decrease in the production of highly valuable Euro 5 diesel fuel that is in demand on the Russian market;

- high prime cost of the obtained hydrocarbon base for drilling fluids due to high costs in the implementation of a two-stage catalytic process, including the use of an isomerization catalyst containing precious metals;

- problems with meeting the requirements for the content of aromatic hydrocarbons (no more than 3 wt.%) in the received component for drilling fluids, because at a given pressure of the hydrotreating process, specified in the patent of the Russian Federation No. 2699419, complete saturation of aromatic hydrocarbons contained in the feed does not occur, this aspect is not covered in this patent.

The closest prototype of the present invention is a method for producing a component for drilling fluids from oil, for example, distillate fractions or products of secondary oil processing [RF patent No. 2668612]. A method for producing a component for drilling fluids from oil includes distillation of oil with the release of fuel oil. The resulting fuel oil is sent to vacuum distillation to obtain vacuum gas oil. The resulting vacuum gas oil is subjected to hydrocracking. The unconverted residue formed in the hydrocracking process is sent to isodewaxing, then to hydrofinishing. The resulting technological product is sent to fractionation. As a component of drilling fluids, a fraction that boils away in the range of 195-305 ° C is selected.

The general features of the prototype and the proposed invention are that as a raw material for obtaining a hydrocarbon base for drilling fluids, oil and the raw material weighted components obtained during its processing are used, as well as the fact that as a result, a hydrocarbon base for drilling fluids with a low sulfur and aromatic content is obtained. hydrocarbons, high flash point and low viscosity and pour point.

The disadvantages of the prototype are:

- the complexity and high costs of the proposed technology, since a three-stage catalytic process is used, carried out at high pressures and temperatures, while our proposed method uses a one-stage catalytic process;

- low yield of the product for the feedstock of the hydrocracking process, vacuum gas oil - less than 1% (information taken from the description to the patent of the Russian Federation No. taken from an article in the journal "Oil refining and petrochemistry", 2018, No. 11, pp. 3-6), this is significantly lower than the product yield according to our proposed method (according to two options 45.7-72.8%, according to the third - more than 20% for hydrogenation feedstock), the implementation of which will increase the production of the hydrocarbon base in comparison with the prototype for drilling fluids by more than 10 times;

- high cost of the obtained hydrocarbon base for drilling fluids due to the low yield of the target product and high costs in the implementation of a three-stage catalytic process at high pressures and temperatures, including the use of an isomerization catalyst containing precious metals.

The objective of the proposed invention is to expand the raw material base and technological solutions for the production of a hydrocarbon base for drilling fluids, reduce the cost of producing a hydrocarbon base for drilling fluids and increase its production in the Russian Federation within the framework of import substitution, obtain a fire and environmentally friendly hydrocarbon base for drilling fluids, allowing for its storage and operation in cold climatic zones in liquid form and to carry out the drilling process with the lowest possible power consumption

The problem is solved by the method of obtaining a hydrocarbon base for drilling fluids, which consists in the fact that mixtures of weighted middle distillate fractions of primary and secondary oil refining processes, boiling away in the temperature range from 155 to 455 ° C, or vacuum gas oil obtained during the distillation of fuel oil, boiling out in the temperature range from 280 to 460 ° C, subjected to a deep hydrogenation process: these mixtures of weighted middle distillate fractions - at a temperature of 325-420 ° C and a pressure of 20.0-31.0 MPa on a nickel-tungsten-sulfide catalyst with the addition of aluminum oxide or on a catalyst, containing hydrogenating components - nickel, molybdenum in oxide form, said vacuum gas oil - at a temperature of 350-420 ° C and a pressure of 23.0-32.0 MPa on a catalyst containing hydrogenating components - nickel, molybdenum in oxide form on an alumina carrier with an additive silicon oxide, obtained in the process of deep hydrogenation of raw materials, hydrogenated product is additionally processed t with an aqueous solution of alkali and subjected to rectification with the release of the target fraction of the hydrocarbon base for drilling fluids, boiling in the range of 195-320 ° C, having the following quality characteristics - the content of aromatic compounds is not more than 3 wt. %, total sulfur not more than 0.001 wt. %, pour point not higher than minus 40 ° С, flash point in a closed crucible not lower than 80 ° С, ensuring operational, environmental and fire safety requirements.

In this case, the invention can be characterized by the following essential features:

- The hydrocarbon base for drilling fluids is obtained by refining oil and petroleum hydrocarbon fractions, which makes it possible to use a wide range of large-tonnage refined products as a raw material base for its production. The technological processes that are used to implement the invention are industry standard. All this leads to a low cost of the hydrocarbon base for drilling fluids according to the claimed invention in comparison with synthetic analogs and analogs obtained on the basis of the hydrocracking process.

- Increased yield of the target product due to the use of catalytic hydrogenation technology at high pressure of raw materials - a mixture of weighted middle distillate fractions of primary and secondary oil refining processes, as well as vacuum gas oil. This will significantly increase the production of a valuable and demanded product in the Russian Federation.

- In addition, the proposed process of catalytic hydrogenation at high pressure makes it possible to realize the production of a hydrocarbon base for drilling fluids using one catalytic stage of raw material processing, which greatly simplifies the production scheme and reduces operating costs.

- In the course of implementation of the invention, fuel oil components are involved in the raw material for obtaining a hydrocarbon base for drilling fluids, boiling up to a temperature of 415-460 ° C, having a low cost, which makes it possible to obtain a more profitable product with lower production costs.

At the same time, the obtained hydrocarbon base for drilling fluids has high operational, environmental and fire-fighting characteristics:

- contains in its composition aromatic compounds not more than 3 wt. %, total sulfur not more than 0.001 wt. %, (ensures environmental safety);

- has a pour point no higher than minus 40 ° C (allows storage and operation in cold climatic zones), a flash point in a closed crucible of at least 80 ° C (provides the required level of fire safety when storing fluid and operating it while drilling);

- has an indicator of kinematic viscosity at 40 ° C not more than 4 mm ² / s (helps to reduce power consumption for the drilling process).

This allows us to conclude that it meets the inventive step criterion.

Implementation of the invention

The proposed invention can be obtained as a result of the sequential execution of the following technological operations:

1. Mixtures of weighted middle distillate fractions of primary and secondary oil refining processes, boiling away in the temperature range from 155 to 455 ° C, or vacuum gas oil obtained during the distillation of fuel oil, boiling out in the temperature range from 280 to 460 ° C, are subjected to deep hydrogenation at high pressure at special catalysts to a level that ensures the content of aromatic compounds in the final product, no more than 3 wt. %.

2. If it is necessary to achieve the required content of total sulfur in the product to a level of not more than 0.001 wt. % (no more than 10 ppm) the resulting hydrogenated product can be additionally alkalized.

3. The resulting hydrogenated product is separated into fractions using a rectification process with the selection of an intermediate fraction, which is the final product that meets all the stated requirements.

In the process of deep catalytic hydrogenation of the feedstock, mono, bi- and polycyclic aromatic compounds are converted into naphthenic hydrocarbons [Handbook of petrochemists. In two volumes. T. 1 / Ed. S.K. Ogrodnikov. - L .: Chemistry, 1978. - 496 p.]. In addition, this process contributes to the removal of sulfur-containing substances by converting their constituent sulfur atoms into gaseous hydrogen sulfide, followed by its separation from the hydrogenate.

Alkalization of the obtained hydrogenated product is carried out as required in order to additionally remove dissolved hydrogen sulfide and achieve the required total sulfur content in the final product up to a content of not more than 0.001 wt. % (no more than 10 ppm).

Depending on the hardware design of the rectification stage and the component composition of the hydrogenation feedstock, the separation of the intermediate fraction can be performed both in a single-column and in a two-column version.

To confirm the possibility of implementing the claimed invention in JSC Angarsk Petrochemical Company (JSC ANHK), pilot runs were carried out to confirm the implementation of the proposed invention according to two schemes using various raw materials, catalysts and hardware design of the rectification stage with obtaining batches of hydrocarbon base for drilling fluids of the required quality.

Example 1

The feedstock for the production of a hydrocarbon base for drilling fluids according to the first scheme was mixtures consisting of weighted middle distillate fractions obtained in the course of primary and secondary oil refining processes, namely, light catalytic cracking gas oil (LGCC), diesel fraction (DPFK) and light delayed gas oil. coking of oil residues (LGZK), weighted straight-run diesel fuel (UPDT). The quality of the indicated middle distillate fractions during the run period is shown in Table 2.

A block diagram of a process for producing a hydrocarbon base for drilling fluids using these feedstock components is shown in Figure 1.

The preparation of mixed raw materials was carried out by mixing the components indicated in Table 2 in tanks with a volume of 1000 m ³ in specified ratios. The ratio of the components in the mixed raw material, which was used during the run, and its quality are presented in table 3.

Next, the mixed raw material was sent to the deep hydrogenation unit (Fig. 1). The process of deep hydrogenation of the mixture was carried out at high pressure in three reactors installed in series on a nickel-tungsten sulfide catalyst with the addition of alumina. Due to the increased content of sulfur compounds in the initial weighted middle distillate fractions of catalytic cracking and delayed coking of oil residues, the resulting hydrogenated product was additionally subjected to an alkalization unit (Fig. 1) treated with an aqueous solution of NaOH with a concentration of 10-12 wt. % for the purpose of additional removal of dissolved hydrogen sulfide from it.

The parameters of the hydrogenation process, the yield and quality of the obtained alkalized hydrogenates are presented in Table 4. It should be noted that the hydrogenated yield on the feedstock is more than 101% due to the hydrogen fed into the process into the hydrogenation reaction (saturation of unsaturated and aromatic hydrocarbons).

The process of separating the final product from the alkalized hydrogenated product was carried out on a rectification unit (Fig. 1) according to a two-column version using atmospheric and vacuum rectification columns. In the first atmospheric distillation column from the upper part, the gases dissolved in the hydrogenate and the gasoline fraction are taken. The stripped hydrogenated product is fed for further separation into a vacuum rectification column, where the required product is removed as the overhead product, and the heavy residue as the bottom product. The operating mode of the column equipment and the fractional composition of the final product (boiling range 195-320 ° C) provide a hydrocarbon base for drilling fluids that meets the requirements for kinematic viscosity, total aromatic hydrocarbon content, pour point and flash point.

The yield and quality parameters of the obtained hydrocarbon base for drilling fluids are presented in Table 5.

Thus, Example 1 confirms the requirements for processing heavy fuel oil components and obtaining an increased yield of the hydrocarbon base of drilling fluids of appropriate quality, as claimed in the task of the invention. From the feedstock, as a result of catalytic hydrogenation at high pressure of a mixture of weighted middle distillate fractions obtained during the processes of primary and secondary oil refining, and subsequent rectification of the alkalized hydrogenate, 45.7-72.8% of the target product is isolated, which is significantly higher than that of the prototype.

Example 2

The pilot industrial run was carried out according to the scheme shown in Example 1 (Fig. 1), but using a different catalyst containing hydrogenating components (nickel, molybdenum) in oxide form. Before using the catalyst, it was sulfided. During sulfidation, the active form of the catalyst is formed - the transition of metals from the oxide form to the sulfide form.

The raw material for the production of a hydrocarbon base for drilling fluids according to example 2 was a mixture consisting of weighted middle distillate fractions obtained during the secondary oil refining processes, namely, light catalytic cracking gas oil (LGCC) and light delayed coking gas oil (LGZK). The quality of the indicated middle distillate fractions during the run period is shown in Table 2, and of the mixed raw materials - in Table 6.

Next, the mixed raw material was sent to the deep hydrogenation unit (Fig. 1). The process of deep hydrogenation of the mixture was carried out at high pressure in three reactors installed in series on a catalyst containing hydrogenating components (nickel, molybdenum) in oxide form. Due to the increased content of sulfur compounds in the initial middle distillate fractions of catalytic cracking and delayed coking of oil residues, the resulting hydrogenated product was additionally subjected to an alkalization unit (Fig. 1) treated with an aqueous solution of NaOH with a concentration of 10-12 wt. % for the purpose of additional removal of dissolved hydrogen sulfide from it.

The parameters of the hydrogenation process, the yield and quality of the obtained alkalized hydrogenate are presented in Table 7. It should be noted that the yield of the hydrogenate on the feedstock is more than 101% due to the hydrogen fed into the process into the hydrogenation reaction (saturation of unsaturated and aromatic hydrocarbons).

The process of isolating the final product from the alkalized hydrogenated product was carried out in a rectification unit (Fig. 1), similar to that described in example 1.

The yield and quality parameters of the obtained hydrocarbon base for drilling fluids are presented in Table 8.

Thus, example 2 confirms the requirements stated in the problem of the invention for processing heavy fuel oil components and obtaining an increased yield of a hydrocarbon base of drilling fluids of appropriate quality. From the feedstock, as a result of catalytic hydrogenation at high pressure of a mixture of weighted middle distillate fractions obtained during the processes of secondary oil refining, and subsequent rectification of the alkalized hydrogenate, 51.9-61.1% of the target product is isolated, which is significantly higher than that of the prototype.

Example 3

As a raw material for the production of a hydrocarbon base for drilling fluids according to the second scheme, vacuum gas oil was used, obtained in the process of primary oil refining during vacuum distillation of fuel oil. The quality of vacuum gas oil during the run is presented in table 9.

A block diagram of a process for producing a hydrocarbon base for drilling fluids using vacuum gas oil as feedstock is shown in Figure 2.

Obtained on the block of vacuum distillation of fuel oil vacuum gas oil was sent to the block of deep hydrogenation (Fig. 2). The process of deep hydrogenation of the mixture was carried out at high pressure in three reactors installed in series on a catalyst containing hydrogenating components (nickel, molybdenum) in oxide form on an alumina support with the addition of silicon oxide. Before using the catalyst, it is sulfided.

The parameters of the hydrogenation process, the yield and quality of the obtained hydrogenated product are presented in Table 10.

The process of separating the final product from the hydrogenated product was carried out on a rectification unit (Fig. 2) according to a one-column version using an atmospheric rectification column. From the upper part of the column, gases and gasoline fraction dissolved in the hydrogenate are taken. The selection of the required fraction, which is a hydrocarbon base for drilling fluids, is performed in the form of an intermediate product. In order to remove light hydrocarbons from the product and, as a consequence, achieve the required value for the flash point, the resulting fraction is sent to the stripping section for additional stripping of low-boiling hydrocarbons with steam. The heavy residue is removed as a bottom product of the column. The operating mode of the string equipment and the fractional composition of the final product (boiling range 195-320 ° C) ensure the production of a hydrocarbon base for drilling fluids of the required quality. The yield and quality parameters of the obtained hydrocarbon base for drilling fluids are presented in Table 11.

Thus, Example 3 also confirms the requirements for processing heavy fuel oil components and obtaining an increased yield of a hydrocarbon base for drilling fluids of appropriate quality, as claimed in the task of the invention. More than 20.0% of the target product is isolated from the raw material as a result of catalytic hydrogenation at high pressure of vacuum gas oil and subsequent rectification of the hydrogenated product, which is significantly higher than that of the prototype.

Example 4

To confirm the possibility of achieving the claimed technical result, a test was carried out of a drilling fluid containing, as a basis, a hydrocarbon base obtained during the run according to example 1. A water-hydrocarbon emulsion of the following composition was used as a basis for the drilling fluid:

- a sample of the proposed invention - 60 vol. %;

- aqueous brine CaCl ₂ (concentration 38 wt.%) - 40 vol. %.

As other components of the solution, various functional additives were used, taking into account the following volumetric ratio of them to the volume of the resulting solution:

- emulsifier - 0.02 m ³ : 1 m ³ solution;

- water repellent - 0.01 m ³ : 1 m ³ solution;

- organobentonite - 0.02 m ³ : 1 m ³ solution;

- filtration regulator - 0.012 m ³ : 1 m ³ solution;

- rheology regulator - 0.012 m ³ : 1 m ³ solution.

The resulting mixture was brought to the final drilling fluid by adding a bridging agent (ground marble) to a density of the final product of 1.25 g / cm ³ .

The results of laboratory tests of the obtained experimental sample of drilling mud are shown in Table 12.

The presented data indicate that the prototype has the required rheological parameters that allow it to be used as a drilling fluid in the technological process of drilling gas and oil wells. This, in turn, confirms the possibility of achieving the claimed technical result, provided that the invention is used.

Claims (1)

A method of obtaining a hydrocarbon base for drilling fluids, which consists in the fact that a mixture of weighted middle distillate fractions of primary and secondary oil refining processes, boiling away in the temperature range from 155 to 455 ° C, or vacuum gas oil obtained by distilling fuel oil, boiling off in the temperature range from 280 to 460 ° C, subjected to a deep hydrogenation process: the indicated mixtures of weighted middle distillate fractions - at a temperature of 325-420 ° C and a pressure of 20.0-31.0 MPa on a nickel-tungsten-sulfide catalyst with the addition of aluminum oxide or on a catalyst containing hydrogenating components - nickel, molybdenum in oxide form, said vacuum gas oil - at a temperature of 350-420 ° C and a pressure of 23.0-32.0 MPa on a catalyst containing hydrogenating components - nickel, molybdenum in oxide form on an alumina carrier with the addition of silicon oxide, the hydrogenated product obtained in the process of deep hydrogenation of raw materials is additionally treated with an aqueous solution of alkali and Rectification is carried out with the release of the target fraction of the hydrocarbon base for drilling fluids, boiling in the range of 195-320 ° C, having the following qualitative characteristics - the content of aromatic compounds is not more than 3 wt.%, the total sulfur is not more than 0.001 wt.%, the pour point is not higher than minus 40 ° С, flash point in a closed crucible not lower than 80 ° С.

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