Method of producing a drag reducer

Abstract

A method of producing a reagent for reducing the hydrodynamic resistance of a turbulent flow of liquid hydrocarbons in pipelines comprises mixing a fine powder of polyalphaolefin, in sizes of 0.1-1.5 mm, with solvents which do not dissolve the polyalphaolefin and consist of a mixture of a monofunctional heteroatomic organic compound with 3 to 16 carbon atoms, a bifunctional heteroatomic organic compound with 3 to 16 carbon atoms, and a separating agent (anti-caking agent). The ratio of components in the composition is as follows: 75 to 90 wt% fine powder of polyalphaolefin, 2 to 15 wt% separating agent, 1 to 10 wt% monofunctional heteroatomic organic compound, and 1 to 10 wt% bifunctional heteroatomic organic compound. The claimed method makes it possible to produce a stable product with a high active substance content, and this makes it possible to decrease the resistance of a flow of oil or gas condensate being transported and decrease the prime cost of the product and the cost of transporting the oil or gas condensate.

Description

[0001] METHOD FOR PRODUCING ANTI-TURBULENCE ADDITIVE

[0002] Field of technology

[0003] This invention relates to the petroleum and petrochemical industries, specifically to the use of pipeline transport of liquid hydrocarbons, and specifically to methods for reducing their hydrodynamic drag during transportation. The proposed invention relates to drag reducing additives (DRA) that reduce the hydrodynamic drag of turbulent flow of hydrocarbon liquids in pipelines, in particular, to fast-dissolving and hydrocarbon-soluble dry dispersions (FD DRA) of high- and ultra-high-molecular-weight (UHMW) (co)polymers that reduce the hydrodynamic drag of turbulent flow in pipelines and contain complex anti-agglomerants and other additives.

[0004] State of the art

[0005] A known method for producing a polymer involves obtaining a finely ground polymer soluble in hydrocarbon liquids. The polymer is synthesized by (co)polymerization of higher alpha-olefins using a Ziegler-Natta catalyst. A product of block polymerization is used as the (co)polymer of higher alpha-olefins. A fine polymer dispersion is obtained by thermal reprecipitation of the polymer in a liquid that is non-solvent for the polymer at room temperature and capable of dissolving it at elevated temperatures (see patent RU 2481357 C1, May 10, 2013).

[0006] The disadvantages of this method of producing the polymer are low yield of the commercial form, significant energy costs, loss of the spatial structure of the polymer when converted into a dissolved state at elevated temperatures, and the need for increased dosages of the additive obtained in this way to maintain acceptable efficiency.

[0007] A method is known for obtaining a non-aqueous suspension that reduces the resistance to the flow of hydrocarbons in pipelines (see patent EA 001538 dated 15.10.1996), which includes a method for forming a stable non-aqueous suspension of a solid, hydrocarbon-soluble, drag reducing additive based on a polyolefin, capable of reducing the hydrodynamic resistance to hydrocarbon flow, in a pipeline, comprising (a) fine (low-temperature) grinding of the polyolefin in the presence of a separating agent to obtain a free-flowing material based on a polyalphaolefin, coated with said separating agent, and b) dispersing the coated polyalphaolefin particles in a substantially non-aqueous suspension medium selected from the group consisting of higher alcohols (<14 C carbon atoms) and glycols (<14 C carbon atoms), and dipropylene glycol methyl ether, tripropylene glycol methyl ether, tetrapropylene glycol methyl ether or ethyl esters of a similar nature, where the separating agent is a fatty acid wax. In this case, mixtures of glycol ethers can be used as suspending agents.

[0008] The closest in essence and achievable technical result is a method for producing an agent for reducing the hydrodynamic drag of hydrocarbon flows (see patent RU 2599986 dated 20.10.2016), which is a stabilized powdered high-molecular polyalphaolefin. The method involves the polymerization of higher alpha-olefins in a medium of fluorinated organic compounds using a titanium-magnesium catalyst modified with an electron-donor compound, followed by the isolation of the powdered polyalphaolefin and its stabilization by the addition of an anti-agglomerant. The electron-donor compound is glycol ethers or phthalic acid esters. Synthesis is carried out at a given ratio of the system components. The drag-reducing agent is characterized by the following component ratio by weight, %: polyalpha-olefin 80-90%, anti-agglomerant 10-20%.

[0009] A disadvantage of this method and its analogs is its low energy efficiency, as it involves interrupting the polymerization process when conversion reaches an average of 40-95%, adding a dispersion medium containing an anti-agglomerant, decanting the polyalpha-olefin suspension, washing the (co)polymer suspension using filter materials, and vacuum drying at 40-60°C to remove unreacted monomer and residual amounts of halogenated organic solvents. The resulting material cannot be used for feeding liquid hydrocarbons transported through a pipeline without a carrier fluid.

[0010] A significant difference is the use of a finely dispersed polymer powder with particle sizes from 10 to 1500 µm, and its treatment with auxiliary materials from the group of monofunctional heteroatomic organic compounds, preferably higher fatty alcohols, and bifunctional heteroatomic organic compounds, preferably glycol derivatives, with a carbon skeleton size from 3 to 16 units with the following distribution by composition, wt.%:

[0011] Finely dispersed polyalphaolefin powder from 75 to 90

[0012] Separating agent (anti-agglomerator) from 2 to 15

[0013] A monofunctional heteroatomic organic compound with a carbon skeleton size from 3 to 16 units from 1 to 10

[0014] A bifunctional heteroatomic organic compound with a carbon skeleton size from 3 to 16 units from 1 to 10.

[0015] The product obtained in this way has satisfactory mechanical properties and can be used to feed hydrocarbon liquid into a stream transported through a pipeline using a dosing device designed for working with powdered polymer materials.

[0016] Disclosure of invention

[0017] The objective of the invention is to obtain a reagent (drag reducing additive) with a high content of active base for reducing the hydrodynamic resistance of the flow of liquid hydrocarbons, which can be dosed in powder form.

[0018] The technical result of the invention is the production of a product characterized by a high, at least 75% by weight, content of the active substance - ultra-high molecular weight polyalphaolefin, which is stable and can be dosed into a pipeline of transported oil or gas condensate at high pressure by means of any known dosing device designed for working with powder materials, thereby making it possible to achieve a reduction in the resistance of the flow of pumped oil or gas condensate, as well as a reduction in the costs of transporting oil and gas condensate.

[0019] The stated task and technical result are achieved by obtaining a reagent for reducing the hydrodynamic resistance of the turbulent flow of liquid hydrocarbons in pipelines - an anti-turbulent additive, with a high content of the active base, not less than 75 wt.% polymer content, by mixing a polymer having the properties of reducing the hydrodynamic resistance of the turbulent flow of liquid hydrocarbons, with sizes of 10 - 1500 μm, obtained by any known method, with solvents that do not dissolve it, with the following ratio of components by composition, wt.%:

[0020] Finely dispersed polyalphaolefin powder from 75 to 90

[0021] Separating agent (anti-agglomerator) from 2 to 15

[0022] A monofunctional heteroatomic organic compound with a carbon skeleton size from 3 to 16 units from 1 to 10

[0023] A bifunctional heteroatomic organic compound with a carbon skeleton size from 3 to 16 units from 1 to 10.

[0024] The polymer is mixed with non-solvent polymer solvents, preferably using mixing equipment for powder polymer materials of any design.

[0025] In a particular embodiment, the polymer powder is mixed with a mixture of glycol with a number of carbon atoms from 2 to 12 and a fatty alcohol with a number of carbon atoms from 4 to 16 in a ratio of polymer powder / mixture of glycol and fatty alcohol - 85 parts by weight / 15 parts by weight.

[0026] The product obtained by the described method is preferably fed into the flow of hydrocarbon liquid transported through a pipeline using a dosing device that mechanically moves the product material by means of a screw auger or a screw feeder, for example, a screw extruder for polymer materials, either directly into the flow of hydrocarbon liquid, or into an intermediate tank for mixing the material with the liquid flow and directing the resulting mixture into the main flow of the pipeline.

[0027] Implementation of the invention

[0028] In this section of the description, the most preferred embodiment of the invention will be given, which, however, does not limit other possible embodiments that clearly follow from the application materials and are understandable to a specialist.

[0029] The method for producing a reagent for reducing the hydrodynamic drag of turbulent flow of liquid hydrocarbons in pipelines is carried out in the following most preferred manner. This method involves using as a starting polymer any polymer capable of reducing the hydrodynamic drag of liquid hydrocarbon flow, obtained, for example, by the known method according to patent RU 2648079 C1 (published 22.03.2018, Bulletin No. 9), in which a UHMWPO polymer with a molecular weight of 1-10 is obtained. 7 -2-10 7a.m.u., a molecular weight distribution of less than 1.5, with a conversion above 90 wt.%, which makes it possible to reduce energy costs for grinding, for example, in a liquid nitrogen environment at a temperature of no higher than minus 65 and no less than minus 120 degrees Celsius, when obtaining dry polymer dispersions with a concentration of more than 75 wt.% in a mixture with non-solvent polymer solvents for drag reducing additives, to protect the polymer from oxidative degradation during storage, to significantly reduce the cost of reagents for reducing the hydrodynamic resistance of oil and petroleum products transported through pipelines, obtained by the proposed method.

[0030] The polymer blocks obtained in accordance with patent RU 2648079 C1 are ground to the required size, for example, using suitable cryogenic grinding equipment, after which they are mixed with non-solvent polymer solvents, obtaining a product with a polymer content of at least 75 wt.%, which is fed into the flow of hydrocarbon liquid pumped through a pipeline using a dosing device designed for working with powdered polymer materials.

[0031] The monomers used in obtaining polymer blocks are C6-C14 alpha-olefins, preferably hex-1-ene, oct-1-ene, dec-1-ene, dodec-1-ene, tetradec-1-ene, and mixtures thereof, most preferably hex-1-ene, dec-1-ene, dodec-1-ene and mixtures thereof with a content of the main alpha-olefin in an amount of at least 70 wt.%.

[0032] Mixtures of a monofunctional heteroatomic organic compound (MFHOC) and a bifunctional heteroatomic organic compound (BHOC) are used as a non-solvent polymer solvent, wherein: organic compounds containing oxygen and nitrogen as a heteroatom can be used as MFHOC - isomers of propanol, butanol, pentanol, hexanol, heptanol, octanol, nonanol, decanol, undecanol, dodecanol, tridecanol, tetradecanol, pentadecanol, hexadecanol, isomers of tripropylamine, tributylamine, tripentylamine, trihexylamine, triheptylamine, trioctylamine, trinonylamine, tridecylamine, triundecylamine, tridodecylamine, tritridecylamine, tritetradecylamine, tripentadecylamine, trihexadecylamine;organic compounds containing oxygen, nitrogen, sulfur, phosphorus as a heteroatom can be used as BFGOS - tripropyl phosphate, tributyl phosphate, tripentyl phosphate, propylene glycol, butyl cellosolve, hexylene glycol, ethyl cellosolve, texanol, diethylene glycol, triethylene glycol, isophorone, morpholine, dioxane, dimethyl sulfoxide, dimethylformamide.

[0033] For mechanical mixing of polymer powder with non-solvent polymer solvents, mixers for powder polymer materials of any design can be used, for example: devices from Pallmann Maschinenfabrik GmbH&Co KG (Germany), Sibprommash LLC (Russian Federation, Novosibirsk).

[0034] For dosing a product with a high, at least 75% by weight, polymer content, dosing devices that mechanically move the product material by means of a screw auger or a screw feeder or similar ones from Kinematica AG (Switzerland), IKA-WERKE GmbH&Co. KG (Germany), extruders Krauss Maffei Berstorff AG (Germany) or similar ones can be used.

[0035] The method for obtaining a reagent for reducing the hydrodynamic resistance of the flow of liquid hydrocarbons in pipelines is explained by the examples presented below, but is not limited to it.

[0036] Example 1 (analogous to 1Ш 2599986)

[0037] A three-necked 250 ml flask equipped with an argon vacuum line and a mechanical stirrer was heated in vacuum for 5-10 min. Into the flask, cooled with ice water to 12-14 °C, were placed 40 ml (71.37 g) of perfluoromethylcyclohexane, 80 ml (54.24 g) of hexene-1, 0.5 ml of TIBA (4 M) and 0.2 ml of a catalyst prepared as follows: Into a 100 ml flask with a magnetic stirrer in an argon flow were placed 5 g (44 mmol) of magnesium ethylate, 40 ml of absolute toluene, 10 ml of titanium tetrachloride and 0.95 ml (0.80 g, 5 mmol) of 2,2-diethylpropanediol-1,3 dimethyl ether. The mixture was heated to 115°C (external bath temperature) for 2 h with stirring. The liquid layer was then decanted, and the precipitate was washed with 2 x 40 ml of toluene at 40°C. After washing, 40 ml of absolute toluene and 8 ml of titanium tetrachloride were placed in the flask, and the mixture was heated to 115°C for 1.5 h with stirring. The precipitate was then washed with 10 x 40 ml of 70 / 100 petroleum ether at 55°C, and the precipitate was suspended in 40 ml of 70 / 100 petroleum ether.50 ml of catalyst suspension with a titanium concentration of 0.06 mol / l was obtained.

[0038] The mixture was stirred for 4 hours and then warmed to room temperature (~5 min). A suspension of 4.5 g of calcium stearate in 41 g of butyl cellosolve was added. The mixture was vigorously stirred for 20 minutes, then stopped, and after 10 minutes, the precipitated perfluoromethylcyclohexane was decanted. The remaining perfluoromethylcyclohexane and monomer were distilled off under vacuum. The product was then washed twice with 20 ml of acetone, filtered, and dried. The mass of the resulting polymer powder was 41.68 g (69% conversion). The polymer content was 89.2%.

[0039] Example 2

[0040] The polymer is obtained according to patent RU 2648079 C1 as follows. Hex-1-ene in an amount of 75 wt.%, dec-1-ene in an amount of 10 wt.%, decalin with a purity of at least 99.8 wt.% in an amount of 11.91 wt.%, cyclooctadecane with a purity of at least 99.8 in an amount of 3.00 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled in a nitrogen stream to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. Then, a catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum in a 1:1 weight ratio in an amount of 0.077 wt.% (0.0385 wt.% each) and a catalyst—titanium trichloride—in an amount of 0.013 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane are fed into the reactor. The reactor contents are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour.The reaction mass is then unloaded in a nitrogen stream into sealed, gas-tight containers with polyethylene liners so that the mass layer height does not exceed 250 mm, or into polymer containers of similar size, hermetically sealed and maintained at a temperature of 15 ± 5 ° C for at least 15 days without access to the atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm in size. The final grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate. A non-solvent solvent consisting of a mixture of isopropanol and ethylene glycol in a ratio of 8: 2 by weight is added to the resulting polymer powder, obtaining a reagent for reducing the hydrodynamic resistance of the flow of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80 ± 5 wt.%.

[0041] Example 3

[0042] The polymer is obtained according to patent RU 2648079 C1 as follows. Hex-1-ene in an amount of 84 wt.%, tetradecene-1 in an amount of 5 wt.%, dodecane with a purity of at least 99.8 wt.% in an amount of 5.91 wt.%, cyclooctane with a purity of at least 99.8 wt.% in an amount of 5.00 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. Then, a catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum in a 1:1 weight ratio in an amount of 0.077 wt.% (0.0385 wt.% each) and a catalyst—titanium trichloride—in an amount of 0.013 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane are fed into the reactor. The reactor contents are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour.The reaction mass is then unloaded in a nitrogen stream into sealed, gas-tight containers with polyethylene liners so that the mass layer height does not exceed 250 mm, or into polymer containers of similar size, hermetically sealed and maintained at a temperature of 15 ± 5 ° C for at least 15 days without access to the atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm in size. The final grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate. A non-solvent solvent consisting of a mixture of butyl cellosolve and ethylene glycol in a 6:4 weight ratio is added to the resulting polymer powder, obtaining a reagent for reducing the hydrodynamic resistance of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80 ± 5 wt.%.

[0043] Example 4

[0044] The polymer is obtained according to patent RU 2648079 C1 as follows. Hex1-ene in an amount of 80 wt.%, decene-1 in an amount of 5 wt.%, decalin with a purity of at least 99.8 wt.% in an amount of 14.81 wt.%, cyclooctadecylcyclooctadecane with a purity of at least 99.8 wt.% in an amount of 0.1 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. Then, a catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum with a mass ratio of 10:1 in an amount of 0.077 wt.% (0.07 wt.% and 0.007 wt.%, respectively) and a catalyst - titanium trichloride are fed into the reactor.

[0045] - in the amount of 0.013 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane. The contents of the reactor are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour. Then, the reaction mass is unloaded in a stream of nitrogen into sealed gas-tight containers with polyethylene liners so that the height of the mass layer does not exceed 250 mm, or polymer containers of similar sizes, hermetically sealed and maintained at a temperature of 15 ± 5 °C for at least 15 days without access to the air atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of sizes 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm. The final grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate.A non-solvent solvent consisting of a mixture of ethyl cellosolve and propyl glycol in a 5:5 ratio by weight is added to the resulting polymer powder, resulting in a reagent for reducing the hydrodynamic resistance of the flow of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80±5 wt.%.

[0046] Example 5

[0047] The polymer is obtained according to patent RU 2648079 C1 as follows. Hex-1-ene in an amount of 80 wt.%, dec-1-ene in an amount of 5 wt.%, decane with a purity of at least 99.8 wt.% in an amount of 12.91 wt.%, cyclohexadecane with a purity of at least 99.7 wt.% in an amount of 2.00 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. Then, a catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum with a mass ratio of 1:10 in an amount of 0.077 wt.% (0.007 wt.% and 0.07 wt.%, respectively) and a catalyst - titanium trichloride are fed into the reactor.

[0048] - in the amount of 0.013 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane. The contents of the reactor are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour. Then the reaction mass is unloaded in a stream of nitrogen into sealed gas-tight containers with polyethylene liners so that the height of the mass layer does not exceed 250 mm, or polymer containers of similar sizes, hermetically sealed and maintained at a temperature of 15 ± 5 °C for at least 15 days without access to the air atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of sizes 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm. The last grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate.A non-solvent solvent consisting of a mixture of octanol and ethylene glycol in a ratio of 8:2 by weight is added to the resulting polymer powder, resulting in a reagent for reducing the hydrodynamic resistance of the flow of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80±5 wt.%.

[0049] Example 6

[0050] The polymer is obtained according to patent RU 2648079 C1 as follows. Octene-1 in an amount of 80 wt.%, hexene-1 in an amount of 15 wt.%, decane with a purity of at least 99.8 wt.% in an amount of 2.91 wt.%, cyclotetradecylcyclohexadecane with a purity of at least 99.8 wt.% in an amount of 2.00 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. A catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum in a 1:1 weight ratio in an amount of 0.077 wt.% (0.0385 wt.% each) and a catalyst—titanium trichloride—in an amount of 0.013 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane are then fed into the reactor. The reactor contents are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour.The reaction mass is then unloaded in a nitrogen stream into sealed, gas-tight containers with polyethylene liners so that the mass layer height does not exceed 250 mm, or into polymer containers of similar size, hermetically sealed and maintained at a temperature of 15 ± 5 ° C for at least 15 days without access to the atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm in size. The final grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate. A non-solvent solvent consisting of a mixture of phosphobutane and ethylene glycol in a 4:6 weight ratio is added to the resulting polymer powder, obtaining a reagent for reducing the hydrodynamic resistance of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80 ± 5 wt.%.

[0051] Example 7

[0052] The polymer is obtained according to patent RU 2648079 C1 as follows. Hex-1-ene in an amount of 70 wt.%, dodec-1-ene in an amount of 5 wt.%, hexadecane with a purity of at least 99.8 wt.% in an amount of 19.908 wt.%, cyclooctane with a purity of at least 99.8 wt.% in an amount of 5.00 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. A catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum in a 1:1 weight ratio in an amount of 0.077 wt.% (0.0385 wt.% each) and a catalyst—titanium trichloride—in an amount of 0.015 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane are then fed into the reactor. The reactor contents are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour.The reaction mass is then unloaded in a nitrogen stream into sealed, gas-tight containers with polyethylene liners so that the mass layer height does not exceed 250 mm, or into polymer containers of similar size, hermetically sealed and maintained at a temperature of 15 ± 5 ° C for at least 15 days without access to the atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm in size. The final grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate. A non-solvent solvent consisting of a mixture of n-butanol and ethylene glycol in a ratio of 8: 2 by weight is added to the resulting polymer powder, obtaining a reagent for reducing the hydrodynamic resistance of the flow of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80 ± 5 wt.%.

[0053] Example 8

[0054] The polymer is obtained according to patent RU 2648079 C1 as follows. Dodec-1-ene in an amount of 90 wt.%, dec-1-ene in an amount of 5 wt.%, decane with a purity of at least 99.8 wt.% in an amount of 2.92 wt.%, cyclohexadecane with a purity of at least 99.8 wt.% in an amount of 2.00 wt.% are loaded into a reactor with a jacket, stirrer, thermocouple, pressure gauge, and gaseous nitrogen with a purity of 99.9 wt.%. The mixture in the reactor is cooled to a temperature of plus 10±2 °C by stirring with a stirrer and feeding a cold coolant into the reactor jacket. Then, a catalyst activator in the form of a mixture of diethylaluminum chloride and triisobutylaluminum in a 1:1 weight ratio in an amount of 0.077 wt.% (0.0385 wt.% each) and a catalyst—titanium trichloride—in an amount of 0.003 wt.% in the form of a suspension with a concentration of 40 wt.% in heptane are fed into the reactor. The reactor contents are stirred, maintaining the temperature in the range from plus 8 to plus 12 °C, for 1 hour.The reaction mass is then unloaded in a nitrogen stream into sealed, gas-tight containers with polyethylene liners so that the mass layer height does not exceed 250 mm, or into polymer containers of similar size, hermetically sealed and maintained at a temperature of 15 ± 5 ° C for at least 15 days without access to the atmosphere. The resulting polymer blocks are successively ground using a cascade of knife mills into particles of 50 ± 40 mm, 3 ± 2 mm and 0.8 ± 0.7 mm in size. The final grinding is carried out in a liquid nitrogen environment in the presence of 15 wt.% calcium stearate. A non-solvent solvent consisting of a mixture of 1-hecanol and propylene glycol in a 5:5 weight ratio is added to the resulting polymer powder, obtaining a reagent for reducing the hydrodynamic resistance of oil and petroleum products in pipelines - a stable fine dispersion with a polymer content of 80 ± 5 wt.%.

[0055] The method of dosing an anti-turbulent additive with a high content of active base into a flow of hydrocarbon liquid transported through a pipeline is carried out in the following most preferred manner.

[0056] The reagent (PTP) obtained in accordance with the method described above is taken and loaded into the hopper mixer 101 equipped with an agitator and a loading unit into the screw dispenser 102. Next, the reagent (PTP) is fed from the hopper mixer 101 into the screw dispenser 102, which ensures dosing of the reagent into the preparation tank 103, where the obtained reagent is dissolved. In front of the preparation tank 103, a hydrocyclone mixing unit (hydrocyclone mixer 104) of the reagent with the hydrocarbon liquid and a check valve 105 are installed. Passing through the hydrocyclone mixer 104, the reagent is mixed with the hydrocarbon liquid, which is fed from the pipeline 106 through the tap 107, the receiving flow meter 108, the pressure-reducing valve 109. Next, in the preparation tank 103, the reagent is dissolved to the required state (to a homogeneous state - suspension). From the preparation tank 103, the resulting suspension is fed into the pipeline through the feed flow meter 110 using a gear pump 111 installed in the line.To prevent the backflow of hydrocarbon liquid from the pipeline into the preparation tank 103, when the pump is stopped or the station is being repaired, the supply line is equipped with a check valve 112 and a tap 113. The dosing of the reagent is regulated by the revolutions of the auger dispenser 102 and is controlled by the difference in the masses of the liquids passing through the receiving flow meter 108 and the supply flow meter 110.

[0057] The dosing scheme described above is shown in Figure 1 (Fig. 1).

[0058] The effectiveness of the resulting products was assessed using a laboratory turborheometer (see table). The reduction in hydrodynamic resistance (DR) to the movement of nefras in a capillary in the presence of the reagent was calculated using the formula: where l is the coefficient of liquid resistance; t is the flow time of 330 cm 3 nefras through a capillary o and p are indices related to the pure solvent and the reagent solution, respectively.

[0059] The product is considered to have passed the tests if the DR value is at least 30% at a reagent concentration in nefras of 2.5 million. 1 .

[0060] Table

[0061] Thus, as follows from the presented examples and table, it can be concluded that the claimed method, in comparison with analogs, including the closest one, allows for the production of a reagent that most fully ensures a reduction in the hydrodynamic resistance of the turbulent flow of liquid hydrocarbons in pipelines and, as a consequence, an increase in the pipeline capacity and a reduction in the costs of transporting hydrocarbon liquids.

Claims

1. A method for the preparation of a reagent for reducing the hydrodynamic drag of a turbulent flow of liquid hydrocarbons in pipelines, characterized by a high polymer content of at least 75 wt %, comprising mixing a polyalphaolefin powder reducing the hydrodynamic drag of a turbulent flow of liquid hydrocarbons with polymer non-solving solvents and a separating agent (anti-agglomerating agent), wherein the polymer non-solving solvents are a mixture of a monofunctional heteroatomic organic compound with carbon atoms from 3 to 16, and a bifunctional heteroatomic organic compound with carbon atoms from 2 to 16, with the following ratio of the components, wt %:Polyalphaolefin powder from 75 to 90Separating agent (anti-agglomerating agent) from 2 to 15Monofunctional heteroatomic organic compound with the number of carbon atoms from 3 to 16 from 1 to 10,Bifunctional heteroatomic organic compound with the number of carbon atoms from 2 to 16 from 1 to 10,wherein the monofunctional heteroatomic organic compound is at least one of isomers of propanol, butanol, pentanol, hexanol, heptanol, octanol, nonanol, decanol, undecanol, dodecanol, tridecanol, tetradecanol, pentadecanol, hexadecanol, isomers of tripropylamine, tributylamine, tripentylamine, trihexylamine, triheptylamine, trioctylamine, trinonylamine, tridecylamine. triundecylamine, tridodecylamine, tritridecylamine, tritetradecylamine, tripentadecylamine, trihexadecylamine,wherein the bifunctional heteroatomic organic compound is at least one of tripropyl phosphate, tributyl phosphate, tripentyl phosphate, propylene glycol, butylene glycol, butyl cellosolve, hexylene glycol, ethyl cellosolve, texanol, diethylene glycol, triethylene glycol, isophorone, morpholine, dioxane, dimethyl sulphoxide, dimethylformamide. 2. The method of claim 1, wherein the polyalphaolefin powder and the mixture of monofunctional heteroatomic organic compound and bifunctional heteroatomic organic compound are taken in the ratio 85 parts by weight / 15 parts by weight.  3. A powder reagent reducing the hydrodynamic drag of a turbulent flow of liquid hydrocarbons in pipelines comprising the following components, wt %:Polyalphaolefin powder from 75 to 90Separating agent (anti-agglomerating agent) from 2 to 15Monofunctional heteroatomic organic compound with the number of carbon atoms from 3 to 16 from 1 to 10Bifunctional heteroatomic organic compound with the number of carbon atoms from 2 to 16 from 1 to 10,wherein the monofunctional heteroatomic organic compound is at least one of isomers of propanol, butanol, pentanol, hexanol, heptanol, octanol, nonanol, decanol, undecanol, dodecanol, tridecanol, tetradecanol, pentadecanol, hexadecanol, isomers of tripropylamine, tributylamine, tripentylamine, trihexylamine, triheptylamine, trioctylamine, trinonylamine, tridecylamine. triundecylamine, tridodecylamine, tritridecylamine, tritetradecylamine, tripentadecylamine, trihexadecylamine,wherein the bifunctional heteroatomic organic compound is at least one of tripropyl phosphate, tributyl phosphate, tripentyl phosphate, propylene glycol, butylene glycol, butyl cellosolve, hexylene glycol, ethyl cellosolve, texanol, diethylene glycol, triethylene glycol, isophorone, morpholine, dioxane, dimethyl sulphoxide, dimethylformamide. 4. The reagent of claim 3, wherein the monofunctional heteroatomic organic compound is fatty alcohol with the number of carbon atoms from 4 to 16. 5. The reagent of claim 3, wherein the bifunctional heteroatomic organic compound is glycol with the number of carbon atoms from 2 to 12. 6. A method for reduction of the hydrodynamic drag of the turbulent flow of liquid hydrocarbons in pipelines comprising injection of the reagent of claim 3 into the flow of hydrocarbon fluid transported through the pipeline, wherein injection of the reagent is performed by means of an injection apparatus for polymer powders. 7. The method of claim 6, wherein the reagent is dissolved in the hydrocarbon fluid into the state of slurry before it is injected into the pipeline. 8. A method for injection of the powder reagent of claim 3 into the flow of a hydrocarbon fluid transported through a pipeline, wherein the reagent is fed into a mixer hopper, then the reagent with the hydrocarbon fluid, which is supplied from the pipeline through a valve, a flow meter, and a pressure reducing valve goes from the screw feeder through a hydro cyclone mixer and a back valve to a preparation tank for dissolving the prepared reagent into the state of slurry, then the dissolved reagent is fed through the flow meter using a gear pump back into the pipeline. 

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