Process for the preparation of a drag reducing agent, drag reducing agent, method for reducing the flow resistance of a liquid hydrocarbon in a pipeline, and method for injecting a drag reducing agent into a hydrocarbon fluid transported through a pipeline

Abstract

The present invention is applied in the field of inorganic and polymer chemistry, i.e. the field of pipeline transportation of oil and oil products. The invention discloses a method for preparing a reagent for reducing the flow resistance of liquid hydrocarbons in pipelines, characterized by a polymer content of at least 75 wt%, comprising mixing 0.1-1.5 mm polymer with a polymer non-dissolving solvent to reduce the flow resistance of liquid hydrocarbons. The product prepared is in the form of a commodity of a reagent with a high polymer content of at least 75 wt% for reducing the hydrodynamic resistance of liquid hydrocarbons flowing in pipelines. The product prepared according to the method is injected into the flow of hydrocarbon fluid transported through pipelines using an injection device that mechanically moves the product using an auger or a screw feeder. The technical result of the invention is the preparation of a product with a high active substance content, stable, which can be injected at high pressure into pipelines for transporting oil or condensate, thus reducing the resistance of pumping oil or condensate, and reducing the cost of the product and the cost of transporting oil or condensate.

Description

Technical Field

[0001] This invention relates to pipeline transportation of liquid hydrocarbons in the petroleum and petrochemical industries, specifically for reducing flow resistance during transportation. The drag reducer is a fast-dissolving and hydrocarbon-soluble dry dispersion of high and ultra-high molecular weight (UHMW) (co)polymers that reduces the flow resistance of hydrocarbon fluids in pipelines and contains a composite anti-caking agent and other additives. Background Technology

[0002] One method involves producing a finely particulate polymer soluble in a carbonaceous liquid. This polymer is synthesized via the (co)polymerization of high-α-olefins in the presence of a Ziegler-Natta catalyst. The high-α-olefin (co)polymerization used is a casting polymerization product. The fine dispersion of the polymer is obtained by thermal reprecipitation in a liquid that is non-solvent to the polymer at room temperature but dissolves it at higher temperatures (see patent RU2481357C1, published May 10, 2013).

[0003] The disadvantages of this method of producing polymers are low production capacity in commercial form, high energy costs, loss of spatial structure when polymers dissolve at high temperatures, and the need to increase the dosage of reagents prepared in this way to maintain optimal efficiency.

[0004] A method for producing a non-aqueous suspension that reduces hydrocarbon resistance in pipelines (see patent EA001538, priority date October 15, 1996) includes forming a thermally stable, hydrocarbon-soluble solid non-aqueous suspension friction reducer, an olefin-based agent capable of reducing resistance in hydrocarbons flowing through the pipeline, comprising: (a) finely dividing (at low temperature) the solid polyolefin in the presence of a distributing agent to provide a free-flowing polyalphaolefin material coated with the distributing agent; and (b) dispersing the coated polyalphaolefin particles in a basic non-aqueous suspension medium selected from alcohols containing (<14 carbon atoms), glycols containing (<14 carbon atoms), and dipropylene glycol methyl ether, tripropylene glycol methyl ether, tetrapropylene glycol methyl ether, ethylene glycol methyl ether, or ethylene glycol ethyl ether, wherein the distributing agent is a fatty acid wax. Simple mixtures of ethylene glycol ethers can be used as suspending agents.

[0005] In terms of its properties and the technical effects achieved, the most similar method is used for producing a reagent to reduce the flow resistance of hydrocarbons (see patent RU2599986, published October 20, 2016), which is a stable powdered high-molecular-weight polyalpha-olefin. This method involves polymerizing a higher alpha-olefin in a fluorinated organic compound medium using a titanium-magnesium catalyst, modifying it with an electron donor compound, then extracting the powdered polyalpha-olefin and stabilizing it by adding an anti-agglomeration agent. The electron donor compound is a glycol ether or a phthalate. The synthesis is carried out under given proportions of system components. The hydrodynamic resistance reducer is characterized by the following component weight ratios: 80-90% polyalpha-olefin and 10-20% adhesion-reducing powder.

[0006] The disadvantages of this method and similar methods are their low energy efficiency, as the polymerization process is interrupted to achieve an average conversion rate of 40-95%, requiring the addition of a dispersion medium, including an anti-agglomerating agent, decanting of the polyalphaolefin suspension, washing of the (co)polymer suspension with a filter material, and vacuum drying at 40-60°C to remove unreacted monomers and residual halogenated organic solvents. The prepared material cannot be used to inject liquid hydrocarbons transported via pipeline into fluids without a carrier liquid.

[0007] The essential difference lies in the use of finely dispersed polymer powder with a particle size of 10 to 1500 μm, treated with auxiliary materials selected from monofunctional heteroatom organic compounds (preferably higher fatty alcohols) and difunctional heteroatom organic compounds (preferably diol derivatives), with 3 to 16 carbon atoms. The component ratios are as follows, by mass percentage:

[0008] Finely dispersed polyalphaolefin powder - 75 to 90;

[0009] Separating agent (anti-caking agent) – 2 to 15;

[0010] Monofunctional heteroatom organic compounds with 3 to 16 carbon atoms: 1 to 10;

[0011] Bifunctional heteroatom organic compounds with 3 to 16 carbon atoms: 1 to 10.

[0012] Products prepared in this manner have satisfactory mechanical properties and can be used to inject hydrocarbon fluids transported through pipelines using a powdered polymer material injection device. Summary of the Invention

[0013] The purpose of this invention is to prepare a reagent (drag reducer) containing a large amount of active base to reduce the flow resistance of liquid hydrocarbons. This reagent can be added in powder form.

[0014] The technical achievement of this invention is the preparation of a product containing 75 wt% of an active substance, which is an ultra-high molecular weight polyalphaolefin. This substance is stable and can be injected into pipelines for high-pressure transportation of petroleum or condensate using any powder injection device, thereby reducing the resistance to the flow of pumped petroleum or condensate and lowering the transportation cost of petroleum or condensate.

[0015] The objective and technical result of this invention is to prepare a reagent for reducing the flow resistance of liquid hydrocarbons in pipelines. This reagent is a drag-reducing agent containing a large amount of active base and at least 75 wt% polymer, achieved by mixing the polymer with a solvent that does not dissolve it, according to any known method. The polymer has the property of reducing the flow resistance of liquid hydrocarbons with a particle size of 10-1500 micrometers, influenced by the following component ratios, by mass percentage:

[0016] Finely dispersed polyalphaolefin powder - 75 to 90;

[0017] Separating agent (anti-caking agent) – 2 to 15;

[0018] Monofunctional heteroatom organic compounds with 3 to 16 carbon atoms: 1 to 10;

[0019] Bifunctional heteroatom organic compounds with 3 to 16 carbon atoms: 1 to 10.

[0020] The polymer is mixed with a non-dissolving polymer solvent, preferably using any polymer powder mixing equipment.

[0021] In a specific implementation scheme, the polymer powder is mixed with a mixture of ethylene glycol having 2 to 12 carbon atoms and a fatty alcohol having 4 to 16 carbon atoms, wherein the ratio of polymer powder to the mixture of ethylene glycol and fatty alcohol is 85 parts (by weight) / 15 parts (by weight).

[0022] The product prepared according to the method is preferably injected into a hydrocarbon fluid transported through a pipeline using an injection device that mechanically moves the product by means of an auger or screw feeder, for example, a screw extruder for polymer materials, or directly into the flowing hydrocarbon fluid or into an intermediate container that mixes the material with the flowing liquid and flows the prepared mixture into the main stream of the pipeline. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the drug delivery method of the present invention. Detailed Implementation

[0024] This section describes the main embodiments of the invention, but does not limit other possible embodiments that are expressly described in the application materials and are obvious to those skilled in the art.

[0025] The preparation method of the reagent for reducing the flow resistance of liquid hydrocarbons in pipelines is carried out by the following main steps.

[0026] The method involves using a primary polymer that reduces the flow resistance of liquid hydrocarbons. This primary polymer is prepared according to the method described in patent RU2648079C1 (published March 22, 2018, Journal No. 9), wherein the polymer (UHMPAO) has a molecular weight of 1.10. 7 ~2.10 7 The amu, with a molecular weight distribution of less than 1.5 and a conversion rate of more than 90 wt%, makes it possible to reduce the energy costs associated with grinding. For example, in the preparation of dry polymer dispersions using a non-solvent with a concentration of more than 75 wt% as a drag-reducing agent in liquid nitrogen at a temperature not higher than -65°C and not lower than -120°C, the polymer is protected from oxidative degradation during storage, and the cost of reagents that reduce the flow resistance of petroleum and petroleum products prepared according to the proposed method and transported by pipeline is significantly reduced.

[0027] The polymer block prepared according to patent RU2648079C1 is ground to the desired size using appropriate cryogenic grinding equipment and then mixed with a polymer non-dissolving solvent to prepare a product with a polymer content of at least 75 wt%. The product is then injected into a hydrocarbon fluid pumped through a pipeline using an injection device suitable for polymer powder.

[0028] The α-olefins are C6-C14, preferably 1-hexene, 1-octene, n-decene, 1-dodecene e-1,2-13C2 and 1-tetradecene and mixtures thereof, more preferably 1-hexene, n-decene and 1-dodecene e-1,2-13C2 and mixtures thereof, and the basic α-olefin content is at least 70 wt%.

[0029] Mixtures of monofunctional heteroatom organic compounds (MHOCs) and difunctional heteroatom organic compounds (BHOCs) are used as non-dissolving solvents for polymers. Among them, organic compounds containing oxygen and nitrogen as heteroatoms can be used as monofunctional heteroatom organic compounds, namely isomers of propanol, butanol, pentanol, hexanol, heptanol, octanol, nonanol, decanol, undecylol, dodecanol, tridecanol, tetradecanol, pentadecanol, and hexadecylol, as well as isomers of tripropylamine, tributylamine, tripentylamine, trihexylamine, triheptylamine, trioctylamine, trinonylamine, tridecanol, trihexadecylamine, tritetradecylamine, tridecylamine, and hexadecylamine. Organic compounds containing heteroatoms such as oxygen, nitrogen, sulfur, and phosphorus can be used as bifunctional heteroatom organic compounds, namely tripropyl phosphate, tributyl phosphate, tripentyl phosphate, propylene glycol, butanediol, butyl cellulose, hexanediol, ethyl cellulose, tert-alcohol, diethylene glycol, triethylene glycol, isophorone, morpholine, dioxane, dimethyl sulfoxide, and dimethylformamide.

[0030] For the mechanical mixing of polymer powders with non-dissolving polymer solvents, any polymer powder mixer can be used, for example, from Pallmann Maschinenfabrik GmbH & Co KG (Germany), OOO Sibprommash (Russian Federation, Novosibirsk).

[0031] For products containing a large amount of polymer of not less than 75 wt%, an injection device that mechanically moves the product by means of an auger or auger feeder can be used. This injection device is manufactured by Kinematica AG (Switzerland), IKA-WERKEGmbH&Co.KG (Germany), and Krauss Maffei Berstorff AG (Germany).

[0032] The preparation method of the reagent for reducing the flow resistance of liquid hydrocarbons in pipelines is illustrated by the examples given below, but is not limited thereto.

[0033] Example 1 (approximately RU2599986)

[0034] Heat a three-necked 250-ml flask equipped with an argon vacuum tube and a mechanical stirrer in a vacuum for 5 to 10 minutes. In a flask cooled to 12–14°C with ice water, add 40 ml (71.37 g) of perfluoromethylcyclohexane, 80 ml (54.24 g) of 1-hexene, 0.5 ml of triiodobenzoic acid (4 M), and 0.2 ml of a catalyst prepared according to the following steps: In an argon atmosphere, add 5 g (44 mmol) of magnesium ethoxide, 40 ml of anhydrous toluene, 10 ml of titanium tetrachloride, and 0.95 ml (0.80 g, 5 mmol) of 2,2-diethylpropylene glycol-1,3 to a 100 ml flask equipped with a magnetic stirrer; heat the mixture to 115°C (external temperature of the container) for 2 hours with stirring; then pour off the liquid layer and wash the precipitate with 2 × 40 ml of toluene at 40°C; after washing, add 40 ml of anhydrous toluene and 8 ml of titanium tetrachloride to the flask, and heat the mixture to 115°C for 1.5 hours with stirring; next, heat at 55°C with 10 × 40 ml of... The precipitate was washed with 70 / 100 petroleum ether and then suspended in 40 ml of 70 / 100 petroleum ether. A catalyst suspension with a titanium concentration of 0.06 mol / L was prepared in 50 ml.

[0035] The mixture was stirred for 4 hours, then heated to room temperature (approximately 5 minutes), and 4.5 g of calcium stearate suspension was added to 41 g of butyl cellulose solvent. The mixture was vigorously stirred for 20 minutes, then stirring was stopped, and the perfluoromethylcyclohexane precipitate was poured off over 10 minutes. The perfluoromethylcyclohexane and monomer residues were distilled off under vacuum. The product was then washed twice with 20 ml of acetone, filtered, and dried. The mass of the prepared polymer powder was 41.68 g (conversion rate 69%). The polymer mass fraction was 89.2%.

[0036] Example 2

[0037] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 75 wt% 1-hexene, 10 wt% n-decene, 11.91 wt% decahydronaphthalene with a purity of not less than 99.8 wt%, and 3.00 wt% cyclooctadecane with a purity of not less than 99.8 wt% were charged, and nitrogen gas with a purity of 99.9 wt% was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C in a nitrogen gas stream by stirring with a stirrer and supplying coolant to the reactor's isolation hood. Then, a catalyst activator was fed into the reactor in the form of a 1:1 mass ratio mixture of diethylaluminum chloride and triisobutylaluminum, at a dosage of 0.077 wt% (0.0385 wt% each), and titanium trichloride was added as a catalyst at a dosage of 0.013 wt%, in a suspension at a concentration of 40 wt% in heptane. The material in the stirred reactor is maintained at a temperature between +8 and +12°C for 1 hour. Next, the reactants are discharged in a nitrogen stream into a sealed, airtight container with a polyethylene liner, ensuring the material layer height does not exceed 250 mm, or discharged into a similar polymer container, sealed, and kept at 15±5°C without air contact for at least 15 days. The resulting polymer lumps are then pulverized using a series of blades into particles of 50±40 mm, 3±2 mm, and 0.8±0.7 mm in size. A final grinding is performed in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A high-molecular-weight non-dissolving solvent, a mixture of isopropanol and ethylene glycol in a weight ratio of 8:2, is added to the prepared polymer powder to prepare a stable, fine dispersion with a polymer content of 80±5 wt%, which reduces the flow resistance of oil and oil products in pipelines.

[0038] Example 3

[0039] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 84 wt% of 1-hexene, 5 wt% of 1-tetradecene, 5.91 wt% of dodecane with a purity of not less than 99.8 wt%, and 5.00 wt% of cyclooctane with a purity of not less than 99.8 wt% were charged, and nitrogen gas with a purity of 99.9 wt% was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C in a nitrogen gas stream by stirring with a stirrer and supplying coolant to the reactor's isolation hood. Then, a catalyst activator was fed into the reactor in the form of a 1:1 mass ratio mixture of diethylaluminum chloride and triisobutylaluminum, at a dosage of 0.077 wt% (0.0385 wt% each), and titanium trichloride was added as a catalyst at a dosage of 0.013 wt%, in a suspension at a concentration of 40 wt% in heptane. The material in the stirred reactor was maintained at a temperature between +8 and +12°C for 1 hour. Next, the reactants were discharged under a nitrogen stream into a sealed, airtight container lined with polyethylene, ensuring the material layer height did not exceed 250 mm, or similarly sized polymer containers were sealed and kept at 15±5°C without air contact for at least 15 days. The resulting polymer blocks were then pulverized using a series of blades into particles of 50±40 mm, 3±2 mm, and 0.8±0.7 mm in size. A final grinding was performed in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A stable, fine dispersion with a polymer content of 80±5 wt% was prepared by adding a high-molecular-weight non-dissolving solvent consisting of a mixture of butyl cellosolve and ethylene glycol in a 6:4 weight ratio to the prepared polymer powder.

[0040] Example 4

[0041] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 80 wt% of 1-hexene, 5 wt% of n-decene, 14.81 wt% of decahydronaphthalene with a purity of not less than 99.8 wt%, and 0.1 wt% of cyclooctadecylcyclooctadecane with a purity of not less than 99.8 wt% were charged, and nitrogen gas of 99.9 wt% purity was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C by stirring with a stirrer and supplying coolant to the reactor's isolation hood. The catalyst activator was then fed into the reactor as a mixture of diethylaluminum chloride and triisobutylaluminum in a mass ratio of 10:1, at a dosage of 0.077 wt% (0.07 wt% and 0.007 wt%, respectively). The catalyst was titanium trichloride, at a dosage of 0.013 wt%, in a 40 wt% suspension in heptane. The material in the reactor was stirred, and the temperature was maintained in the range of +8 to +12 °C for 1 hour. Next, the reactants were discharged under a nitrogen stream into a sealed, airtight container with a polyethylene liner, ensuring that the material layer height did not exceed 250 mm, or a similarly sized polymer container was sealed and kept at 15 ± 5 °C without air contact for at least 15 days. Subsequently, the resulting polymer lumps were pulverized into particles of 50 ± 40 mm, 3 ± 2 mm, and 0.8 ± 0.7 mm in size using a series of blades. A final grinding was carried out in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A stable, finely dispersed polymer with a content of 80±5wt% was prepared by adding a mixture of ethyl cellosolve and propylene glycol in a weight ratio of 6:4 to the prepared polymer powder to reduce the flow resistance of oil and oil products in pipelines.

[0042] Example 5

[0043] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 80 wt% of 1-hexene, 5 wt% of n-decene, 12.91 wt% of decahydronaphthalene with a purity of not less than 99.8 wt%, and 2.00 wt% of cyclooctadecane with a purity of not less than 99.7 wt% were charged, and nitrogen gas with a purity of 99.9 wt% was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C by stirring with a stirrer and supplying coolant to the reactor's isolation hood. Then, the catalyst activator was fed into the reactor in the form of a mixture of diethylaluminum chloride and triisobutylaluminum in a mass ratio of 1:10, at a dosage of 0.077 wt% (0.07 wt% and 0.007 wt%, respectively). The catalyst was titanium trichloride, at a dosage of 0.013 wt%, in a suspension with a concentration of 40 wt% in heptane. The material in the reactor was stirred, and the temperature was maintained in the range of +8 to +12 °C for 1 hour. Next, the reactants were discharged under a nitrogen stream into a sealed, airtight container with a polyethylene liner, ensuring that the material layer height did not exceed 250 mm, or a similarly sized polymer container was sealed and kept at a temperature of 15 ± 5 °C without air contact for at least 15 days. Subsequently, the resulting polymer block was pulverized into particles with sizes of 50 ± 40 mm, 3 ± 2 mm, and 0.8 ± 0.7 mm using a series of blades. The final grinding was carried out in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A polymeric non-dissolving solvent composed of a mixture of octanol and ethylene glycol in a weight ratio of 8:2 was added to the prepared polymer powder to prepare a stable, fine dispersion of 80 ± 5 wt% polymer, which reduces the flow resistance of oil and petroleum products in pipelines.

[0044] Example 6

[0045] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 80 wt% 1-octene, 15 wt% 1-hexene, 2.91 wt% decane with a purity of not less than 99.8 wt%, and 2.00 wt% tetradecylcyclohexadecane with a purity of not less than 99.8 wt% were charged, and nitrogen gas with a purity of 99.9 wt% was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C by stirring with a stirrer and supplying coolant to the reactor's isolation hood. Then, a catalyst activator was fed into the reactor in a 1:1 mass ratio of diethylaluminum chloride and triisobutylaluminum, at a dosage of 0.077 wt% (0.0385 wt% each), and titanium trichloride was added as a catalyst at a dosage of 0.013 wt%, in a 40 wt% suspension in heptane. The material in the stirred reactor was maintained at a temperature between +8 and +12°C for 1 hour. Next, the reactants were discharged in a nitrogen stream into a sealed, airtight container with a polyethylene liner, ensuring the material layer height did not exceed 250 mm, or discharged into a similar polymer container, sealed, and kept at 15 ± 5°C without air contact for at least 15 days. The resulting polymer lumps were then pulverized using a series of blades into particles of 50 ± 40 mm, 3 ± 2 mm, and 0.8 ± 0.7 mm in size. A final grinding was performed in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A high-molecular-weight non-dissolving solvent, consisting of a mixture of butane phosphate and ethylene glycol in a 4:6 weight ratio, was added to the prepared polymer powder to prepare a stable, fine dispersion with a polymer content of 80 ± 5 wt%, which reduces the flow resistance of oil and oil products in pipelines.

[0046] Example 7

[0047] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 70 wt% of 1-hexene, 5 wt% of 1-dodecene e-1,2-13C2, 19.908 wt% of n-hexadecane with a purity of not less than 99.8 wt%, and 5.00 wt% of cyclooctane with a purity of not less than 99.8 wt% were charged, and nitrogen gas with a purity of 99.9 wt% was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C by stirring with a stirrer and supplying coolant to the reactor's isolation hood. The catalyst activator was then fed into the reactor as a 1:1 mixture of diethylaluminum chloride and triisobutylaluminum chloride at a dosage of 0.077 wt% (0.0385 wt% each), and the catalyst was titanium trichloride at a dosage of 0.015 wt%, in a 40 wt% suspension in heptane. The material in the reactor was stirred, and the temperature was maintained in the range of +8 to +12 °C for 1 hour. Next, the reactants were discharged in a nitrogen stream into a sealed, airtight container with a polyethylene liner, ensuring that the material layer height did not exceed 250 mm, or discharged into a similar polymer container, sealed, and kept at a temperature of 15 ± 5 °C without air contact for at least 15 days. Subsequently, the resulting polymer lumps were pulverized into particles of 50 ± 40 mm, 3 ± 2 mm, and 0.8 ± 0.7 mm in size using a series of blades. A final grinding was carried out in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A polymeric non-dissolving solvent consisting of a mixture of n-butanol and ethylene glycol in a weight ratio of 8:2 was added to the prepared polymer powder to prepare a stable fine dispersion with a polymer content of 80±5wt% to reduce the flow resistance of oil and oil products in pipelines.

[0048] Example 8

[0049] The polymer was prepared according to the following steps of RU2648079C1. In a reactor equipped with a jacket, stirrer, thermocouple, and pressure gauge, 90 wt% of 1-dodecene e-1,2-13C2, 5 wt% of n-decene, 2.92 wt% of decane with a purity of not less than 99.8 wt%, and 2.00 wt% of cyclohexadecane with a purity of not less than 99.8 wt% were charged, and nitrogen gas of 99.9 wt% purity was supplied. The mixture in the reactor was cooled to a temperature of +10 ± 2 °C by stirring with a stirrer and supplying coolant to the reactor's isolation hood. The catalyst activator was then fed into the reactor as a 1:1 mixture of diethylaluminum chloride and triisobutylaluminum chloride at a dosage of 0.077 wt% (0.0385 wt% each), and the catalyst was titanium trichloride at a dosage of 0.013 wt%, in a 40 wt% suspension in heptane. The material in the reactor was stirred, and the temperature was maintained in the range of +8 to +12 °C for 1 hour. Next, the reactants were discharged in a nitrogen stream into a sealed, airtight container with a polyethylene liner, ensuring that the material layer height did not exceed 250 mm, or discharged into a similar polymer container, sealed, and kept at a temperature of 15 ± 5 °C without air contact for at least 15 days. Subsequently, the resulting polymer lumps were pulverized into particles of 50 ± 40 mm, 3 ± 2 mm, and 0.8 ± 0.7 mm in size using a series of blades. A final grinding was carried out in a medium composed of liquid nitrogen and 15 wt% calcium stearate. A polymeric non-dissolving solvent consisting of a mixture of 1-hexanol and propylene glycol in a weight ratio of 5:5 was added to the prepared polymer powder to prepare a stable fine dispersion with a polymer content of 80±5wt% to reduce the flow resistance of oil and oil products in pipelines.

[0050] The method of injecting drag-reducing agents containing a large amount of active base into hydrocarbon fluids transported through pipelines is carried out according to the following main steps.

[0051] The reagent (DRA) prepared according to the above method is fed into a mixing hopper 101, which is equipped with a stirrer and a loading unit in a screw feeder 102. The reagent (DRA) in the mixing hopper 101 is then fed into the screw feeder 102 to ensure that the reagent is delivered to the preparation tank 103, where the prepared reagent is dissolved. A device (cyclone mixer 104) and a check valve 105 are located before the preparation tank 103 for hydrocyclone mixing of the reagent with a hydrocarbon fluid. While passing through the cyclone mixer 104, the reagent is mixed with the hydrocarbon fluid supplied from the pipeline 106 via valve 107, inlet flow meter 108, and pressure reducing valve 109. The reagent is then dissolved in the preparation tank 103 until homogeneous. The prepared slurry is supplied from the preparation tank 103 to the pipeline via a supply flow meter 110 using an in-line gear pump 111. To prevent hydrocarbon fluids from flowing back into the preparation tank 103 during pump shutdown or maintenance, a reflux valve 112 and a valve 113 are installed on the supply line. The dosage of the reagent is adjusted by rotating the screw feeder 102 and controlled by the mass difference of the liquid flowing through the inlet flow meter 108 and the supply flow meter 110.

[0052] The above dosing regimen is described in [link to dosing regimen]. Figure 1 ( Figure 1 ).

[0053] The efficiency of the product preparation was evaluated on a laboratory turbine flow meter (see table). The drag reduction (DR) of this reagent on petroleum solvent flowing in a capillary was calculated using the following formula:

[0054]

[0055] in:

[0056] λ is the fluid resistance coefficient;

[0057] t is the time it takes for 330 cubic centimeters of petroleum solvent to flow through the capillary tube;

[0058] o and p are indicators related to pure solvent and reagent solution, respectively.

[0059] The product passes the test if the DR value is at least 30% when the reagent concentration of 2.5 ppm petroleum solvent is used for preparation.

[0060] surface

[0061]

[0062] From the above embodiments and tables, it can be concluded that, compared with the closest analogues, the claimed method makes it possible to prepare a reagent that is most effective in reducing the flow resistance of liquid hydrocarbons in pipelines, and as a result, ensures the speed of transporting hydrocarbon fluids and reduces costs.

Claims

1. A method for the preparation of a powder agent for reducing the flow resistance of liquid hydrocarbons in a pipeline, characterized in that The powder reagent is capable of being injected in solid powder form into a liquid hydrocarbon by a screw feeder and comprises at least 75 wt% of a polymer having a molecular weight of 1-2-10 7 amu; the method comprising: 7 amu; the method comprising: A poly-alpha-olefin powder that reduces the flow resistance of liquid hydrocarbons is mixed with a high molecular non-solvent and a separating agent, wherein the high molecular non-solvent is a mixture of a monofunctional heteroatomic organic compound having a carbon number of 3 to 16 and a difunctional heteroatomic organic compound having a carbon number of 3 to 16, in mass percentages of: Poly-alpha-olefin powder: 75 to 90; Separating agent: 2 to 15; Monofunctional heteroatomic organic compound having a carbon number of 3 to 16: 1 to 10; Difunctional heteroatomic organic compound having a carbon number of 3 to 16: 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, isomers of hexadecanol, tripropylamine, tributylamine, tripentylamine, trihexylamine, triheptylamine, trioctylamine, trinonylamine, tridecylamine, triundecylamine, tridodecylamine, tritridecylamine, tritetradecylamine, tripentadecylamine, trihexadecylamine; the difunctional heteroatomic organic compound is at least one of propylene glycol, butylene glycol, hexylene glycol, diethylene glycol.

2. A powder agent for reducing the flow resistance of a liquid hydrocarbon in a pipeline, characterized in that, The powder reagent comprises at least 75 wt% of a polymer having a molecular weight of 1 · 10 7 ~ 2 · 10 7 amu, and comprises the following components in mass percentage: Poly-alpha-olefin powder: 75 to 90; Separating agent: 2 to 15; Monofunctional heteroatomic organic compound having a carbon number of 3 to 16: 1 to 10; Difunctional heteroatomic organic compound having a carbon number of 3 to 16: 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, isomers of hexadecanol, tripropylamine, tributylamine, tripentylamine, trihexylamine, triheptylamine, trioctylamine, trinonylamine, tridecylamine, triundecylamine, tridodecylamine, tritridecylamine, tritetradecylamine, tripentadecylamine, trihexadecylamine; the difunctional heteroatomic organic compound is at least one of propylene glycol, butylene glycol, hexylene glycol, diethylene glycol.

3. The powder reagent for reducing the flow resistance of a liquid hydrocarbon in a pipeline according to claim 2, wherein wherein the monofunctional heteroatomic organic compound is butanol, pentanol, hexanol, heptanol, octanol, nonanol, decanol, undecanol, dodecanol, tridecanol, tetradecanol, pentadecanol, isomers of hexadecanol.

4. A method of reducing the flow resistance of a liquid hydrocarbon in a pipeline, characterized by, Injecting the powder reagent of claim 2 into a hydrocarbon fluid stream being transported through a pipeline, wherein the injection of the reagent is performed by means of an injection device for the polymer powder.

5. The method of reducing the flow resistance of a liquid hydrocarbon in a pipeline of claim 4, wherein, wherein the reagent is dissolved in the hydrocarbon fluid into a slurry state before being injected into the pipeline.

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