Industrial discharging and dispersing process after polymerization reaction of high-molecular thick oil viscosity reducer

Abstract

The invention discloses an industrial emptying and dispersing process after polymerization reaction of a high-molecular thick oil viscosity reducer, which comprises the following steps: (1) after the polymerization reaction of the high-molecular thick oil viscosity reducer is finished, obtaining a high-molecular thick oil viscosity reducer solution, and continuously introducing inert gas or nitrogen into a reactor for protection, adding a proper amount of polymerization reaction solvent into the high-molecular thick oil viscosity reducer solution again; (2) slowly adding the diluted polymer type thick oil viscosity reducer solution into a dispersing sieve plate, wherein the screened polymer type thick oil viscosity reducer forms a water drop shape under the condition of free falling and falls into a dispersing tank filled with a dispersing agent; (3) discharging a mixed solution of the polymerization reaction solvent and the dispersing agent through a screen at the bottom of the dispersing tank after discharging and dispersing; and (4) pumping the precipitated small particles of the high-molecular thick oil viscosity reducer into a washing instrument, and washing for multiple times.

Description

Technical Field

[0001] The invention relates to an industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer, and belongs to the technical field of polymer materials. Background Art

[0002] Chinese invention patent application CN104213870A discloses a method for producing artificial foamed oil in a water-driven heavy oil reservoir. The production method comprises the following steps: step 1: deploying an injection-production well network; step 2: injecting a gelling agent into the injection well; step 3: injecting a highly oil-resistant foaming agent into the injection well; step 4: injecting a water-in-oil emulsified viscosity reducer solution into the injection well; wherein step 3 and step 4 are repeated alternately, and during the injection process, the production well continuously produces, and the water-driven heavy oil reservoir is a water-driven development well group with an average water content greater than 90% and a water content greater than 98% in at least one production well. Chinese invention patent application CN109025894A discloses a method for plugging steam channeling in a heavy oil thermal recovery horizontal well, comprising the following steps: (1) lowering a steam injection pipe string into the oil layer, and injecting steam to preheat the formation in a general injection manner; (2) injecting high-viscosity gel; (3) injecting a silicate high-temperature plugging agent; (4) repeating steps (2) and (3) until the injection pressure requirement of the construction design is reached; (5) injecting steam to heat the plugging agent, and shutting down the well for 3 to 5 days; and (6) injecting steam for huff-and-puff production.

[0003] However, the above-mentioned mining methods have the following shortcomings: Due to the large oil-water mobility ratio, the development effect of water-driven heavy oil is generally poor. The recovery rate of Shengli water-driven heavy oil is less than 20%. After multiple rounds of steam injection of thermal heavy oil, the periodic oil production and oil-steam ratio are getting lower and lower due to the influence of water invasion, steam channeling and the limit injection radius; at the same time, due to the influence of steam injection cost, energy consumption and environmental pressure, the cost of thermal recovery has doubled and the benefit has become worse and worse. The recovery rate of Shengli thermal heavy oil is about 20.8%.

[0004] Based on this, technicians in this industry have turned their attention to polymer heavy oil cold recovery. Polymer heavy oil cold recovery is a tertiary oil recovery method that uses polymer solution as an oil displacement agent. It can effectively improve the sweep coefficient and thus improve the crude oil recovery rate. It is an important means to stabilize and increase oil production in the current stage of oil fields. For example, Chinese invention patent application CN 108729893A discloses a foam composite cold recovery method for improving the recovery rate of heavy oil reservoirs. The method mainly includes: alternately injecting a heavy oil viscosity reduction oil displacement agent, water, and a polymer composite foam oil displacement system into a water injection well, and then performing water flooding; the present invention can effectively improve the recovery rate of heavy oil under non-heating conditions, and the recovery rate can be increased by more than 15%.

[0005] Active polymers are the core agents of polymer flooding, and the quality of their properties largely determines the effect of polymer flooding. Ultra-high molecular weight heavy oil viscosity reducers are a type of active polymer, which can increase the viscosity of the ternary system, reduce the permeability of high permeability oil layers, increase the water absorption thickness, and improve the water absorption capacity of medium and low permeability layers, which is conducive to significantly improving crude oil recovery. Compared with low molecular weight heavy oil viscosity reducers, high molecular weight heavy oil viscosity reducers have the advantages of high viscosity and large residual resistance coefficient. The large residual resistance coefficient can increase the recovery rate. Therefore, the application of ultra-high molecular weight heavy oil viscosity reducers will greatly improve the economic effect of tertiary oil recovery technology. The application of ultra-high molecular weight heavy oil viscosity reducers can reduce the dosage by more than 2 / 5 compared with low molecular weight agents, greatly reducing the cost of tertiary recovery, and further improving the recovery rate. Therefore, increasing the molecular weight of polyacrylamide has become the main topic of various manufacturers and research institutions.

[0006] The polymer type heavy oil viscosity reducer is generally an acrylamide copolymer. Through industrial production and amplification, an industrial product is obtained, with a molecular weight of more than 22 million and a filtration factor of less than 1.5. At present, the production process of the polymer type heavy oil viscosity reducer adopts a solution polymerization synthesis method to carry out a one-step nucleophilic substitution reaction, which is mainly divided into polymerization process and post-treatment process.

[0007] The polymerization process of high molecular weight heavy oil viscosity reducer includes: a) Copolymerization process: acrylamide and acrylic acid are copolymerized. Due to the difference in polymerization rate and the degree of influence of pH value, different molecular weights and their distributions can be obtained by accurately controlling the pH value of the system. Among them, the purity of acrylic acid is the main factor determining the molecular weight of the product. b) Homopolymerization and co-hydrolysis process: acrylamide monomer is polymerized with alkali and then hydrolyzed to form a partially hydrolyzed polyacrylamide product. Since the alkali is added to the aqueous solution of acrylamide monomer, the mixture is evenly mixed and the degree of hydrolysis of the product is uniform. However, existing studies have shown that this process requires slightly more factors to be controlled in order to increase the molecular weight of the product. c) Homopolymerization and post-hydrolysis process: acrylamide monomer is first homopolymerized and then hydrolyzed with alkali. This process requires relatively fewer factors to be controlled in order to increase the molecular weight of the product, but there are problems of uneven mixing and uneven degree of hydrolysis of the product.

[0008] After the polymerization reaction is completed, the polymer is first dispersed. The dispersion process is mainly as follows: inject the polymerized viscous liquid into the dispersant, and then separate the polymer-type heavy oil viscosity reducer from the solution. The separated polymer-type heavy oil viscosity reducer is subjected to post-processing processes such as crushing, washing, drying, granulation and packaging. Among them, the separation and washing of the polymer-type heavy oil viscosity reducer from the polymer solution is particularly important. The polymer solution after the polymerization contains unreacted inorganic salts of sodium carbonate or sodium bicarbonate, potassium carbonate or potassium bicarbonate, as well as the by-products of the reaction, sodium chloride or potassium chloride, unreacted monomer raw materials, coloring metal ions brought by the system and materials, and other mechanical impurities. They must be removed to obtain high-quality polymer-type heavy oil viscosity reducer.

[0009] The existing dispersion technology mostly adopts the water precipitation high-speed crushing method. This method is to inject the polymerized viscous liquid into water after the polymerization reaction is completed, and use a high-speed crusher to crush the polymer of the high-molecular-weight heavy oil viscosity reducer into microparticles, precipitate the inorganic salt particles wrapped in the polymer, release the polymerization solvent into the dispersant and dissolve it into one, and then remove the solvent recovery system after filtering and separation. However, this method has the following shortcomings: 1. The shape and structure of the obtained high-molecular-weight heavy oil viscosity reducer active polymer are irregular, which increases the difficulty of the subsequent washing process; 2. The washing solvent consumption is large and the pollution emission is large; 3. The polymerization solvent and inorganic salt residues are high, the transparency is reduced, and the product color is dark and the purity is low. Summary of the invention

[0010] Purpose of the invention: In view of the shortcomings of the above-mentioned prior art, the present invention provides an industrialized material discharge and dispersion process after the polymerization reaction of a polymer-type heavy oil viscosity reducer, which solves the problems of the prior art such as high difficulty in washing process, large consumption of washing solvent, large pollution emissions, high residues of polymerization solvent and inorganic salts, reduced transparency, dark product color and low purity.

[0011] Technical solution: An industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer, comprising the following steps:

[0012] (1) After the polymerization reaction of the polymeric heavy oil viscosity reducer is completed, a polymeric heavy oil viscosity reducer solution is obtained, and an inert gas or nitrogen is continuously introduced into the reactor for protection, and at the same time, an appropriate amount of polymerization reaction solvent is again added to the polymeric heavy oil viscosity reducer solution;

[0013] (2) slowly adding the diluted high molecular weight heavy oil viscosity reducer solution into the dispersion screen plate, and the high molecular weight heavy oil viscosity reducer after screening forms a water drop shape under free fall and falls into the dispersion tank filled with the dispersant;

[0014] (3) After the material is discharged and dispersed, the mixed solution of the polymerization solvent and the dispersant is discharged through the screen at the bottom of the dispersion tank;

[0015] (4) The precipitated small particles of high molecular weight heavy oil viscosity reducer are pumped into a washing instrument for multiple washings.

[0016] Furthermore, the polymer type heavy oil viscosity reducer is selected from one of anionic acrylamide copolymer and nonionic acrylamide copolymer.

[0017] Furthermore, the functional monomer of the anionic acrylamide copolymer is at least one of acrylic acid, p-styrene sulfonate, 2-acrylamide-2-methylpropane sulfonic acid, and allyl sulfonic acid.

[0018] Furthermore, the functional monomer of the nonionic acrylamide copolymer is at least one of N-vinyl pyrrolidone and vinyl polyether.

[0019] Furthermore, the polymerization reaction solvent in step (1) is selected from one of methanol, ethanol, isopropanol, tetrahydrofuran and dimethylformamide.

[0020] Furthermore, the mass of the polymerization solvent added again after the polymerization reaction in step (1) is 10%-50% of the mass of the polymerization solvent added before the polymerization reaction, preferably 20%-30%.

[0021] Furthermore, in step (1), during the process of adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 70-200°C, preferably 80-180°C.

[0022] Furthermore, the water content of the polymerization reaction solvent in step (1) is ≤0.5%.

[0023] Furthermore, the sieve hole diameter of the dispersion sieve plate in step (2) is 2-10 mm, preferably 5-8 mm.

[0024] Furthermore, the porosity of the dispersion screen plate in step (2) is 8%-20%, preferably 10%-15%.

[0025] Furthermore, the free fall height of the dispersion screen plate in step (2) from the dispersant liquid level in the dispersion tank is 0.5-2.5 m, preferably 1-2 m.

[0026] Furthermore, the dispersant in step (2) is one of deionized water, ethanol and methanol, preferably deionized water. During the dispersion process, the temperature of the dispersant is controlled at 15-55°C.

[0027] Furthermore, a stirrer is installed in the dispersion tank, and during the entire dispersion process of step (2), the stirrer is kept in working state to stir the dispersant.

[0028] The positive effects of the present invention are:

[0029] The problem that the high-temperature viscous polymer is irregularly dispersed in the existing production process of the high-molecular-weight heavy oil viscosity reducer, resulting in uneven washing and low product qualification rate, is solved. The product quality and washing efficiency of the high-molecular-weight heavy oil viscosity reducer produced by the present invention are effectively improved, the solvent recovery rate is high, the operation is simple, the cost is low, and the pollution is small.

[0030] The invention discloses a process for industrialized material discharge and dispersion after polymerization of a polymeric heavy oil viscosity reducer. The process is as follows: after the polymerization of the polymeric heavy oil viscosity reducer is completed, a polymerization solvent identical to the polymerization solvent is added, and the reaction temperature is lowered by precisely controlling the amount of the polymerization solvent added, thereby further terminating the polymerization reaction and reducing the viscosity of the reaction liquid. Inert gas or nitrogen is filled in the entire reaction process for anti-oxidation protection.

[0031] After the reaction, the active polymer of the high molecular weight heavy oil viscosity reducer forms a water drop shape under free fall, and is stirred and dispersed in contact with the dispersant;

[0032] The mixed solution of the dispersant and the polymerization reaction solvent is discharged through the screen at the bottom of the dispersion tank;

[0033] The small particles of high molecular weight heavy oil viscosity reducer precipitated after dispersion are sent to the washing process for washing.

[0034] This process can greatly reduce the residual polymerization solvent and inorganic salt, increase the transparency and color of the product, and greatly improve the qualified rate of the product. After adopting this method, the residual polymerization solvent and inorganic salt of the polymer type heavy oil viscosity reducer polymerization reaction industrial amplification can be reduced by more than 8%, and the qualified rate of the polymer type heavy oil viscosity reducer product can be increased by more than 5%.

[0035] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0036] (1) The polymerization reaction of the polymer-type heavy oil viscosity reducer of the present invention fully optimizes the reaction solvent and reactant concentrations, realizes accurate feeding, and the entire reaction occurs under the protection of an inert gas, fully ensuring the completeness of the reaction and the purity of the product;

[0037] (2) This reaction proposes a new industrial scale-up method for the polymerization reaction of polymer-type heavy oil viscosity reducers, which fully optimizes the processing flow. The paste-like polymer-type heavy oil viscosity reducer after the reaction forms water droplets through free fall, which increases the contact area with the dispersant and is fully dispersed, greatly reducing the polymerization solvent and inorganic salt residues, and increasing the transparency and color of the product.

[0038] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 The present invention discloses a flow chart of an industrialized material discharging and dispersing process after the polymerization reaction of a high-molecular-weight heavy oil viscosity reducer. DETAILED DESCRIPTION

[0040] The specific embodiments of the present invention are described in detail below.

[0041] The endpoint values ​​and any values ​​of the range disclosed in the present invention are not limited to the precise range or value, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be regarded as specifically disclosed in this article.

[0042] Example 1

[0043] An industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer comprises the following steps:

[0044] (1) After the polymerization reaction of the polymeric heavy oil viscosity reducer is completed in the polymerization reactor, a polymeric heavy oil viscosity reducer solution is obtained, nitrogen is continuously introduced into the polymerization reactor for protection, and an appropriate amount of polymerization reaction solvent is again added to the polymeric heavy oil viscosity reducer solution;

[0045] (2) slowly adding the diluted high molecular weight heavy oil viscosity reducer solution into the dispersion screen plate, and the high molecular weight heavy oil viscosity reducer after screening forms a water drop shape under free fall and falls into the dispersion tank filled with the dispersant;

[0046] (3) After the material is discharged and dispersed, the mixed solution of the polymerization solvent and the dispersant is discharged through the screen at the bottom of the dispersion tank;

[0047] (4) The precipitated small particles of high molecular weight heavy oil viscosity reducer are pumped into a washing instrument for eight washings.

[0048] Furthermore, the polymer type heavy oil viscosity reducer is selected from anionic acrylamide copolymer.

[0049] Furthermore, the functional monomer of the anionic acrylamide copolymer is acrylic acid. In another embodiment, the functional monomer of the anionic acrylamide copolymer is acrylic acid, p-styrene sulfonate, 2-acrylamide-2-methylpropane sulfonic acid, and allyl sulfonic acid in equal mass ratios. In another embodiment, the functional monomer of the anionic acrylamide copolymer is p-styrene sulfonate. In another embodiment, the functional monomer of the anionic acrylamide copolymer is 2-acrylamide-2-methylpropane sulfonic acid. In another embodiment, the functional monomer of the anionic acrylamide copolymer is allyl sulfonic acid.

[0050] Further, the polymerization reaction solvent described in step (1) is isopropanol. In another embodiment, the polymerization reaction solvent described in step (1) is methanol. In another embodiment, the polymerization reaction solvent described in step (1) is ethanol. In another embodiment, the polymerization reaction solvent described in step (1) is tetrahydrofuran. In another embodiment, the polymerization reaction solvent described in step (1) is dimethylformamide.

[0051] Further, the mass of the polymerization solvent added again after the polymerization reaction in step (1) is 10% of the mass of the polymerization solvent added before the polymerization reaction. In another embodiment, the mass of the polymerization solvent added again after the polymerization reaction in step (1) is 20% of the mass of the polymerization solvent added before the polymerization reaction.

[0052] Furthermore, in step (1), during the process of adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 70° C. In another embodiment, in step (1), during the process of adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 80° C.

[0053] Furthermore, the water content of the polymerization reaction solvent in step (1) is ≤0.5%.

[0054] Furthermore, the mesh diameter of the dispersion screen plate described in step (2) is 2 mm. In another embodiment, the mesh diameter of the dispersion screen plate described in step (2) is 5 mm.

[0055] Furthermore, the porosity of the dispersion screen plate in step (2) is 8%. In another embodiment, the porosity of the dispersion screen plate in step (2) is 10%.

[0056] Furthermore, the free fall height of the dispersing screen plate in step (2) from the dispersant liquid level in the dispersing tank is 0.5 m. In another embodiment, the free fall height of the dispersing screen plate in step (2) from the dispersant liquid level in the dispersing tank is 1 m.

[0057] Furthermore, the dispersant in step (2) is deionized water, and during the dispersion process, the temperature of the dispersant is controlled at 15°C.

[0058] Furthermore, a stirrer is installed in the dispersion tank, and during the entire dispersion process of step (2), the stirrer is kept in working state to stir the dispersant.

[0059] After crushing, washing and drying, the residual amount of isopropanol in the polymer is 0.0012%, and the number of water washing times is reduced from 10 times to 8 times, which improves the product quality and washing efficiency and reduces the amount of washing water.

[0060] Example 2

[0061] An industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer comprises the following steps:

[0062] (1) After the polymerization reaction of the polymeric heavy oil viscosity reducer is completed in the polymerization reactor, a polymeric heavy oil viscosity reducer solution is obtained, helium is continuously introduced into the polymerization reactor for protection, and an appropriate amount of polymerization reaction solvent is again added to the polymeric heavy oil viscosity reducer solution;

[0063] (2) slowly adding the diluted high molecular weight heavy oil viscosity reducer solution into the dispersion screen plate, and the high molecular weight heavy oil viscosity reducer after screening forms a water drop shape under free fall and falls into the dispersion tank filled with the dispersant;

[0064] (3) After the material is discharged and dispersed, the mixed solution of the polymerization solvent and the dispersant is discharged through the screen at the bottom of the dispersion tank;

[0065] (4) The precipitated small particles of high molecular weight heavy oil viscosity reducer are pumped into a washing instrument for eight washings.

[0066] Furthermore, the polymer type heavy oil viscosity reducer is a non-ionic acrylamide copolymer.

[0067] Furthermore, the functional monomer of the nonionic acrylamide copolymer is N-vinyl pyrrolidone. In another embodiment, the functional monomer of the nonionic acrylamide copolymer is N-vinyl pyrrolidone and vinyl polyether in an equal mass ratio. In another embodiment, the functional monomer of the nonionic acrylamide copolymer is vinyl polyether.

[0068] Furthermore, the polymerization reaction solvent in step (1) is tetrahydrofuran.

[0069] Further, the mass of the polymerization solvent added again after the polymerization reaction in step (1) is 50% of the mass of the polymerization solvent added before the polymerization reaction. In another embodiment, the mass of the polymerization solvent added again after the polymerization reaction in step (1) is 30% of the mass of the polymerization solvent added before the polymerization reaction.

[0070] Furthermore, in step (1), during the process of adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 200° C. In another embodiment, in step (1), during the process of adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 180° C.

[0071] Furthermore, the water content of the polymerization reaction solvent in step (1) is ≤0.5%.

[0072] Furthermore, the mesh diameter of the dispersion screen plate described in step (2) is 10 mm. In another embodiment, the mesh diameter of the dispersion screen plate described in step (2) is 8 mm.

[0073] Furthermore, the porosity of the dispersion screen plate in step (2) is 20%. In another embodiment, the porosity of the dispersion screen plate in step (2) is 15%.

[0074] Furthermore, the free fall height of the dispersion screen plate in step (2) from the dispersant liquid level in the dispersion tank is 2.5 m. In another embodiment, the free fall height of the dispersion screen plate in step (2) from the dispersant liquid level in the dispersion tank is 2 m.

[0075] Furthermore, the dispersant in step (2) is ethanol, and during the dispersion process, the temperature of the dispersant is controlled at 55°C.

[0076] Furthermore, a stirrer is installed in the dispersion tank, and during the entire dispersion process of step (2), the stirrer is kept in working state to stir the dispersant.

[0077] After crushing, washing and drying, the residual tetrahydrofuran in the active polymer is 0.0008%, and the number of water washing times is reduced from 10 times to 8 times, which improves the product quality and washing efficiency and reduces the amount of washing water.

[0078] Example 3

[0079] An industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer comprises the following steps:

[0080] (1) After the polymerization reaction of the polymeric heavy oil viscosity reducer is completed, a polymeric heavy oil viscosity reducer solution is obtained in the polymerization reactor, neon gas is continuously introduced into the polymerization reactor for protection, and at the same time, an appropriate amount of polymerization reaction solvent is again added to the polymeric heavy oil viscosity reducer solution;

[0081] (2) slowly adding the diluted high molecular weight heavy oil viscosity reducer solution into the dispersion screen plate, and the high molecular weight heavy oil viscosity reducer after screening forms a water drop shape under free fall and falls into the dispersion tank filled with the dispersant;

[0082] (3) After the material is discharged and dispersed, the mixed solution of the polymerization solvent and the dispersant is discharged through the screen at the bottom of the dispersion tank;

[0083] (4) The precipitated small particles of high molecular weight heavy oil viscosity reducer are pumped into a washing instrument for eight washings.

[0084] Furthermore, the polymer type heavy oil viscosity reducer is selected from anionic acrylamide copolymer.

[0085] Furthermore, the functional monomers of the anionic acrylamide copolymer are acrylic acid and p-styrene sulfonate in equal weight ratios.

[0086] Furthermore, the polymerization reaction solvent in step (1) is dimethylformamide.

[0087] Furthermore, the mass of the polymerization solvent added again after the polymerization reaction in step (1) is 25% of the mass of the polymerization solvent added before the polymerization reaction.

[0088] Furthermore, in step (1), during the process of adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 100°C.

[0089] Furthermore, the water content of the polymerization reaction solvent in step (1) is ≤0.5%.

[0090] Furthermore, the sieve hole diameter of the dispersion sieve plate described in step (2) is 6 mm.

[0091] Furthermore, the opening rate of the dispersion screen plate in step (2) is 12%

[0092] Furthermore, the free fall height of the dispersion screen plate described in step (2) from the dispersant liquid level in the dispersion tank is 1.5 m.

[0093] Furthermore, the dispersant in step (2) is methanol, and during the dispersion process, the temperature of the dispersant is controlled at 30°C.

[0094] Furthermore, a stirrer is installed in the dispersion tank, and during the entire dispersion process of step (2), the stirrer is kept in working state to stir the dispersant.

[0095] After crushing, washing and drying, the residual amount of dimethylformamide in the polymer is 0.0015%, and the number of water washing times is reduced from 10 times to 8 times, which improves the product quality and washing efficiency and reduces the amount of washing water.

[0096] The above examples prove that the dispersed particles of the polymer type heavy oil viscosity reducer with uniform particles obtained by the present invention, after being washed by a subsequent pulverizer, can effectively improve the product quality and washing efficiency of the polymer type heavy oil viscosity reducer, with a high solvent recovery rate, simple operation, low cost and less pollution.

[0097] The above describes the embodiments of the present invention in detail. However, the present invention is not limited to the above embodiments, and various changes can be made within the knowledge of ordinary technicians in the relevant technical field without departing from the purpose of the present invention.

Claims

1. An industrial dispersing process for polymer-type heavy oil viscosity reducer after polymerization reaction, characterized in that: The following steps are involved: (1) After the polymerization reaction of the polymeric heavy oil viscosity reducer is completed, a polymeric heavy oil viscosity reducer solution is obtained, and an inert gas or nitrogen is continuously introduced into the reactor for protection, and at the same time, an appropriate amount of polymerization reaction solvent is again added to the polymeric heavy oil viscosity reducer solution; (2) slowly adding the diluted high molecular weight heavy oil viscosity reducer solution into the dispersion screen plate, and the high molecular weight heavy oil viscosity reducer after screening forms a water drop shape under free fall and falls into the dispersion tank filled with the dispersant; (3) After the material is discharged and dispersed, the mixed solution of the polymerization solvent and the dispersant is discharged through the screen at the bottom of the dispersion tank; (4) The precipitated small particles of high molecular weight heavy oil viscosity reducer are pumped into a washing instrument for multiple washings.

2. The industrial dispersing process of polymer-type heavy oil viscosity reducer after polymerization reaction as claimed in claim 1, characterized in that: The polymer type heavy oil viscosity reducer is selected from one of anionic acrylamide copolymer and nonionic acrylamide copolymer.

3. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer as claimed in claim 2, characterized in that: The functional monomer of the anionic acrylamide copolymer is at least one of acrylic acid, p-styrene sulfonate, 2-acrylamide-2-methylpropane sulfonic acid and allyl sulfonic acid.

4. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 2, characterized in that: The functional monomer of the nonionic acrylamide copolymer is at least one of N-vinyl pyrrolidone and vinyl polyether.

5. The industrial dispersing process of polymer-type heavy oil viscosity reducer after polymerization reaction as claimed in claim 1, characterized in that: The polymerization reaction solvent described in step (1) is selected from one of methanol, ethanol, isopropanol, tetrahydrofuran and dimethylformamide.

6. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The mass of the polymerization solvent added again after the polymerization reaction in step (1) is 10%-50% of the mass of the polymerization solvent added before the polymerization reaction, preferably 20%-30%.

7. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: In step (1), when adding an appropriate amount of polymerization reaction solvent to the polymeric heavy oil viscosity reducer solution again, the temperature of the material is controlled at 70-200°C, preferably 80-180°C.

8. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The water content of the polymerization reaction solvent in step (1) is ≤0.5%.

9. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The sieve hole diameter of the dispersion sieve plate described in step (2) is 2-10 mm, preferably 5-8 mm.

10. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The opening rate of the dispersion screen plate described in step (2) is 8%-20%, preferably 10%-15%.

11. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The free fall height of the dispersion screen plate described in step (2) from the dispersant liquid level in the dispersion tank is 0.5-2.5m, preferably 1-2m.

12. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The dispersant in step (2) is one of deionized water, ethanol and methanol, preferably deionized water. During the dispersion process, the temperature of the dispersant is controlled at 15-55°C.

13. The industrialized material discharging and dispersing process after the polymerization reaction of a polymer type heavy oil viscosity reducer according to claim 1, characterized in that: The dispersion tank is equipped with a stirrer. During the entire dispersion process of step (2), the stirrer is kept in working state to stir the dispersant.

Images