Method for regulating molecular weight change of electronic-grade acrylic resin

Abstract

The invention provides a method for regulating and controlling molecular weight change of electronic-grade acrylic resin. The method adopts a mixture A for a polymerization reaction process and a mixture D for controlling reaction concentration to realize regulation and control of polymerization reaction, the mixture A comprises a monomer A, an initiator and an organic solvent A; the mixture B comprises a monomer B, an organic solvent B and a water-carrying agent. The method comprises the following specific steps: S1, adding a mixture A into a reactor in an inert gas atmosphere, and heating for polymerization reaction; and S2, adding the mixture B according to a reaction consumption rate, and keeping the inert gas in the reactor to continuously circulate in the polymerization reaction process. By adopting the starvation reactor, on one hand, the reaction concentration is accurately regulated and controlled so as to regulate and control the molecular weight, and on the other hand, the water-carrying agent is utilized to take away heat of a reaction system and hot moisture azeotropic with the water-carrying agent into an inert atmosphere, so that the electronic-grade acrylic resin is prepared.

Description

Technical Field

[0001] The invention relates to the technical field of polymer materials, and in particular to a method for regulating and controlling the molecular weight change of electronic-grade acrylic resin. Background Art

[0002] In the preparation of bottom anti-reflective coating materials, the traditional process requires the addition of monomers and initiators to the solution or emulsion and the polymerization reaction to be carried out for a long time under heating, nitrogen atmosphere and other conditions to achieve the desired molecular weight of acrylic resin. However, in the early stage of this process, due to the long initiator induction time and the inevitable existence of chain growth and chain termination reactions, and the difficulty in controlling the initial reaction, more short-chain polymers may be generated. The polymerization reaction is a random copolymerization. The traditional process will introduce new impurity ions and cannot meet the electronic grade requirements.

[0003] In the prior art, a variety of methods are disclosed to control molecular weight in order to prepare corresponding polymer materials. For example, CN1950401A discloses a method for preparing macromonomers by free radical-initiated aqueous emulsion polymerization of at least one ethylenically unsaturated monomer in a polymerization reactor, and a novel CCTP method using a hydrophobic Co chelate catalyst in an aqueous emulsion to form macromonomers. Thus, when using such a hydrophobic Co catalyst, this method allows the use of a significantly reduced amount of Co catalyst (compared to the amount of Co catalyst required to achieve comparable molecular weight reduction to date) to prepare very low molecular weight macromonomers. Patent CN114044843A discloses that by using a single polymer as a substrate and reacting with various functional alcohols, the molecular weight distribution can be well controlled, and the prepared photoresist resin has a controllable molecular weight and a narrow distribution. Patent CN116323729A discloses a method for manufacturing a carboxyl-containing resin that can control molecular weight and has excellent performance stability between manufacturing batches, and a method for controlling the molecular weight of a carboxyl-containing resin. The control method includes the following steps: controlling the water content of a first liquid containing a reaction product A obtained by reacting an epoxy compound (a) with an unsaturated monobasic acid (b) in an organic solvent to obtain a second liquid containing a reaction product A, adding a polyacid dianhydride (c) and a polyacid monoanhydride (d) to the second liquid containing the reaction product A and reacting to obtain a carboxyl-containing resin. Patent CN106432582A relates to a polymerization method for controlling the molecular weight distribution of acrylates by using the concentration of reactants. By pre-adding part of the monomer and solvent in a reactor, by controlling the concentration of the initiator, the free radical polymerization is carried out smoothly and slowly, and the monomer is dripped at the same time, so that the monomer concentration in the reactor is always maintained in a stable range, so that the internal environment of the polymerization reaction remains basically unchanged, thereby obtaining an acrylate pressure-sensitive adhesive with a narrow molecular weight distribution. Patent CN112694558A provides a method for regulating the molecular weight of methacrylic resin, comprising the following steps: placing a monomer of methacrylic resin in a glass bottle; adding a photoinitiator to the glass bottle, mixing evenly, to obtain a prepolymer, wherein the photoinitiator is miscible with the monomer of the methacrylic resin, and the prepolymer does not contain a solvent; and irradiating the prepolymer in the glass bottle with light of a certain intensity to cause the prepolymer to undergo a photopolymerization reaction, to obtain methacrylic resin. Summary of the invention

[0004] The object of the present invention is to provide a method for regulating the change of the molecular weight of an electronic-grade acrylic resin. The method adopts a starvation reactor to accurately regulate the reaction concentration so as to regulate the molecular weight, and utilizes a water-carrying agent to take away the heat of the reaction system and the hot water that is azeotroped with the water-carrying agent into an inert atmosphere, so as to obtain an electronic-grade acrylic resin.

[0005] To achieve the above object, the technical solution of the present invention is as follows:

[0006] In one aspect, the present invention provides a method for regulating the molecular weight change of an electronic grade acrylic resin, wherein the method uses a mixture A for a polymerization reaction process and a mixture B for controlling a reaction concentration to achieve regulation of the polymerization reaction;

[0007] The mixture A comprises monomer A, initiator and organic solvent A;

[0008] The mixture B comprises a monomer B, an organic solvent B and a water-carrying agent.

[0009] Furthermore, the specific steps of the method are as follows:

[0010] S1: In an inert gas atmosphere, mixture A is added into a reactor and the temperature is raised to perform a polymerization reaction;

[0011] S2: Mixture B is added at a reaction consumption rate. During the polymerization reaction, an inert gas is continuously circulated in the reactor.

[0012] Furthermore, the mixture B is added into the polymerization reaction system in a variety of ways, for example, the mixture B is added below the liquid level of the polymerization reaction system using a feeding pipe.

[0013] Furthermore, the mixture A is prepared as follows: in an inert gas atmosphere, the monomer A, the initiator and the organic solvent A are uniformly mixed. Before the mixture A is put into the reactor, it is in an unpolymerized form or in a slightly polymerized form.

[0014] Furthermore, the mixture B is prepared as follows: in an inert gas atmosphere, the monomer B, the organic solvent B and the water-carrying agent are mixed uniformly.

[0015] Furthermore, the concentration ratio of monomer A in the mixture A to monomer B in the mixture B is 1:1-10.

[0016] Furthermore, the mass ratio of the initiator to the water-carrying agent is 1 to 10:1.

[0017] Furthermore, the mass ratio of the monomer to the water-carrying agent is 100 to 1000:1, wherein the mass of the monomer is the sum of the masses of monomer A and monomer B.

[0018] Further, the volume ratio of the monomer to the organic solvent is 1:3-10, wherein the volume of the organic solvent is the volume sum of the organic solvent A and the organic solvent B, wherein the mass of the monomer is the mass sum of the monomer A and the monomer B. The volume ratio of the organic solvent A to the organic solvent B is 1:1-10.

[0019] Furthermore, the reaction consumption rate is the replenishment rate of the mixture B, and the replenishment rate is the concentration change rate, that is, 0.1% to 10% / min.

[0020] Furthermore, the polymerization reaction temperature is 50-90°C.

[0021] Furthermore, the reaction time of the polymerization reaction is 4 to 8 hours.

[0022] Furthermore, the initiator can be appropriately selected from azo free radical initiators, peroxide free radical initiators, redox free radical initiators, etc. in the prior art. As azo free radical initiators, 2,2'-azobisisobutyronitrile, 2,2'-azobis(2,4-dimethylvaleronitrile), 2,2'-azobismethoxyisoheptanenitrile, etc. can be listed. As peroxide free radical initiators, percarbonate compounds such as diisopropyl peroxydicarbonate, bis(2-ethylhexyl) peroxydicarbonate, and diethoxyethyl peroxydicarbonate can be listed; perester compounds such as tert-butyl peroxyneodecanoate, α-cumyl peroxyneodecanoate, and tert-butyl peroxyneodecanoate; acetylcyclohexylsulfone peroxide, diisobutyryl peroxide; 2,4,4-trimethylpentyl-2-peroxyphenoxyacetate, etc. can be listed.

[0023] Furthermore, the water-carrying agent can be appropriately selected from one or more of benzene, toluene, n-propanol, isobutanol, ethanol, isopropanol, chloroethanol, cyclohexane, chloroform, and carbon tetrachloride in the prior art. The water-carrying agent can be any organic solvent that does not participate in the polymerization reaction.

[0024] Further, the organic solvent is selected from ethylene glycol monomethyl ether, ethylene glycol monoethyl ether, methyl cellosolve acetate, ethyl cellosolve acetate, diethylene glycol monomethyl ether, diethylene glycol monoethyl ether, propylene glycol, propylene glycol monomethyl ether, propylene glycol monomethyl ether acetate, propylene glycol propyl ether acetate, toluene, xylene, methyl ethyl ketone, cyclopentanone, cyclohexanone, 2-hydroxyethyl propionate, 2-hydroxy-3-methylbutyrate, methyl 3-methoxypropionate, ethyl 3-methoxypropionate, ethyl 3-ethoxypropionate, methyl 3-ethoxypropionate, methyl pyruvate, ethyl pyruvate, ethyl acetate, butyl acetate, ethyl lactate, butyl lactate, N,N-dimethylformamide and N-methylpyrrolidone. The organic solvent is any organic solvent that does not participate in the reaction in the polymerization reaction.

[0025] Further, the monomer is selected from one or more of methyl methacrylate, butyl acrylate, 2-methyl-2-adamantyl methacrylate, methyl methacrylate butyrolactone, 2-hydroxyethyl methacrylate, ethyl acrylate, butyl acrylate, isooctyl acrylate, β-hydroxypropyl acrylate, β-hydroxypropyl methacrylate, 2-carboxy-6-norbornyl lactone-5-methacrylate, 3-hydroxy-1-adamantyl methacrylate, 2-ethyl-2-adamantyl methacrylate, 2-hydroxyethyl methacrylate, and hydroxyethyl acrylate.

[0026] Furthermore, the inert gas is selected from nitrogen, argon and other gases that do not participate in the reaction under the polymerization reaction conditions. The inert gas is continuously circulated during the polymerization reaction, which means that the inert gas at room temperature continuously enters the reactor, and at the same time, the inert gas with a certain amount of heat that is entrained with the water-carrying agent and moisture is continuously extracted from the reactor. Furthermore, the circulation rate of the inert gas is 1 to 100 mL / min, and the continuously circulated inert atmosphere not only takes away the heat of the reaction system, but also takes away the water-carrying agent and moisture that are azeotropically mixed into the inert atmosphere.

[0027] Furthermore, the reactor may be any reactor, reaction device or reaction system that can realize a starvation reaction, such as a starvation reactor.

[0028] Furthermore, the specific process of the method is as follows:

[0029] Pretreatment: Mixture A is prepared as follows: Under a nitrogen atmosphere, monomer A, initiator and organic solvent A are mixed evenly and set aside; Mixture B is prepared as follows: Under a nitrogen atmosphere, monomer B, organic solvent B and water-carrying agent are mixed evenly and set aside;

[0030] S1: In a nitrogen atmosphere, add mixture A into a starvation reactor, raise the temperature to 50-90°C, stir at 90-390 r / min (preferably 290 r / min), and perform polymerization for 4-8 hours;

[0031] S2: Using a feeding tube, the mixture B is added below the liquid surface of the polymerization reaction system at a reaction consumption rate of 0.1% to 10% / min. During the polymerization reaction, nitrogen is continuously circulated in the reactor. After the reaction is completed, an electronic grade acrylic resin is obtained.

[0032] In another aspect, the acrylic resin or macromonomer or graft copolymer prepared by the method of the present invention is used in coating applications.

[0033] In one aspect, the acrylic resin or macromonomer or graft copolymer prepared by the method of the present invention is used in graphic arts applications, including film coatings and overprint varnishes.

[0034] In one aspect, the acrylic resin or macromonomer or graft copolymer prepared by the method of the present invention is used in adhesive applications.

[0035] The present invention uses precise control of the concentration of reactants to control the molecular weight of the product, ensures that the circulating inert gas cooperates with the water-carrying agent to control the temperature of the reaction system, and other methods to achieve the acquisition of electronic grade acrylic resin or macromolecular monomer or graft copolymer. Specifically, it is embodied in:

[0036] ① The mixture A enters the reactor and starts the polymerization reaction first; the mixture B is added in a manner that the addition rate is consistent with the consumption rate and is directly added into the polymerization reaction system. The addition method of the mixture B consumes a certain amount of heat on the one hand, and controls the speed of the polymerization reaction on the other hand, and generally controls the heat release of the entire polymerization reaction.

[0037] ② On the one hand, after being added into the polymerization reaction system, the water-carrying agent of the present invention absorbs the water generated in the system, so that the reaction system solution forms a microemulsion; relative to the polymer particles, the concentration of the monomer expanded micelles is higher, and thus the possibility of the free radicals in the reaction system entering the particles and terminating is smaller; on the other hand, the continuously flowing inert atmosphere not only takes away the heat of the reaction system, but also takes away the water-carrying agent and water that are azeotropically mixed into the inert atmosphere.

[0038] Based on the combined effects of ① and ②, not only can the reaction temperature of the polymerization reaction system be effectively controlled at 50-90°C (preferably 70-90°C), but the molecular weight of the polymer in the polymerization reaction can also be controlled, which is beneficial to the production of electronic grade acrylic resin.

[0039] The experimental environment conditions of the embodiments of the present application are experiments conducted in a clean room environment, and the process parameters also require no metal devices.

[0040] Compared with the prior art, the beneficial technical effects of the present invention are as follows:

[0041] 1: The present invention controls the molecular weight by controlling the feeding rate and feeding position of the mixture B, and can keep the dispersion unchanged.

[0042] 2: The present invention utilizes a water-carrying agent and a circulating inert atmosphere to not only remove the heat of the reaction system, but also remove the moisture in the reaction system, inhibit the occurrence of side reactions, and simultaneously control the temperature of the reaction system and the reaction rate. DETAILED DESCRIPTION

[0043] The technical solution of the present invention is illustrated below by way of example, and the scope of protection requested by the present invention includes but is not limited to the following embodiments.

[0044] Preparation Example

[0045] The mixture A is prepared as follows: under a nitrogen atmosphere, the monomer A, the initiator and the organic solvent A are mixed uniformly and set aside;

[0046] The mixture B is prepared as follows: under a nitrogen atmosphere, the monomer B, the organic solvent B and the water-carrying agent are mixed evenly and set aside;

[0047] S1: In a nitrogen atmosphere, add mixture A into a starvation reactor, raise the temperature to 50-90°C, stir at 290 r / min, and perform polymerization for 4-8 hours;

[0048] S2: Using a feeding tube, the mixture B is added below the liquid level of the polymerization reaction system at a reaction consumption rate of 0.1% to 10% / min. During the polymerization reaction, the nitrogen in the reactor is kept flowing at a rate of 0.1 mL / min. After the reaction is completed, an electronic grade acrylic resin is obtained.

[0049] Example 1

[0050] Monomer A is methyl methacrylate; initiator is 2,2'-azobisisobutyronitrile; organic solvent A is ethylene glycol monomethyl ether; monomer B is methyl methacrylate; organic solvent B is ethylene glycol monomethyl ether;

[0051] The concentration ratio of monomer A in mixture A to monomer B in mixture B is 1:1; the volume ratio of monomer to organic solvent is 1:3, and the volume ratio of organic solvent A to organic solvent B is 1:1;

[0052] A method for regulating the molecular weight change of electronic grade acrylic resin comprises the following steps:

[0053] Pretreatment: Mixture A is prepared as follows: Under a nitrogen atmosphere, monomer A, initiator and organic solvent A are mixed evenly and set aside; mixture B is prepared as follows: Under a nitrogen atmosphere, monomer B and organic solvent B are mixed evenly and set aside.

[0054] Synthesis of resin: Under nitrogen atmosphere, mixture A was added to the starvation reactor, and then the starvation reactor was placed in an oil bath. The rotor speed was adjusted to 290 r / min and the oil bath temperature was 60°C. At the same time, two pipes a and b were left in the starvation reactor. Pipe a was passed under the liquid surface, and pipe b was placed above the liquid surface. Mixture B was added to the starvation reactor through port a at room temperature, and the addition rate was 1% / min. Pipe b simultaneously extracted the gas above the reactor. During the reaction, nitrogen was kept flowing in the two devices. The reaction time was 6 hours. After the reaction was completed, samples were taken for GPC measurement.

[0055] Example 2

[0056] The difference from Example 1 is that the concentration ratio of monomer A in mixture A to monomer B in mixture B is 1:2; and the charging acceleration rate is 0.8% / min.

[0057] Example 3

[0058] The difference from Example 1 is that the concentration ratio of monomer A in mixture A to monomer B in mixture B is 1:3; and the charging acceleration rate is 1.2% / min.

[0059] Example 4

[0060] The difference from Example 1 is that the concentration ratio of monomer A in mixture A to monomer B in mixture B is 1:4; and the charging acceleration rate is 3% / min.

[0061] Example 5

[0062] The difference from Example 1 is that:

[0063] The mixture B is prepared as follows: in a nitrogen atmosphere, the monomer B, the organic solvent B and the water carrier are uniformly mixed; the water carrier is toluene;

[0064] The mass ratio of the monomer to the water-carrying agent is 100:1, the concentration ratio of the monomer A in the mixture A to the monomer B in the mixture B is 1:1; and the replenishment acceleration rate is 0.4% / min.

[0065] Example 6

[0066] The difference from Example 1 is that:

[0067] The mixture B is prepared as follows: in a nitrogen atmosphere, the monomer B, the organic solvent B and the water carrier are uniformly mixed; the water carrier is toluene;

[0068] The mass ratio of the monomer to the water-carrying agent is 100:1, the concentration ratio of the monomer A in the mixture A to the monomer B in the mixture B is 1:2; and the replenishment acceleration rate is 0.8% / min.

[0069] Embodiments 7 to 16

[0070] The difference from Example 1 is that:

[0071]

[0072]

[0073]

[0074] Comparison Example 1

[0075] The difference from Example 1 is that:

[0076] The preparation method of traditional acrylic resin includes the following steps:

[0077] Put the monomer, organic solvent and initiator into the starvation reactor at one time, then put the starvation reactor into the oil bath, adjust the rotor speed to 290r / min and the oil bath temperature to 60°C, ensure that the device reacts under a nitrogen atmosphere during the reaction, the reaction time is 6h, and after the reaction is completed, take samples for GPC sampling.

[0078] Comparison Example 2

[0079] The difference from Example 1 is that:

[0080] The preparation method of traditional acrylic resin includes the following steps:

[0081] Put the monomer, organic solvent, initiator and water-carrying agent into the starvation reactor at one time, then put the starvation reactor into the oil bath, adjust the rotor speed to 290r / min and the oil bath temperature to 60°C, ensure that the device reacts under a nitrogen atmosphere during the reaction, the reaction time is 6h, and after the reaction, take samples for GPC sampling.

[0082] Comparison Example 3

[0083] The difference from Example 1 is that:

[0084] The preparation method of traditional acrylic resin includes the following steps:

[0085] Put the monomer, organic solvent, initiator and water-carrying agent into the starvation reactor at one time, then put the starvation reactor into the oil bath, adjust the rotor speed to 290r / min and the oil bath temperature to 60°C, ensure that the device reacts in a nitrogen atmosphere during the reaction, and the nitrogen continues to flow. The reaction time is 6h. After the reaction, take samples for GPC sampling.

[0086] Product sampling test of each embodiment:

[0087] The experimental results are shown in Table 1:

[0088] Table 1. Polymerization results under different conditions

[0089] Example Weight average molecular weight / g·mol Polydispersity Temperature rise indication Example 1 31701 2.56 7℃ Example 2 26584 2.44 6℃ Example 3 25957 2.25 5℃ Example 4 22467 2.21 4℃ Example 5 21891 2.17 3℃ Example 6 20794 2.13 3℃ Comparative Example 1 67234 3.21 10℃ Comparative Example 2 56379 2.84 8℃ Comparative Example 3 51056 2.75 8℃

[0090] During the reaction process of Examples 1 to 4, no water-carrying agent was used. From the test results, it can be seen that by adding the mixture B and controlling the addition method, the molecular weight can be more accurately regulated, and the temperature rise effect can also be controlled to a certain extent.

[0091] By comparing Examples 1-2 with Examples 5-6, it can be seen that after adding the water-carrying agent, the temperature rise in the reactor is further controlled, and the molecular weight of the obtained polymer is also further controlled.

[0092] By comparing the results of Examples 1 and 6 with Comparative Examples 1 to 3, it can be seen that the molecular weight of the traditional method changes with the increase of temperature and the change of concentration. The method of the present application can indeed accelerate the polymerization of the monomers. At the same time, the reaction temperature is effectively controlled, which can slow down the polymerization explosion. At the same time, by adding mixture B, the polymerization reaction proceeds smoothly and the polymerization molecular weight is controlled more accurately.

[0093] The experimental environment conditions of the embodiments of the present application are experiments conducted in a clean room environment, and the process parameters also require metal-free devices; the purified electronic-grade resin is tested by ICP-MS-MS, and the metal ion content is less than 50ppb, and the chloride ion content is less than 10ppm.

[0094] Comparison Example 4

[0095] The difference from Example 1 is that the experimental environment is an ordinary laboratory room, and the reaction container and the sampling pipelines a and b have low requirements for metal impurities. The purified ordinary grade resin is tested by ICP-MS-MS, and the metal ion content is less than 10ppm, the chloride ion content is less than 500ppm, the product Mw=31701, and PDI=2.56.

[0096] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A method for regulating the molecular weight change of electronic grade acrylic resin, characterized in that: The method adopts a mixture A for the polymerization process and a mixture B for controlling the reaction concentration to achieve the regulation of the polymerization reaction; The mixture A comprises monomer A, initiator and organic solvent A; The mixture B includes a monomer B and an organic solvent B; The specific steps of the method are as follows: S1: In an inert gas atmosphere, mixture A is added into a reactor and the temperature is raised to perform a polymerization reaction; S2: Mixture B is added at a reaction consumption rate. During the polymerization reaction, an inert gas is continuously circulated in the reactor.

2. The method according to claim 1, characterized in that: The mixture B also includes a water carrier.

3. The method according to claim 1, characterized in that: The mixture B is added below the liquid level of the polymerization reaction system by using a feeding tube, wherein the inert gas is selected from nitrogen and argon; The mixture A is prepared as follows: in an inert gas atmosphere, monomer A, initiator and organic solvent A are uniformly mixed; The mixture B is prepared as follows: in an inert gas atmosphere, the monomer B, the organic solvent B and the water-carrying agent are mixed uniformly.

4. The method according to claim 2, characterized in that: The concentration ratio of monomer A in the mixture A to monomer B in the mixture B is 1:1 to 10; further, the mass ratio of the initiator to the water-carrying agent is 1 to 10:1; further, the mass ratio of the monomer to the water-carrying agent is 100 to 1000:1, wherein the mass of the monomer is the sum of the masses of monomer A and monomer B.

5. The method according to claim 2, characterized in that: The volume ratio of the monomer to the organic solvent is 1:3-10, wherein the volume of the organic solvent is the sum of the volumes of the organic solvent A and the organic solvent B, and the mass of the monomer is the sum of the masses of the monomer A and the monomer B.

6. The method according to claim 2, characterized in that: The reaction consumption rate is the feed rate of mixture B, that is, 0.1% to 10% / min; further, the polymerization temperature is 50 to 90° C.; further, the polymerization time is 4 to 8 hours.

7. The method according to claim 2, characterized in that: The initiator is selected from at least one of an azo free radical initiator, a peroxide free radical initiator, and a redox free radical initiator; The water-carrying agent is selected from one or more of benzene, toluene, n-propanol, isobutanol, ethanol, isopropanol, chloroethanol, cyclohexane, chloroform, and carbon tetrachloride; Further, the organic solvent A and the organic solvent B are independently selected from ethylene glycol monomethyl ether, ethylene glycol monoethyl ether, methyl cellosolve acetate, ethyl cellosolve acetate, diethylene glycol monomethyl ether, diethylene glycol monoethyl ether, propylene glycol, propylene glycol monomethyl ether, propylene glycol monomethyl ether acetate, propylene glycol propyl ether acetate, toluene, xylene, methyl ethyl ketone, cyclopentanone, cyclohexanone, ethyl 2-hydroxypropionate, methyl 2-hydroxy-3-methylbutyrate, methyl 3-methoxypropionate, ethyl 3-methoxypropionate, ethyl 3-ethoxypropionate, methyl 3-ethoxypropionate, methyl pyruvate, ethyl pyruvate, ethyl acetate, butyl acetate, ethyl lactate, butyl lactate, N,N-dimethylformamide and N-methylpyrrolidone.

8. The method according to claim 1, characterized in that: The monomer A and monomer B are independently selected from one or more of methyl methacrylate, butyl acrylate, 2-methyl-2-adamantyl methacrylate, methyl methacrylate butyrolactone, 2-hydroxyethyl methacrylate, ethyl acrylate, butyl acrylate, isooctyl acrylate, β-hydroxypropyl acrylate, β-hydroxypropyl methacrylate, 2-carboxy-6-norbornyl lactone-5-methacrylate, 3-hydroxy-1-adamantyl methacrylate, methyl methacrylate, 2-ethyl-2-adamantyl methacrylate, 2-hydroxyethyl methacrylate, and hydroxyethyl acrylate.

9. The method according to claim 1, characterized in that: The method process is as follows: Pretreatment: Mixture A is prepared as follows: Under a nitrogen atmosphere, monomer A, initiator and organic solvent A are mixed evenly and set aside; Mixture B is prepared as follows: Under a nitrogen atmosphere, monomer B, organic solvent B and water-carrying agent are mixed evenly and set aside; S1: In a nitrogen atmosphere, add mixture A into a starvation reactor, heat to 50-90°C, stir at 90-390 r / min, and perform polymerization for 4-8 hours; S2: Using a feeding tube, the mixture B is added below the liquid surface of the polymerization reaction system at a reaction consumption rate of 0.1% to 10% / min. During the polymerization reaction, nitrogen is continuously circulated in the reactor. After the reaction is completed, an electronic grade acrylic resin is obtained.

10. Use of the acrylic resin or macromonomer or graft copolymer prepared by the method of claim 1 in coating applications, graphic arts applications and adhesive applications.

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