A method for preparing high quality bisphenol a polyoxypropylene ether

Abstract

This application belongs to the field of polymer compound preparation technology, and specifically relates to a method for preparing high-quality bisphenol A polyoxypropylene ether. Reactor A serves as a preparation vessel for a mixed solution of bisphenol A and propylene oxide, while reactor B serves as a polymerization vessel for bisphenol A polyoxypropylene ether. Solid bisphenol A is used as the initiator; a portion of the initiator is added as solid feed, and the remaining solid bisphenol A is mixed and dissolved with propylene oxide to form a bisphenol A-propylene oxide solution. This bisphenol A-propylene oxide solution is used as a monomer for polymerization. After the reaction, the product is purified to obtain bisphenol A polyoxypropylene ether. The bisphenol A polyoxypropylene ether produced by this method has a light color value, narrow molecular weight distribution, low unsaturation, and stable product quality. The method reduces the initial amount of solid bisphenol A during production, ensuring high-efficiency production while reducing equipment requirements and operational difficulty, eliminating mechanical damage from stirring, and avoiding production accidents and economic losses.

Description

Technical Field

[0001] This application belongs to the field of polymer compound preparation technology, and specifically relates to a method for preparing high-quality bisphenol A polyoxypropylene ether. Background Technology

[0002] Bisphenol A, also known as 2,2-bisphenol A propane, is a key organic chemical raw material, and its derived bisphenol A polyoxypropylene ethers are widely used in the chemical industry. Due to the rigidity imparted by the aromatic rings in their molecular structure and the toughness provided by the carbon-oxygen segments, these polyethers can significantly optimize polymer properties. They are not only important monomers for synthesizing stable resins and can be used to prepare shock-resistant, photosensitizing, and adhesive materials, but also serve as polymer chain modifiers, playing an important role in coatings, adhesives, and rubber. Bisphenol A epoxy resins synthesized using bisphenol A as an intermediate possess excellent properties such as high temperature resistance, acid and alkali resistance, and strong adhesion.

[0003] Due to the high melting point of bisphenol A, the preparation of bisphenol A polyoxypropylene ether in existing production technologies mainly adopts two feeding methods: one is to directly feed solid bisphenol A. Because of the large amount of solid particles present, the stirring equipment needs to withstand extremely high loads in the early stage of the reaction, which not only easily leads to equipment wear, failure, or even production accidents, but also makes the system a solid-gas two-phase state, resulting in uneven contact between bisphenol A and propylene oxide and catalyst, slow reaction rate, and poor polymerization stability; the other is to mix bisphenol A with low molecular weight bisphenol A polyether for feeding. Although the feeding state is improved to a certain extent, the production efficiency is low, and the solid bisphenol A is still prone to "clumping" phenomenon, which damages the stirring equipment and affects the uniformity of the reaction.

[0004] Furthermore, existing technologies also have significant product quality issues. The phenolic hydroxyl groups of bisphenol A are easily oxidized to generate colored impurities, directly leading to a darker color value in the product. Propylene oxide monomers are mostly fed in a single batch, and at high concentrations, they are prone to side reactions such as local self-polymerization and cross-linking, further resulting in a wide molecular weight distribution, high unsaturation, and large batch-to-batch quality fluctuations, which seriously restricts the application effect of bisphenol A polyoxypropylene ether in downstream fields. Summary of the Invention

[0005] To address the technical problems in existing technologies, such as the high melting point of bisphenol A leading to heavy equipment load, damage, and uneven reaction due to solid feeding, as well as the resulting products having dark color values, wide molecular weight distribution, high unsaturation, and poor stability, this application provides a method for preparing high-quality bisphenol A polyoxypropylene ether. The bisphenol A polyoxypropylene ether produced by this method has a light color value, narrow molecular weight distribution, low unsaturation, and stable product quality. This method reduces the initial amount of solid bisphenol A fed into the production process, ensuring high-efficiency production while lowering equipment requirements and operational difficulty. It also eliminates mechanical damage from stirring and avoids production accidents and economic losses.

[0006] This application provides a method for preparing high-quality bisphenol A polyoxypropylene ether, comprising the following steps:

[0007] S1. Add bisphenol A and propylene oxide to reactor A, stir and mix them in an inert gas atmosphere to obtain a bisphenol A and propylene oxide mixed solution, and keep it under inert gas pressure protection for later use.

[0008] S2. Add bisphenol A and potassium hydroxide to reactor B, stir and heat in an inert gas atmosphere, then add the bisphenol A and propylene oxide mixed solution prepared in step S1 to reactor B in batches. After the first addition of the bisphenol A and propylene oxide mixed solution, raise the temperature to 90-120℃, and then add the bisphenol A and propylene oxide mixed solution to reactor B a second time. Carry out the polymerization reaction at 100-140℃ and pressure <0.4MPa for 1-3 hours.

[0009] S3. Remove the monomer from the product after step S2 and then perform post-treatment to obtain bisphenol A polyoxypropylene ether.

[0010] Furthermore, in step S1, 500-1500 parts by mass of bisphenol A and 1000-3000 parts by mass of propylene oxide are added to reactor A.

[0011] Furthermore, the weight ratio of bisphenol A to propylene oxide in step S1 is 1:1 to 1:7.

[0012] Furthermore, in step S2, the amount of solid bisphenol A added to reactor B is 500-1500 parts by mass, and the amount of potassium hydroxide is 4-12 parts by mass.

[0013] Furthermore, in step S2, the first addition of the bisphenol A propylene oxide mixed solution is 50-150 parts by weight, and the second addition of the bisphenol A propylene oxide mixed solution is 2500-3500 parts by weight.

[0014] Furthermore, in step S1, the stirring and mixing time is 0.5-2 hours, and the temperature is 5-20℃.

[0015] Furthermore, the inert gas atmosphere described in step S2 is replaced by nitrogen with positive and negative pressure, and the oxygen content of the atmosphere is ≤100ppm.

[0016] Furthermore, in step S2, bisphenol A and potassium hydroxide are stirred and heated in an inert gas atmosphere at a temperature of 50-60°C.

[0017] Furthermore, the monomer removal temperature in step S3 is 100-110℃.

[0018] In existing technologies, bisphenol A, due to its high melting point of 158-160℃, is often directly added to the reaction system in solid form during production. This leads to problems such as a sharp increase in stirring load, uneven solid-gas two-phase reaction, and severe equipment wear. Step S1, by pre-mixing a portion of bisphenol A with propylene oxide in reactor A, transforms the previously difficult-to-handle solid bisphenol A into a homogeneous solution, thereby reducing the initial amount of solid bisphenol A added to the subsequent polymerization reactor. Propylene oxide serves as both a solvent for dissolving bisphenol A and a core monomer for the subsequent polymerization reaction, improving raw material utilization and simplifying the process. The phenolic hydroxyl groups in the bisphenol A molecule have a certain polarity, while propylene oxide, as a polar cyclic ether compound, can dissolve during mixing through intermolecular forces, forming a homogeneous phase. This avoids the drawbacks of bisphenol A existing in solid particulate form. The phenolic hydroxyl groups of bisphenol A are easily oxidized by oxygen in the air, generating colored impurities such as quinone compounds. This directly leads to a darker color in the final product. Inert gases not only isolate oxygen, preventing the oxidation of bisphenol A and propylene oxide, but also maintain a slightly positive pressure environment within reactor A through "pressure protection," preventing external air from mixing into the solution and ensuring the purity and stability of the mixed solution, providing a clean raw material basis for subsequent polymerization reactions. The preparation of the mixed solution significantly reduces the amount of solid bisphenol A required in reactor B, fundamentally reducing the stirring load on reactor B. The original condition requiring the stirring of a large number of solid particles is transformed into a liquid-based mixed system, significantly reducing stirring resistance and completely avoiding mechanical damage to the stirring equipment caused by excessively hard or numerous solid particles, thus reducing equipment maintenance costs and the risk of production accidents. Furthermore, the solution-state bisphenol A and propylene oxide can enter the reaction system more uniformly during subsequent feeding, avoiding the common "agglomeration" phenomenon of solid bisphenol A, laying the foundation for a uniform polymerization reaction. In addition, the protection of inert gas effectively reduces the generation of oxidation byproducts, improving the color value of the product from the source and ensuring the final result of a light-colored product.

[0019] Step S2 involves adding bisphenol A and potassium hydroxide to reactor B and stirring and heating under an inert gas atmosphere. This operation establishes a stable polymerization initiation system. Retaining a portion of solid bisphenol A as an initiator is necessary because completely dissolved bisphenol A may not form a sufficiently active polymerization starting point in the initial stage. The presence of a small amount of solid bisphenol A serves as an anchor point for the reaction, working in conjunction with the potassium hydroxide catalyst to initiate polymerization. Potassium hydroxide, as a strong base, works by reacting with the phenolic hydroxyl group of bisphenol A in an acid-base reaction, causing the hydroxyl group to dehydrogenate and form a phenoxy anion. The phenoxy anion is a strong nucleophile capable of attacking the epoxy groups of propylene oxide, thereby initiating the ring-opening polymerization of propylene oxide. Heating and stirring promote the interaction between bisphenol A and potassium hydroxide, while stirring further enhances the homogeneity of the system, preventing uneven reaction caused by excessively high or low catalyst concentrations in certain areas. The inert gas atmosphere continues to isolate oxygen, preventing the activated phenoxy anions from being oxidized and ensuring the purity of the starting system.

[0020] The key innovation of step S2 is the subsequent addition of the mixed solution prepared in step S1 in batches. The initial addition of a small amount of the mixed solution, followed by a further increase in temperature to 100°C, is intended to initiate the initial polymerization reaction and form oligomeric seeds. Adding a small amount of the mixed solution avoids excessively high local concentrations caused by a large influx of monomers at once. If a large amount of solution were added at once, the high concentration of propylene oxide might trigger violent local reactions, producing side reactions such as self-polymerization and cross-linking, leading to a wider molecular weight distribution and increased unsaturation. By adding a small amount initially, the activated bisphenol A reacts gently with propylene oxide to generate short-chain oligomers. These oligomers can serve as templates for subsequent polymerization, allowing the added monomers to grow chains more orderly, thereby controlling the molecular weight distribution. Heating to 100°C raises the system temperature to the suitable active range for the polymerization reaction, ensuring the stable formation of seed oligomers and laying a uniform starting point for subsequent reactions. The secondary addition of the mixed solution and control of the reaction conditions are to achieve a stable and controllable polymerization reaction. Below 100℃, the ring-opening polymerization rate of propylene oxide is slow, resulting in low reaction efficiency. Above 140℃, excessively high temperatures exacerbate the self-polymerization reaction of propylene oxide and may trigger chain transfer reactions, increasing the unsaturation of the product. The 100-140℃ range ensures efficient polymerization while minimizing side reactions. Controlling the pressure to <0.4MPa is for both safety and reaction efficiency. Propylene oxide has a low boiling point; excessively high system pressure could exceed the equipment's limits, leading to a safety accident. Conversely, excessively low pressure would cause propylene oxide to volatilize, reducing monomer utilization and disrupting the homogeneity of the reaction system. Internal pressure reaction for 1-3 hours ensures complete monomer conversion. Maintaining a certain pressure allows propylene oxide to fully participate in the reaction in the liquid phase, reducing unreacted monomer residue. The beneficial effects of step S2 are significant. First, the phased feeding combined with the formation of seed oligomers completely solves the problems of solid bisphenol A agglomeration and stirring damage in existing technologies. The addition of the mixed solution keeps the system in a predominantly liquid state, ensuring uniform stirring load and avoiding the impact of solid particles on the stirring equipment. Second, precise temperature and pressure control ensures the uniformity of the polymerization reaction. The guidance of seed oligomers allows the chain growth process to proceed in an orderly manner, reducing the phenomenon of inconsistent molecular chain lengths, thus resulting in a narrow molecular weight distribution of the product. The reduction of side reactions directly improves product performance, resulting in a lighter color value and lower unsaturation. In addition, the optimization of reaction conditions reduces the requirements for equipment. There is no need for high-intensity stirring equipment to handle large amounts of solid feed, nor is it necessary to withstand excessive pressure. Equipment investment and maintenance costs are reduced, while production accidents caused by equipment overload are avoided, improving production safety.

[0021] Step S3 aims to further improve product purity and stability, ensuring the final product meets application requirements. The monomer removal process targets unreacted propylene oxide remaining after the polymerization reaction. If these residual monomers are present in the product, they will volatilize during subsequent processing or application, causing fluctuations in material properties such as volume shrinkage, decreased adhesion, and even the generation of irritating odors, affecting the product's application scenarios. The principle of monomer removal utilizes the boiling point difference between propylene oxide and bisphenol A polyoxypropylene ether. Propylene oxide has a low boiling point, while the polyether product has a high boiling point. Through heating or reduced pressure, the residual propylene oxide can be volatilized and removed, ensuring that the amount of residual monomer in the product is reduced to an extremely low level. The principle of the post-treatment stage is to remove impurities from the system. If the potassium hydroxide catalyst used in the reaction remains, it will cause the product to be alkaline, which may trigger degradation reactions during storage, affecting product stability. Simultaneously, alkaline residues can interfere with crosslinking or curing reactions in subsequent applications. By adding acid to neutralize potassium hydroxide, easily filterable salts are generated, which are then removed by filtration, completely removing catalyst residues. Dehydration removes trace amounts of moisture that may be generated during the reaction, as the presence of moisture can affect the product's storage stability and processing performance. In summary, the three steps are interconnected: from raw material pretreatment to polymerization reaction control, and finally to product refining. Each step is designed to address the pain points of existing technologies. Through the combination of chemical principles and process optimization, high-quality production of bisphenol A polyoxypropylene ether has been achieved. This not only solves the problems of equipment wear and tear and safety hazards in production but also significantly improves product performance, laying a solid foundation for its application in multiple fields.

[0022] In summary, the beneficial effects of this application are as follows:

[0023] 1. By using a premixing process to prepare a homogeneous solution from a portion of bisphenol A and propylene oxide, the initial amount of solid bisphenol A fed into reactor B is significantly reduced. This avoids the problems of increased stirring load, uneven solid-gas two-phase reaction, and equipment wear caused by solid particles, and significantly reduces stirring resistance and equipment maintenance costs.

[0024] 2. Propylene oxide combines the functions of a solvent for dissolving bisphenol A and a monomer for polymerization, eliminating the need for additional solvents. This improves the overall utilization rate of raw materials and eliminates the need for additional solvent addition, effectively simplifying the production process.

[0025] 3. Solution-state bisphenol A avoids solid agglomeration. The batch feeding mode, combined with the formation of seed oligomers, guides the orderly growth of chains, resulting in a narrower molecular weight distribution of the product. Inert gas protection reduces oxidation byproducts, and precise temperature and pressure control reduces side reactions such as self-polymerization, significantly improving the product's color value, reducing unsaturation, and greatly enhancing quality stability.

[0026] 4. No need to configure high-strength mixing equipment to handle large amounts of solid feed. The pressure is controlled within a safe range, which reduces equipment investment costs and overload risks, and also reduces production accidents caused by equipment overload, significantly improving the safety of production operations. Detailed Implementation

[0027] Example 1

[0028] S1. At 18℃, towards 5m 3 1335 parts by mass of bisphenol A and 1780 parts by mass of propylene oxide were added to reactor A. Nitrogen gas was used for positive and negative pressure replacement. The oxygen content was measured to be ≤100ppm. Stirring was started and the mixture was stirred for 2 hours before being discharged to obtain a bisphenol A and propylene oxide mixed solution for later use. Nitrogen gas was used for pressure protection at 0.3MPa.

[0029] S2. 915.7 parts by weight of solid bisphenol A and 10.6 parts by weight of potassium hydroxide are evenly pumped into a 5m3 stainless steel reactor B in batches. Nitrogen gas is used for positive and negative pressure replacement five times each. After nitrogen gas positive and negative pressure replacement, the oxygen content is tested to be ≤100ppm.

[0030] S3. Start stirring and heat to 50°C. Press 105.5 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. Continue heating to 100°C, and then add 3009.5 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. The reaction temperature is 110°C, the reaction pressure is <0.2MPa, and the internal pressure reaction is carried out for 1.5 hours. After that, unreacted propylene oxide monomers are removed at 110°C to obtain crude polyether.

[0031] S4, after neutralization, adsorption drying, and filtration, bisphenol polyoxypropylene ether is obtained.

[0032] Similar effects can be achieved by adding 1000-1500 parts by mass of bisphenol A into reactor A.

[0033] In the experiment, potassium hydroxide can also be used in quantities of 10-12 parts by mass.

[0034] Example 2

[0035] S1. At 18℃, towards 5m 3 1000 parts by mass of bisphenol A and 1782 parts by mass of propylene oxide were added to reactor A. Nitrogen gas was used for positive and negative pressure replacement. The oxygen content was measured to be ≤100ppm. Stirring was started and the mixture was stirred for 0.5h. The mixture was then discharged to obtain a bisphenol A and propylene oxide mixed solution for later use. Nitrogen gas was used for pressure protection at 0.3MPa.

[0036] S2. 1250.7 parts by weight of solid bisphenol A and 8.2 parts by weight of potassium hydroxide are evenly pumped into a 5m... 3Inside stainless steel reactor B, nitrogen was used for positive and negative pressure purging five times each. After the nitrogen was used for positive and negative pressure purging, the oxygen content was measured to be ≤100ppm.

[0037] S3. Start stirring and heat to 60°C. Press 85.3 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. Continue heating to 90°C, and then add 2696.7 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. The reaction temperature is 90°C and the reaction pressure is <0.3MPa. After reacting under internal pressure for 2 hours, remove unreacted propylene oxide monomers at 100-110°C to obtain crude polyether.

[0038] S4, after neutralization, adsorption drying, and filtration, bisphenol A polyoxypropylene ether is obtained.

[0039] Similar results can be achieved by adding 1000-1500 parts by mass of solid bisphenol A in reactor B.

[0040] The propylene oxide in reactor A reacts well at concentrations of 1000-1500 parts by mass and 1500-1800 parts by mass.

[0041] Example 3

[0042] S1. At 18℃, towards 5m 3 800 parts by mass of bisphenol A and 2680 parts by mass of propylene oxide were added to reactor A. Nitrogen gas was used for positive and negative pressure replacement. The oxygen content was measured to be ≤100ppm. Stirring was started and the mixture was stirred for 0.5h. The mixture was then discharged to obtain a bisphenol A and propylene oxide mixed solution for later use. Nitrogen gas was used for pressure protection at 0.3MPa.

[0043] S2. 615.5 parts by weight of solid bisphenol A and 7.4 parts by weight of potassium hydroxide are evenly pumped into a 5m container in batches. 3 Inside stainless steel reactor B, nitrogen was used for positive and negative pressure purging five times each. After the nitrogen was used for positive and negative pressure purging, the oxygen content was measured to be ≤100ppm.

[0044] S3. Start stirring and heat to 55°C. Press 92.8 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. Continue heating to 120°C, and then add 3387.2 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. The reaction temperature is 140°C and the reaction pressure is <0.3MPa. After reacting under internal pressure for 2 hours, remove unreacted propylene oxide monomers at 105°C to obtain crude polyether.

[0045] S4, after neutralization, adsorption drying, and filtration, bisphenol A polyoxypropylene ether is obtained.

[0046] Adding 500-800 parts by mass of solid bisphenol A to reactor B can achieve similar results.

[0047] In the experiment, similar results could be obtained with 4-8 parts by mass of potassium hydroxide.

[0048] Example 4

[0049] S1. At 20℃, towards 5m 3 500 parts by mass of bisphenol A and 2686 parts by mass of propylene oxide were added to reactor A. Nitrogen gas was used for positive and negative pressure replacement. The oxygen content was measured to be ≤100ppm. Stirring was started and the mixture was stirred for 1.5h. The mixture was then discharged to obtain a bisphenol A and propylene oxide mixed solution for later use. Nitrogen gas was used for pressure protection at 0.3MPa.

[0050] S2. 915.5 parts by weight of solid bisphenol A and 10.1 parts by weight of potassium hydroxide are evenly pumped into a 5m3 stainless steel reactor B in batches. Nitrogen gas is used for positive and negative pressure replacement five times each. After nitrogen gas positive and negative pressure replacement, the oxygen content is tested to be ≤100ppm.

[0051] S3. Start stirring and heat to 55°C. Press 136.7 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. Continue heating to 100°C, and then add 3049.3 parts by mass of bisphenol A propylene oxide mixed solution into reactor B through reactor A. The reaction temperature is 120°C and the reaction pressure is <0.3MPa. After reacting under internal pressure for 2 hours, remove unreacted propylene oxide monomers at 110°C to obtain crude polyether.

[0052] S4, after neutralization, adsorption drying, and filtration, bisphenol A polyoxypropylene ether is obtained.

[0053] According to experiments, adding approximately 2680-3000 parts by mass of propylene oxide to the reactor can yield similar results.

[0054] According to the experimental results, the initial addition of the bisphenol A propylene oxide mixture can be 50-150 parts by weight; the secondary addition of the bisphenol A propylene oxide mixture can be 2500-3500 parts by weight.

[0055] In step S3, the reaction can proceed normally under a reaction pressure of 0.3±0.1MPa and an internal pressure reaction environment of 2h±1h.

[0056] Comparative Example 1

[0057] S1. 2254.8 parts by weight of solid bisphenol A and 12 parts by weight of potassium hydroxide are evenly pumped into a 5m container in batches. 3 Inside the stainless steel reactor, nitrogen was used for positive and negative pressure purging five times each. After the nitrogen was used for positive and negative pressure purging, the oxygen content was measured to be ≤100ppm.

[0058] S3. Start stirring, heat to 50℃, add 155.8 parts by mass of propylene oxide to the reactor, continue heating to 100℃, add 1625.6 parts by mass of bisphenol A propylene oxide mixed solution, reaction temperature 110℃, reaction pressure <0.3MPa, after reacting under internal pressure for 4 hours, remove unreacted propylene oxide monomers at 100-110℃ to obtain crude polyether.

[0059] S4, after neutralization, adsorption drying, and filtration, bisphenol polyoxypropylene ether is obtained.

[0060] Comparative Example 2

[0061] S1. Add 2000 parts by weight of solid bisphenol A, 500 parts by weight of BPA-3 polyether, and 9.8 parts by weight of potassium hydroxide sequentially to 5m 3 Inside the stainless steel reactor, nitrogen was used for positive and negative pressure purging five times each. After the nitrogen was used for positive and negative pressure purging, the oxygen content was measured to be ≤100ppm.

[0062] S3. Start stirring, heat to 60℃, add 90.3 parts by mass of propylene oxide to the reactor, continue heating to 100℃, add 1494.7 parts by mass of bisphenol A propylene oxide mixed solution, reaction temperature 110℃, reaction pressure <0.3MPa, react under internal pressure for 4 hours, remove unreacted propylene oxide monomer at 110℃ to obtain crude polyether.

[0063] S4, after neutralization, adsorption drying, and filtration, bisphenol polyoxypropylene ether is obtained.

[0064] The product performance data obtained from Examples 1 and 2, Examples 3 and 4, and Comparative Examples 1-2 are shown in the table below:

[0065]

Claims

1. A method for preparing high-quality bisphenol A polyoxypropylene ether, characterized in that, Includes the following steps: S1. Add bisphenol A and propylene oxide to reactor A, stir and mix them in an inert gas atmosphere to obtain a bisphenol A and propylene oxide mixed solution, and keep it under inert gas pressure protection for later use. S2. Add bisphenol A and potassium hydroxide to reactor B, stir and heat in an inert gas atmosphere, then add the bisphenol A and propylene oxide mixed solution prepared in step S1 to reactor B in batches. After the first addition of the bisphenol A and propylene oxide mixed solution, raise the temperature to 90-120℃, then add the bisphenol A and propylene oxide mixed solution to reactor B a second time, and carry out the polymerization reaction at 100-140℃ and pressure <0.4MPa for 1-3 hours. S3. Remove the monomer from the product after step S2, and then perform post-treatment to obtain bisphenol A polyoxypropylene ether; In step S1, 500-1500 parts by mass of bisphenol A and 1000-3000 parts by mass of propylene oxide are added to reactor A. In step S2, the amount of solid bisphenol A added to reactor B is 500-1500 parts by mass, and the amount of potassium hydroxide is 4-12 parts by mass. In step S2, the first addition of the bisphenol A propylene oxide mixed solution is 50-150 parts by weight, and the second addition of the bisphenol A propylene oxide mixed solution is 2500-3500 parts by weight. In step S1, the stirring and mixing time is 0.5-2 hours, and the temperature is 5-20℃; In step S2, bisphenol A and potassium hydroxide are stirred and heated in an inert gas atmosphere at a temperature of 50-60°C.

2. The method for preparing high-quality bisphenol A polyoxypropylene ether according to claim 1, characterized in that: The weight ratio of bisphenol A to propylene oxide in step S1 is 1:1 to 1:

7.

3. The method for preparing high-quality bisphenol A polyoxypropylene ether according to claim 1, characterized in that: The inert gas atmosphere described in step S2 is achieved by nitrogen positive and negative pressure replacement, with an oxygen content of ≤100ppm.

4. The method for preparing high-quality bisphenol A polyoxypropylene ether according to claim 1, characterized in that: The monomer removal temperature in step S3 is 100-110℃.

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