Polyether polyol for low hysteresis loss polyurethane foam tire and continuous preparation method thereof

Abstract

The present invention belongs to the technical field of polyether polyol synthesis, and specifically relates to a polyether polyol for low hysteresis loss polyurethane foam tire and a continuous preparation method thereof. The polyether polyol uses a 6-functionality small molecule alcohol as an initiator, a phosphazene catalyst or a phosphazene and an alkali metal catalyst mixed catalyst for catalytic reaction, and adopts a continuous preparation method, with a short production cycle and high yield. The prepared polyether polyol has the characteristics of high functionality, high molecular weight, low unsaturation, narrow molecular weight distribution, etc., and can be used in the preparation of polyurethane foam tires to reduce the compression permanent deformation of the material, reduce endogenous heat, and improve resilience, thereby solving the industry bottleneck problem that the foam tire cannot rebound or rebounds slowly after being loaded.

Description

Technical Field

[0001] The invention belongs to the technical field of polyether polyols, and in particular relates to a polyether polyol for a low hysteresis loss polyurethane foam tire and a continuous preparation method thereof. Background Art

[0002] Unlike traditional rubber tires, polyurethane foam tires do not need to be inflated, and have good resistance to cutting, tearing, abrasion, and needle puncture, as well as excellent acid and alkali resistance. They are becoming more and more popular, and are currently widely used in the fields of cargo carts, baby carriages, slow electric vehicles, etc. The polyether polyols obtained by traditional KOH catalytic polymerization have the disadvantages of low functionality, high unsaturation, and wide relative molecular weight distribution. The foam tires obtained have poor mechanical properties and poor resilience. When stacked for storage or under long-term load, they are prone to large compression permanent deformation or slow rebound, which restricts the development of foam tires.

[0003] In recent years, continuous processes have been increasingly accepted by many polyether manufacturers due to their short production cycle, high production capacity and low manufacturing cost. Most of them use DMC catalytic process, which has extremely high catalyst activity, small dosage and no need for post-treatment, but cannot prepare high-activity polyether terminated with ethylene oxide. Compared with alkaline catalysts such as KOH, phosphazene catalysts have high catalytic activity and low unsaturation of polyether. Compared with DMC catalysts, small molecule initiators can be used for polymerization and ethylene oxide can be used for termination.

[0004] Chinese patent 202011098909.7, published on July 23, 2021. A method for continuously preparing low-viscosity, low-unsaturation, low-odor, and high-activity polyether polyols by using a phosphazene catalyst as an oxidized olefin ring-opening polymerization catalyst is proposed. By continuously adding a phosphazene catalyst, an initiator, and an oxidized olefin into a continuous reactor to prepare a high-activity polyether polyol with a narrow molecular weight distribution and low unsaturation, and using a blending technical solution for the prepared polyol, the problem of high viscosity caused by narrow molecular distribution is solved, which provides the possibility for the semi-continuous preparation of low-viscosity, low-unsaturation, low-odor, and high-activity polyether polyols for industrial production. However, this method is a semi-continuous process and does not remove the strongly alkaline phosphazene catalyst in the polyether, which affects the catalyst activity during application, and is prone to cause polymerization kettles in the prepolymer synthesis process, which will cause foam coke during the high-resilience foam foaming process.

[0005] Chinese patent 202111008444.6, published on November 19, 2021. A method for preparing a sorbitol-based high molecular weight polyether polyol is proposed, using solid sorbitol and oligosorbitol-based polyether polyol as composite initiators, alkali metal as catalyst, ring-opening polymerization with epoxy compound, and then post-treatment to obtain a sorbitol-based high molecular weight polyether polyol with a nominal functionality of 6, but the method is an intermittent process, and the catalyst is an alkali metal, and the obtained polyether has a wide molecular weight distribution and high unsaturation.

[0006] In summary, the existing technology can prepare highly active polyether polyols, but it mostly adopts intermittent production with long cycle and low production capacity. There are also continuous reactors or semi-continuous production. However, continuous production can only be achieved through synthesis processes with simple processes such as DMC catalysis and no need for post-treatment. The polyether products synthesized by these processes are limited in downstream applications, which limits the development of continuous production by complex processes. Summary of the invention

[0007] In view of the deficiencies in the prior art, the object of the present invention is to provide a polyether polyol for a low hysteresis loss polyurethane foam tire, which has the characteristics of high functionality, high molecular weight, low unsaturation, and narrow molecular weight distribution.

[0008] Another object of the present invention is to provide a continuous preparation method of polyether polyol for low hysteresis loss polyurethane foam tires. The completely continuous preparation method can be used for large-scale industrial production. The preparation of polyurethane foam tires can reduce the compression permanent deformation of the material, reduce endogenous heat, and improve resilience, thereby solving the industry bottleneck problem that the foam tire cannot rebound or rebounds slowly after being loaded.

[0009] The technical solution adopted by the present invention is:

[0010] The continuous preparation method of polyether polyol for low hysteresis loss polyurethane foam tire comprises the following steps:

[0011] (1) Leakage test and nitrogen replacement are performed on the reaction kettle to make the oxygen content in the kettle less than 50 ppm. The 6-functionality initiator and the catalyst are continuously introduced into the first premixing kettle in proportion. After the liquid level in the kettle reaches 75-95%, the reaction kettle is evacuated at a temperature of 90-120° C. and the vacuum degree is lower than -0.09 MPa. After the water content is measured to be lower than 0.03%, the reaction kettle is transferred to the second premixing kettle for storage;

[0012] (2) adding the dehydrated initiator and catalyst mixture and propylene oxide to the propylene oxide polymerization kettle in proportion, maintaining the reaction temperature at 85-90° C., the reaction pressure at 0.2-0.6 MPa, the material residence time at 1-5 h, and the material overflowing into the ethylene oxide polymerization kettle after being full;

[0013] (3) the overflow material of the propylene oxide polymerization kettle and ethylene oxide are continuously added into the ethylene oxide polymerization kettle in a ratio of (1-9):1, the reaction temperature is maintained at 100-110° C., the reaction pressure is maintained at 0.2-0.6 MPa, the material residence time is maintained at 0.2-2 h, and after the material is full, it overflows into the flash kettle for stripping;

[0014] (4) Continuously add the material from the flash kettle to the adsorption kettle. When the liquid level reaches 70-80%, the two adsorption kettles are switched to each other, and cation exchange resin and adsorbent are added at a temperature of 80-105°C. Stir for 0.5-2h, filter and circulate, and continuously discharge the material to obtain the target polyether polyol.

[0015] The preparation method adopts a mode of 5 groups of reactors connected in series, wherein the first reactor is two premixing reactors connected in series, the second and third reactors are propylene oxide and ethylene oxide polymerization reactors respectively, the fourth reactor is a flash reactor, and the fifth reactor is two adsorption reactors connected in parallel.

[0016] In step (1), the high temperature vacuuming time is 1 to 10 hours, preferably 2 to 6 hours, and the moisture content of the initiator is strictly controlled not to exceed 0.03%. The dehydration has two effects: a. removing methanol from the phosphazene catalyst; b. removing moisture from the initiator. On the one hand, it prevents moisture from participating in the reaction and reducing the functionality of the target product; on the other hand, it prevents residual moisture or small molecular by-products from reacting with ethylene oxide, reducing the product solubility and making the target product turbid, affecting the product quality.

[0017] The hexafunctional initiator is one or more of sorbitol, mannitol, dipentaerythritol, cyclohexanehexol and iohexol. At the same time, a small amount of low-functionality small molecule alcohol or low molecular weight polyether, such as propylene glycol, glycerol and other 2-3 functional alcohol substances or 2-4 functional polyether with molecular weight of 200-5000 can be added according to application requirements.

[0018] The catalyst is a phosphazene catalyst or a mixture of a phosphazene catalyst and an alkali metal catalyst in any proportion, and the amount of the catalyst is 0.01-0.50% of the mass of the target product, preferably 0.05-0.30%. The phosphazene catalyst is prepared by mixing phosphazene salt with potassium methoxide and anhydrous methanol.

[0019] The vacuuming time is 1 to 10 hours, preferably 2 to 6 hours, and the water content of the initiator shall not exceed 0.03%.

[0020] The ethylene oxide content is 10-50% of the total mass of the material.

[0021] The cation exchange resin is one of the hydrogen ion type or sodium ion type strong acid styrene cation exchange resins, and the dosage is 0.1-10% of the total mass of the polyether in the kettle, preferably 0.5-5%.

[0022] The adsorbent is one of acidic or neutral adsorbents, and the amount is 0.05-5%, preferably 0.1-2%, of the total mass of the polyether in the kettle. The adsorbent is an acidic or neutral adsorbent with good potassium removal effect, preferably one or both of CP adsorbent and 700NS adsorbent.

[0023] The polyether polyol for low hysteresis loss polyurethane foam tire is prepared by the above preparation method, and has a number average molecular weight of 10000-14000, a functionality of 5.5-6, a hydroxyl value of 23-33 mgKOH / g, and a viscosity of 1500-2300 mPa·s at 25°C.

[0024] Compared with the prior art, the present invention has the following beneficial effects:

[0025] (1) The present invention adopts a continuous production method to prepare high molecular weight and high activity polyether, which has a short production cycle and high yield. The prepared polyether has a low metal ion content and will not cause adverse effects on downstream applications;

[0026] (2) The polyether polyol prepared by the present invention has the characteristics of high functionality, high molecular weight, high activity and narrow molecular weight distribution. It can be used in the preparation of polyurethane foam tires to reduce the compression permanent deformation of the material, reduce endogenous heat, and improve resilience, thereby solving the industry bottleneck problem that the foam tire cannot rebound or rebounds slowly after being loaded. DETAILED DESCRIPTION

[0027] The present invention is further described below with reference to the embodiments, but they do not limit the implementation of the present invention.

[0028] Example 1

[0029] (1) Leakage test and nitrogen replacement were performed on five groups of reaction kettles. The oxygen content in the kettle was measured to be less than 50 ppm. 748 g of sorbitol and 52 g of phosphazene catalyst were added to the first 1 L premix kettle. The temperature was raised to 90° C. and the vacuum degree was lower than -0.09 MPa for dehydration for 4 h. After the water content was measured to be lower than 0.03%, the mixture was transferred to the second premix kettle for storage and the temperature was maintained at 90° C.;

[0030] (2) continuously adding the dehydrated catalyst and sorbitol mixture and propylene oxide into a propylene oxide polymerization kettle at a mass ratio of 1:54.3, maintaining the reaction temperature at 90° C., the reaction pressure at 0.4 MPa, and the material residence time at 3 h. After the material is full, it overflows into the ethylene oxide polymerization kettle;

[0031] (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide were continuously added into the ethylene oxide polymerization kettle at a mass ratio of 5.7:1, the reaction temperature was maintained at 105° C., the reaction pressure was 0.4 MPa, the material residence time was 1 h, and after the material was full, it overflowed into the flash kettle for stripping;

[0032] (4) The material from the flash kettle was continuously added to the first 3.5L adsorption kettle. After the liquid level reached 80%, the material was switched to the second adsorption kettle. At this time, 20g of hydrogen-type cation exchange resin and 20g of CP adsorbent were added to the first adsorption kettle. The temperature was maintained at 85°C, stirred for 1h, and filtered for 20min before continuously discharging the material to obtain the target polyether polyol 1.

[0033] Example 2

[0034] (1) Before the experiment, five groups of reactors were tested for leaks and replaced with nitrogen. The oxygen content in the reactor was measured to be less than 50 ppm. 762 g of dipentaerythritol and 38 g of phosphazene catalyst were added to the first 1 L premixing reactor. The temperature was raised to 100 ° C. and the vacuum degree was lower than -0.09 MPa for dehydration for 3 h. After the water content was measured to be lower than 0.03%, it was transferred to the second premixing reactor for storage and maintained at 95 ° C.

[0035] (2) continuously adding the dehydrated catalyst, dipentaerythritol mixture and propylene oxide into a propylene oxide polymerization kettle at a mass ratio of 1:39.3, maintaining the reaction temperature at 95° C., the reaction pressure at 0.3 MPa, the material residence time at 4 h, and the material overflowing into the ethylene oxide polymerization kettle after being full;

[0036] (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide were continuously added into the ethylene oxide polymerization kettle at a mass ratio of 5.7:1, the reaction temperature was maintained at 110° C., the reaction pressure was 0.5 MPa, the material residence time was 1 h, and after the material was full, it overflowed into the flash kettle for stripping;

[0037] (4) The material from the flash kettle was continuously added to the first 3.5L adsorption kettle. After the liquid level reached 80%, the material was switched to the second adsorption kettle. At this time, 20g of hydrogen-type cation exchange resin and 20g of CP adsorbent were added to the first adsorption kettle. The temperature was maintained at 85°C, stirred for 1h, and filtered for 20min before continuously discharging the material to obtain the target polyether polyol 2.

[0038] Example 3

[0039] (1) Before the experiment, five groups of reactors were tested for leaks and replaced with nitrogen. The oxygen content in the reactor was measured to be less than 50 ppm. 768 g of sorbitol, 32 g of phosphazene catalyst, and 26.7 g of KOH were added to the first 1 L premixing reactor. The temperature was raised to 110° C. and the vacuum degree was lower than -0.09 MPa for dehydration for 2 h. After the water content was measured to be lower than 0.03%, it was transferred to the second premixing reactor for storage and maintained at 100° C.;

[0040] (2) continuously adding the dehydrated catalyst and sorbitol mixture and propylene oxide into a propylene oxide polymerization kettle at a mass ratio of 1:55.7, maintaining the reaction temperature at 100° C., the reaction pressure at 0.5 MPa, the material residence time at 4 h, and the material overflowing into the ethylene oxide polymerization kettle after being full;

[0041] (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide were continuously added into the ethylene oxide polymerization kettle at a mass ratio of 5.7:1, the reaction temperature was maintained at 105° C., the reaction pressure was 0.3 MPa, the material residence time was 1.5 h, and after the material was full, it overflowed into the flash kettle for stripping;

[0042] (4) The material from the flash kettle was continuously added to the first 3.5L adsorption kettle. After the liquid level reached 80%, the material was switched to the second adsorption kettle. At this time, 20g of hydrogen-type cation exchange resin and 20g of CP adsorbent were added to the first adsorption kettle. The temperature was maintained at 85°C, stirred for 1h, and filtered for 20min before continuously discharging the material to obtain the target polyether polyol 3.

[0043] Example 4

[0044] (1) Before the experiment, five groups of reactors were tested for leaks and replaced with nitrogen. The oxygen content in the reactor was measured to be less than 50 ppm. 708 g of sorbitol, 40 g of glycerol and 52 g of phosphazene catalyst were added to the first 1 L premixing reactor. The temperature was raised to 90° C. and the vacuum degree was lower than -0.09 MPa for dehydration for 2 h. After the water content was measured to be lower than 0.03%, it was transferred to the second premixing reactor for storage and maintained at 90° C.;

[0045] (2) continuously adding the dehydrated catalyst and sorbitol mixture and propylene oxide into a propylene oxide polymerization kettle at a mass ratio of 1:54.3, maintaining the reaction temperature at 90° C., the reaction pressure at 0.4 MPa, and the material residence time at 3 h. After the material is full, it overflows into the ethylene oxide polymerization kettle;

[0046] (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide were continuously added into the ethylene oxide polymerization kettle at a mass ratio of 5.7:1, the reaction temperature was maintained at 105° C., the reaction pressure was 0.4 MPa, the material residence time was 1 h, and after the material was full, it overflowed into the flash kettle for stripping;

[0047] (4) The material from the flash kettle was continuously added to the first 3.5L adsorption kettle. After the liquid level reached 80%, the material was switched to the second adsorption kettle. At this time, 20g of hydrogen-type cation exchange resin and 20g of CP adsorbent were added to the first adsorption kettle. The temperature was maintained at 85°C, stirred for 1h, and filtered for 20min before continuously discharging the material to obtain the target polyether polyol 4.

[0048] Example 5

[0049] (1) Before the experiment, five groups of reactors were tested for leaks and replaced with nitrogen. The oxygen content in the reactor was measured to be less than 50 ppm. 636 g of sorbitol, 136 g of R403 and 48 g of phosphazene catalyst were added to the first 1L premixed reactor. The temperature was raised to 90°C and the vacuum degree was lower than -0.09 MPa for dehydration for 2 h. After the water content was measured to be lower than 0.03%, it was transferred to the second premixed reactor for storage and maintained at 90°C. R403 has a functionality of 4 and a molecular weight of 300, and is a commercially available product of Yinuowei New Materials Co., Ltd.;

[0050] (2) continuously adding the dehydrated catalyst and sorbitol mixture and propylene oxide in a mass ratio of 1:49.6 into a propylene oxide polymerization kettle, maintaining the reaction temperature at 90° C., the reaction pressure at 0.4 MPa, the material residence time at 3 h, and the material overflowing into the ethylene oxide polymerization kettle after being full;

[0051] (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide were continuously added into the ethylene oxide polymerization kettle at a mass ratio of 5.7:1, the reaction temperature was maintained at 105° C., the reaction pressure was 0.4 MPa, the material residence time was 1 h, and after the material was full, it overflowed into the flash kettle for stripping;

[0052] (4) The material from the flash kettle was continuously added to the first 3.5L adsorption kettle. After the liquid level reached 80%, the material was switched to the second adsorption kettle. At this time, 20g of hydrogen-type cation exchange resin and 20g of CP adsorbent were added to the first adsorption kettle. The temperature was maintained at 85°C, stirred for 1h, and filtered for 20min before continuously discharging the material to obtain the target polyether polyol 5.

[0053] Comparative Example 1

[0054] (1) Before the experiment, five groups of reactors were tested for leaks and replaced with nitrogen. The oxygen content in the reactor was measured to be less than 50 ppm. 748 g of sorbitol and 52 g of phosphazene catalyst were added to the first 1L premixing reactor. The reactor was heated to 90°C and dehydrated for 2 hours under the condition of vacuum degree less than -0.09 MPa. After the moisture content was tested to be qualified, the reactor was transferred to the second premixing reactor for storage and the temperature was maintained at 90°C.

[0055] (2) continuously adding the dehydrated catalyst and sorbitol mixture and propylene oxide into a propylene oxide polymerization kettle at a mass ratio of 1:54.3, maintaining the reaction temperature at 90° C., the reaction pressure at 0.4 MPa, and the material residence time at 3 h. After the material is full, it overflows into the ethylene oxide polymerization kettle;

[0056] (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide were continuously added into the ethylene oxide polymerization kettle at a mass ratio of 5.7:1, the reaction temperature was maintained at 105° C., the reaction pressure was 0.4 MPa, the material residence time was 1 h, and after the material was full, it overflowed into the flash kettle for monomer removal. The product after monomer removal was directly discharged to obtain polyether polyol 6.

[0057] The hydroxyl value is tested in accordance with GB / T12008.3-2009 "Plastic polyether polyols Part 3: Determination of hydroxyl value"; the number average molecular weight is determined by gel permeation chromatography (GPC); the potassium ion content is tested in accordance with GB / T12008.3-2009 "Plastic polyether polyols Part 4: Determination of sodium and potassium"; the viscosity is tested in accordance with GB / T12008.3-2009 "Plastic polyether polyols Part 7: Determination of viscosity"; the unsaturation is tested in accordance with GB / T12008.3-2009 "Plastic polyether polyols Part 6: Determination of unsaturation".

[0058] The test results of Examples 1-5 and Comparative Example 1 are shown in Table 1.

[0059] Table 1 Test results of Examples 1-5 and Comparative Example 1

[0060]

[0061] The polyether polyols prepared in Examples 1-5 and Comparative Example 1 are used in foamed tires, wherein the foamed tire formulas of Examples 6-10 correspond to the polyether polyols prepared in Examples 1-5, respectively, and the foamed tire formula of Comparative Example 2 corresponds to the polyether polyol prepared in Comparative Example 1. The polyether polyol in Comparative Example 3 uses INOVOL F3600, a 3-mer 6000 molecular weight polyether, which is a commercially available product of Shandong Yinuowei New Materials Co., Ltd.

[0062] The preparation method of the foamed tire is as follows:

[0063] Component A is polyether polyol, polymer polyol, chain extender, crosslinker, catalyst, foam stabilizer and foaming agent stirred at room temperature for 2 hours and then sealed and stored; component B is polyester polyol modified MDI, NCO content is between 22%. When in use, put components A and B in the corresponding tanks of the low-pressure pouring machine, pour component A and component B into the dynamic tire mold at a mass ratio of 100:65, open the mold for three minutes, trim and exhaust, and you will get a polyurethane foam tire.

[0064] Rebound speed test method: press a weight of 1 ton on the product made by the above method for 24 hours, and record the rebound time of the product; compression permanent deformation is tested in accordance with GB / T7759.1-2015 "Determination of compression permanent deformation of vulcanized rubber or thermoplastic rubber Part 1: At room temperature and high temperature conditions".

[0065] The polyurethane foam tire formulations and performance test results of Examples 6-10 and Comparative Examples 2-3 are shown in Table 2.

[0066] Table 2 Polyurethane foam tire formulations and performance test results of Examples 6-10 and Comparative Examples 2-3

[0067]

[0068] According to the performance test results in Table 2, the polyurethane foam tires obtained in each embodiment under the same conditions have better rebound speed and lower compression permanent deformation than the products obtained in the comparative examples. The polyether polyol prepared by the present invention has high functionality, provides a good degree of crosslinking in the product molecules, and can effectively reduce the displacement and stress relaxation of molecules under long-term stress, maintain a high recovery ability, and reduce compression permanent deformation; the polyether prepared by the present invention has a high molecular weight and a moderate ethylene oxide polymerization segment, providing good elasticity to the product; at the same time, the polyether polyol prepared by the present invention has a low degree of unsaturation and a low metal ion content, and will not have adverse effects on the application.

Claims

1. A continuous preparation method of polyether polyol for low hysteresis loss polyurethane foam tire, characterized in that: The following steps are involved: (1) Test the reactor for leaks and replace with nitrogen to make the oxygen content in the reactor less than 50ppm. First, introduce the 6-functionality initiator and catalyst into the first premixing reactor in proportion. After the liquid level in the reactor reaches 75-95%, evacuate at a temperature of 90-120℃ and the vacuum degree is lower than -0.09MPa. After the water content is lower than 0.03%, transfer it to the second premixing reactor for storage; (2) Add the dehydrated initiator and catalyst mixture and propylene oxide to the propylene oxide polymerization kettle in proportion, maintain the reaction temperature at 85-105°C, the reaction pressure at 0.2-0.6 MPa, the material residence time at 1-5 h, and overflow into the ethylene oxide polymerization kettle after the material is full; (3) The overflow material from the propylene oxide polymerization kettle and ethylene oxide are continuously added into the ethylene oxide polymerization kettle in a ratio of (1-9):1, the reaction temperature is maintained at 100-110°C, the reaction pressure is maintained at 0.2-0.6 MPa, the material residence time is maintained at 0.2-2 h, and after the material is full, it overflows into the flash kettle for stripping; (4) Continuously add the material from the flash reactor to the adsorption reactor. When the liquid level reaches 70-80%, the two adsorption reactors are switched to each other, and cation exchange resin and adsorbent are added at a temperature of 80-105°C. Stir for 0.5-2 hours, filter and cycle, and continuously discharge the material to obtain the target polyether polyol. The preparation method adopts a mode of 5 groups of reactors connected in series, wherein the first reactor is two premixing reactors connected in series, the second and third reactors are propylene oxide and ethylene oxide polymerization reactors respectively, the fourth reactor is a flash reactor, and the fifth reactor is two adsorption reactors connected in parallel; The hexafunctional initiator is one or more of sorbitol, mannitol, dipentaerythritol, cyclohexanehexol, and iohexol; The catalyst is a phosphazene catalyst or a mixture of a phosphazene catalyst and an alkali metal catalyst in any proportion, and the amount of the catalyst is 0.01-0.50% of the mass of the target product; The cation exchange resin is one of the strong acid styrene cation exchange resins of hydrogen ion type or sodium ion type, and the amount used is 0.1-10% of the total mass of the polyether in the kettle; The adsorbent is one of an acidic or neutral adsorbent, and the amount used is 0.05-5% of the total mass of the polyether in the kettle.

2. The continuous preparation method of polyether polyol for low hysteresis loss polyurethane foam tire according to claim 1, characterized in that: The vacuuming time is 1 to 10 hours, and the moisture content of the initiator shall not exceed 0.03%.

3. The continuous preparation method of polyether polyol for low hysteresis loss polyurethane foam tire according to claim 1, characterized in that: The ethylene oxide content is 10-50% of the total mass of the material.

4. A polyether polyol for low hysteresis loss polyurethane foam tire, characterized in that: The invention is prepared by the continuous preparation method of polyether polyol for low hysteresis loss polyurethane foam tire according to any one of claims 1 to 3.

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