Process for the preparation of a semi-bio-based nylon 610 / 6t copolymer and product

Abstract

This invention belongs to the field of polymer copolymerization and modification technology, and discloses a method for preparing a semi-bio-based nylon 610 / 6T copolymer and the resulting product. The product comprises hexamethylenediamine, sebacic acid, and terephthalic acid, and is prepared through a salt-forming stage and a polymerization stage. The polymer preparation method provided by this patent is simple, uses environmentally friendly solvents, has a controllable production process, and is easy to industrialize. The novel semi-bio-based nylon 610 / 6T copolymer prepared exhibits improved strength and heat resistance, demonstrating excellent overall performance.

Description

Technical Field

[0001] This invention belongs to the field of polymer copolymerization and modification technology, specifically relating to a method for preparing a semi-biological nylon 610 / 6T copolymer and its product. Background Technology

[0002] Nylon 610 is an environmentally friendly bio-based nylon with a bio-based content of 64% (by mass) produced through condensation polymerization of hexamethylenediamine and bio-based sebacic acid. It features green, environmentally friendly, and renewable characteristics. The amide groups have a low density, giving it not only the good mechanical properties and abrasion resistance of nylon, but also good flexibility, low water absorption, good dimensional stability, excellent dielectric properties, and low density. It is widely used in the automotive, electronics, aerospace, hardware, food, and household products industries.

[0003] While Nylon 610 has many advantages, it also suffers from drawbacks such as low strength and poor heat resistance. Patent application number 201310654178.3 discloses "A semi-aromatic nylon 610T material with controllable melting point and its preparation method." This patent showcases the advantages of semi-aromatic nylon 610T material, but the tensile strength and melting point improvement of the prepared nylon 610T material are limited, and the synthesis process involves catalysts and nucleating agents, making it relatively cumbersome. Furthermore, this patent fails to provide key control indicators from a production technology perspective; the product indicator only reflects the melting point, which has certain limitations.

[0004] Patent application number 201710449761.9 discloses "a low coefficient of linear expansion polyphenylene ether / nylon 610 alloy material and its preparation method," comprising polyphenylene ether, polystyrene, nylon 610 resin, hydrogenated styrene-butadiene copolymer grafted with glycidyl methacrylate (SEBS-GMA), styrene-maleic anhydride block copolymer (SMA), dispersant, and composite filler. The alloy material is formed through stirring, dispersion, copolymerization, and granulation. The product exhibits good processability, excellent mechanical properties, low anisotropy, and outstanding dimensional stability, with a coefficient of linear expansion reaching the level of metallic materials such as aluminum alloys. It can replace metallic materials in the manufacture of water pump impellers and pump bodies, turbocharger turbines, and volutes. The raw materials for this invention are widely available and suitable for industrial production. However, this material relies on metallic materials to form an alloy, making preparation difficult and inconsistent with the concept of sustainable development. Summary of the Invention

[0005] To overcome the shortcomings of the prior art, the present invention provides a method for preparing a semi-biological nylon 610 / 6T copolymer and a product thereof. By controlling the reaction conditions to change the copolymer composition of 610 / 6T, the strength and high temperature resistance of nylon 610 / 6T are improved.

[0006] The above-mentioned objective of the present invention is achieved through the following technical solution: a method for preparing a semi-biological nylon 610 / 6T copolymer, comprising two stages: salt formation and polymerization;

[0007] 1. Salt formation stage: Deionized water is added to the reaction vessel, followed by hexamethylenediamine and mixed acid, and nitrogen gas is introduced. After the feeding is completed, the stirring is turned on to carry out the salt formation reaction. The salt formation reaction ends when the pH of the salt solution reaches the specified range, and the salt formation is confirmed to be complete.

[0008] 2. Polymerization stage: Set the temperature inside the reactor and concentrate the nylon 610 / 6T salt solution. When the concentration of the salt solution inside the reactor is within the specified range, the concentration step ends. Then, gradually increase the temperature and pressure for the reaction. After a certain time, release the pressure inside the reactor to atmospheric pressure, then evacuate the polymerization reactor and gradually reduce the stirring speed. When the speed drops to a certain point, the reaction reaches its endpoint. After introducing nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, discharge the material to obtain the novel semi-bio-based nylon 610 / 6T copolymer.

[0009] Furthermore, in the salt formation stage, the mixed acid consists of sebacic acid and terephthalic acid, with a molar ratio of sebacic acid to terephthalic acid of (9-6):(1-4).

[0010] Furthermore, the molar ratio of hexamethylenediamine to mixed acid added in the salt-forming stage is (1.0-1.25):1, and the amount of deionized water added is calculated based on a salt solution concentration of 30-50 wt% (more preferably 38-40 wt%) after salt formation.

[0011] Furthermore, the stirring rate during the salt formation stage is 90 rpm, and the temperature inside the reactor is 50–80°C (more preferably 72–75°C).

[0012] Furthermore, the salt formation stage has a salt formation reaction endpoint of pH 7.0–8.0 and a reaction time of 2–3 hours.

[0013] Furthermore, the concentration of the salt solution in the reactor during the polymerization stage is specified to be in the range of 80–85 wt%.

[0014] Furthermore, the vacuuming pressure during the polymerization stage is < -50 kPa, and the vacuuming time is 0.5 to 1 hour.

[0015] Furthermore, the reaction endpoint is reached when the stirring speed drops to 30 rpm during the polymerization stage.

[0016] Furthermore, the aggregation stage steps are specifically as follows:

[0017] ① Set the temperature inside the reactor to 120-150℃ and concentrate the Nylon 610 / 6T salt solution. The concentration endpoint is determined by calculating the amount of water discharged. When the concentration of the salt solution inside the reactor is 80-85wt% after calculation, the concentration step is completed. The concentration time is 1-5 hours.

[0018] ② Set the temperature inside the reactor to 200-230℃, the reaction time to 0.5-3h, and the pressure inside the reactor to 1.4MPa-1.75MPa;

[0019] ③ Set the temperature inside the reactor to 250-255℃, the reaction time to 0.5-3h, and the pressure inside the reactor to 1.70-1.80MPa;

[0020] ④ Set the temperature inside the reactor to 265-270℃, open the pressure relief valve, and slowly release the pressure inside the reactor to atmospheric pressure. The pressure relief time should be controlled between 0.5 and 2 hours.

[0021] ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor. During this process, as the viscosity of the polymer continues to increase, the stirring speed gradually decreases from 90 rpm. When the stirring speed drops to 30 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain the novel semi-bio-based nylon 610 / 6T copolymer.

[0022] Another object of the present invention is to protect a semi-biological nylon 610 / 6T copolymer comprising hexamethylenediamine, sebacic acid and terephthalic acid, wherein the molar ratio of sebacic acid and terephthalic acid is (9-6):(1-4), and the molar ratio of hexamethylenediamine to the molar ratio of sebacic acid + terephthalic acid is (1.0-1.25):1.

[0023] The novel semi-biological nylon 610 / 6T copolymer prepared in this invention has the following reaction equation:

[0024]

[0025] The beneficial effects of this invention compared with the prior art are: the polymer preparation method provided by this patent is simple, the solvent is green and environmentally friendly, the production process is controllable, and it is easy to industrialize. The prepared novel semi-biological nylon 610 / 6T copolymer has improved strength and heat resistance and has excellent comprehensive performance. Attached Figure Description

[0026] The present invention will be further described below with reference to the accompanying drawings and specific embodiments.

[0027] Figure 1 These are the infrared spectra of the samples in the embodiments and comparative examples of this invention;

[0028] Figure 2 This is the 1H NMR spectrum of the sample in the embodiments and comparative examples of this invention. Detailed Implementation

[0029] The present invention is described in detail below through specific embodiments, but this does not limit the scope of protection of the present invention. Unless otherwise specified, the experimental methods used in the present invention are all conventional methods, and the experimental equipment, materials, reagents, etc. used can all be obtained commercially.

[0030] Example 1

[0031] Salt formation stage:

[0032] Take 464.84 g of 4 mol hexamethylenediamine and 794.55 g of 4 mol mixed acid (sebacic acid: terephthalic acid = 9:1). Calculate the final salt solution concentration as 40 wt%, and add 1800 g of deionized water. Add the deionized water, hexamethylenediamine, and mixed acid raw materials sequentially into the polymerization reactor, and purge with nitrogen. After the materials are added, start stirring and slowly adjust the stirring speed to 90 rpm. Turn on the heating switch and set the reactor temperature to 75℃ to initiate the salt formation reaction, which takes approximately 2–3 hours. After the salt formation reaction begins, sample the salt solution every 30 minutes and measure the pH until the pH of the salt solution is within the range of 7.0–8.0, at which point the salt formation reaction endpoint is determined.

[0033] Aggregation phase:

[0034] ① Set the temperature inside the reactor to 120℃ and the jacket temperature to 180℃, and carry out water drainage concentration. The drainage volume is about 90% of the total output water volume, and the concentration time is 2 to 3 hours.

[0035] ② Set the temperature inside the reactor to 200-230℃, the jacket temperature to 260℃, the reaction time to 0.5-1h, and the pressure to approximately 1.4MPa-1.75MPa.

[0036] ③ Set the temperature inside the reactor to 250℃, the jacket temperature to 310℃, the reaction time to 40min, and the pressure to 1.75MPa.

[0037] ④ Set the temperature inside the vessel to 265℃ and the jacket temperature to 330℃, and open the pressure relief valve to slowly release the pressure inside the vessel to atmospheric pressure.

[0038] ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor to a pressure < -50 kPa, in order to increase the polymer viscosity. The evacuation time is approximately 0.5 to 1 hour. During this process, as the polymer viscosity continuously increases, the stirring speed is gradually reduced from 90 rpm. When the stirring speed drops to 30 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain Nylon 610 / 6T-1# resin.

[0039] Example 2

[0040] Salt formation stage:

[0041] Take 464.84 g of 4 mol hexamethylenediamine and 780.1 g of 4 mol mixed acid (sebacic acid mol: terephthalic acid mol = 8:2). Calculate the final salt solution concentration as 40 wt%, and add 1800 g of deionized water. Add the deionized water, hexamethylenediamine, and mixed acid raw materials sequentially into the polymerization reactor, and purge with nitrogen. After the materials are added, start stirring and slowly adjust the stirring speed to 90 rpm. Turn on the heating switch and set the reactor temperature to 75℃ to initiate the salt formation reaction, which takes approximately 2–3 hours. After the salt formation reaction begins, sample the salt solution every 30 minutes and measure the pH until the pH of the salt solution is within the range of 7.0–8.0, at which point the salt formation reaction endpoint is determined.

[0042] Aggregation phase:

[0043] ① Set the temperature inside the reactor to 120℃ and the jacket temperature to 180℃, and carry out water drainage concentration. The drainage volume is about 90% of the total output water volume, and the concentration time is 2 to 3 hours.

[0044] ② Set the temperature inside the reactor to 200-230℃, the jacket temperature to 260℃, the reaction time to 0.5-1h, and the pressure to approximately 1.4MPa-1.75MPa.

[0045] ③ Set the temperature inside the reactor to 250℃, the jacket temperature to 310℃, the reaction time to 40min, and the pressure to 1.75MPa.

[0046] ④ Set the temperature inside the vessel to 265℃ and the jacket temperature to 330℃, and open the pressure relief valve to slowly release the pressure inside the vessel to atmospheric pressure.

[0047] ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor to a pressure < -50 kPa, in order to increase the polymer viscosity. The evacuation time is approximately 0.5 to 1 hour. During this process, as the polymer viscosity continuously increases, the stirring speed is gradually reduced from 90 rpm. When the stirring speed drops to 30 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain Nylon 610 / 6T-2# resin.

[0048] Example 3

[0049] Salt formation stage:

[0050] Take 464.84 g of 4 mol hexamethylenediamine and 765.66 g of 4 mol mixed acid (sebacic acid: terephthalic acid = 7:3). Calculate the final salt solution concentration as 40 wt%, and add 1800 g of deionized water. Add the deionized water, hexamethylenediamine, and mixed acid raw materials sequentially into the polymerization reactor, and purge with nitrogen. After the materials are added, start stirring and slowly adjust the stirring speed to 90 rpm. Turn on the heating switch and set the reactor temperature to 75℃ to initiate the salt formation reaction, which takes approximately 2–3 hours. After the salt formation reaction begins, sample the salt solution every 30 minutes and measure the pH until the pH of the salt solution is within the range of 7.0–8.0, at which point the salt formation reaction endpoint is determined.

[0051] Aggregation phase:

[0052] ① Set the temperature inside the reactor to 120℃ and the jacket temperature to 180℃, and carry out water drainage concentration. The drainage volume is about 90% of the total output water volume, and the concentration time is 2 to 3 hours.

[0053] ② Set the temperature inside the reactor to 200-230℃, the jacket temperature to 260℃, the reaction time to 0.5-1h, and the pressure to approximately 1.4MPa-1.75MPa.

[0054] ③ Set the temperature inside the reactor to 250℃, the jacket temperature to 310℃, the reaction time to 40min, and the pressure to 1.75MPa.

[0055] ④ Set the temperature inside the vessel to 265℃ and the jacket temperature to 330℃, and open the pressure relief valve to slowly release the pressure inside the vessel to atmospheric pressure.

[0056] ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor to a pressure < -50 kPa, in order to increase the polymer viscosity. The evacuation time is approximately 0.5 to 1 hour. During this process, as the polymer viscosity continuously increases, the stirring speed is gradually reduced from 90 rpm. When the stirring speed drops to 30 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain Nylon 610 / 6T-3# resin.

[0057] Example 4

[0058] Salt formation stage:

[0059] Take 464.84 g of 4 mol hexamethylenediamine and 751.21 g of 4 mol mixed acid (sebacic acid: terephthalic acid = 6:4). Calculate the final salt solution concentration as 40 wt%, and add 1800 g of deionized water. Add the deionized water, hexamethylenediamine, and mixed acid raw materials sequentially to the polymerization reactor, and purge with nitrogen. After the materials are added, start stirring and slowly adjust the stirring speed to 90 rpm. Turn on the heating switch and set the reactor temperature to 75℃ to initiate the salt formation reaction, which takes approximately 2–3 hours. After the salt formation reaction begins, sample the salt solution every 30 minutes and measure the pH until the pH of the salt solution is within the range of 7.0–8.0, at which point the salt formation reaction endpoint is determined.

[0060] Aggregation phase:

[0061] ① Set the temperature inside the reactor to 120℃ and the jacket temperature to 180℃, and carry out water drainage concentration. The drainage volume is about 90% of the total output water volume, and the concentration time is 2 to 3 hours.

[0062] ② Set the temperature inside the reactor to 200-230℃, the jacket temperature to 260℃, the reaction time to 0.5-1h, and the pressure to approximately 1.4MPa-1.75MPa.

[0063] ③ Set the temperature inside the reactor to 250℃, the jacket temperature to 310℃, the reaction time to 40min, and the pressure to 1.75MPa.

[0064] ④ Set the temperature inside the vessel to 265℃ and the jacket temperature to 330℃, and open the pressure relief valve to slowly release the pressure inside the vessel to atmospheric pressure.

[0065] ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor to a pressure < -50 kPa, in order to increase the polymer viscosity. The evacuation time is approximately 0.5 to 1 hour. During this process, as the polymer viscosity continuously increases, the stirring speed is gradually reduced from 90 rpm. When the stirring speed drops to 30 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain Nylon 610 / 6T-4# resin.

[0066] Comparative Example 1

[0067] Salt formation stage:

[0068] Sebacic acid and hexamethylenediamine were weighed in equimolar amounts. First, 464.84 g of 4 mol hexamethylenediamine was taken, followed by 809 g of 4 mol sebacic acid. Based on a final salt solution concentration of 40 wt%, 1800 g of deionized water was added. The deionized water, hexamethylenediamine, and sebacic acid were then successively added to the polymerization reactor, and nitrogen gas was introduced. After the addition was complete, the stirring switch was turned on and the stirring speed was slowly adjusted to 90 rpm. The heating switch was turned on and the reactor temperature was set to 75°C to initiate the salt formation reaction. The final pH value of the salt formation reaction should be between 7.0 and 8.0. Salt formation was confirmed when equilibrium was reached. The reaction time was 2–3 hours.

[0069] Aggregation phase:

[0070] ① Set the temperature inside the reactor to 120℃ and the jacket temperature to 180℃, and carry out water drainage concentration. The drainage volume is about 90% of the total output water volume, and the concentration time is 2 to 3 hours.

[0071] ② Set the temperature inside the reactor to 200-230℃, the jacket temperature to 260℃, the reaction time to 0.5-1h, and the pressure to approximately 1.4MPa-1.75MPa.

[0072] ③ Set the temperature inside the reactor to 250℃, the jacket temperature to 310℃, the reaction time to 40min, and the pressure to 1.75MPa.

[0073] ④ Set the temperature inside the vessel to 265℃ and the jacket temperature to 330℃, and open the pressure relief valve to slowly release the pressure inside the vessel to atmospheric pressure.

[0074] ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor to a pressure < -50 kPa, in order to increase the polymer viscosity. The evacuation time is approximately 0.5 to 1 hour. During this process, as the polymer viscosity continuously increases, the stirring speed is gradually reduced from 90 rpm. When the stirring speed drops to 30 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain Nylon 610 resin.

[0075] The resins described in Examples 1-4 and Comparative Example 1 were subjected to the following performance tests:

[0076] (1) Infrared spectroscopy (FTIR) test: Fourier transform infrared spectrometer was used with a scanning wavenumber of 4000-500 cm⁻¹. -1 The sample is tested after scanning within the range to eliminate the influence of other substances in the air, such as... Figure 1 As shown.

[0077] (2) Nuclear magnetic resonance hydrogen spectrum (NMR) 1 ¹H NMR test: Deuterated concentrated sulfuric acid was used as the solvent, and its residual solvent peak was used as the internal standard. 1 The chemical shift at 7.88 in the 1H-NMR spectrum is the chemical shift peak of H on the benzene ring in the 6T structural unit. This shift gradually increases with the increase of the PTA feed ratio. Figure 2 As shown.

[0078] (3) Thermal performance testing: The melting temperature was tested using a differential scanning calorimeter at a heating rate of 10℃ / min, reaching 345℃ and holding for 5 min to eliminate thermal history. Thermogravimetric analysis was performed using a simultaneous thermal analyzer, with the temperature increasing from 30℃ to 700℃ at a heating rate of 20℃ / min under a nitrogen atmosphere, as shown in Table 1.

[0079] Table 1 Thermal performance data of the examples and comparative examples

[0080] sample <![CDATA[T m / ℃]]> <![CDATA[T 5％ / ℃]]> Example 1 236.63 418.7 Example 2 241.34 424.1 Example 3 252.29 420.4 Example 4 261.95 423.5 Comparative Example 226.03 414.8

[0081] (4) Mechanical property testing: Electronic universal testing machine and impact testing machine were used, and the tests were conducted in accordance with the provisions of GB / T 1040.2 Determination of tensile properties of plastics, GB / T 9341 Determination of bending properties of plastics, and GB / T 1843 Determination of impact properties of plastic cantilever beams, as shown in Table 2.

[0082] Table 2 Mechanical property test data for examples and comparative examples

[0083]

[0084] Analysis of the examples and comparative examples using infrared and nuclear magnetic resonance methods shows that 1500 cm⁻¹ -1 The characteristic absorption peak of the stretching vibration of the benzene ring skeleton at position 865 cm⁻¹ -1 The absorption peak of the in-plane bending vibration of the benzene ring CH is observed, and the content of PA610 / 6T in the copolymer increases with the increase of the PTA ratio.

[0085] Through thermal performance tests of the examples and comparative examples, the heat resistance of the prepared nylon 610 / 6T resin was improved compared with that of the comparative example.

[0086] Through thermal performance tests of the examples and comparative examples, the mechanical properties of the prepared nylon 610 / 6T resin were significantly improved compared with those of the comparative example.

[0087] The embodiments described above are merely preferred embodiments of the present invention, and not all feasible embodiments of the present invention. Any obvious modifications made by those skilled in the art without departing from the principles and spirit of the present invention should be considered to be included within the scope of protection of the claims of the present invention.

Claims

1. A method for preparing a semi-biological nylon 610 / 6T copolymer, characterized in that, It includes two stages: salt formation and polymerization; S1. Salt formation stage: Deionized water is added to the reaction vessel, followed by hexamethylenediamine and mixed acid, and nitrogen gas is introduced. After the feeding is completed, the stirring is turned on to carry out the salt formation reaction. The salt formation reaction ends when the pH of the salt solution reaches the specified range. Salt formation is then confirmed to be complete. S2. Polymerization stage: Set the temperature inside the reactor and concentrate the nylon 610 / 6T salt solution. When the concentration of the salt solution inside the reactor is within the specified range, the concentration step ends. Then, gradually increase the temperature and pressure for the reaction. After a certain time, release the pressure inside the reactor to atmospheric pressure, then evacuate the polymerization reactor and gradually reduce the stirring speed. When the speed drops to a certain speed, the reaction reaches the endpoint. After nitrogen is introduced to restore the pressure inside the reactor to atmospheric pressure, the product is discharged to obtain the novel semi-bio-based nylon 610 / 6T copolymer.

2. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, In the salt formation stage, the mixed acid consists of sebacic acid and terephthalic acid, with a molar ratio of sebacic acid to terephthalic acid of (9-6):(1-4).

3. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The molar ratio of hexamethylenediamine to mixed acid added during the salt formation stage is (1.0-1.25):1, and the amount of deionized water added is calculated based on a salt solution concentration of 30-50 wt% after salt formation.

4. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The stirring rate during the salt formation stage is 60–100 rpm, and the temperature inside the reactor is 50–80°C.

5. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The salt-forming stage ends at pH 7.0–8.0, with a reaction time of 2–3 hours.

6. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The specified range for the concentration of the salt solution in the reactor during the polymerization stage is 80–85 wt%.

7. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The vacuuming pressure during the polymerization stage is < -50 kPa, and the vacuuming time is 0.5 to 1 hour.

8. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The reaction reaches its endpoint when the stirring speed drops to 10-50 rpm during the polymerization stage.

9. The method for preparing the semi-biological nylon 610 / 6T copolymer according to claim 1, characterized in that, The specific steps of the aggregation phase are as follows: ① Set the temperature inside the reactor to 120-150℃ and concentrate the Nylon 610 / 6T salt solution. The concentration endpoint is determined by calculating the amount of water discharged. When the concentration of the salt solution inside the reactor is 80-85wt% after calculation, the concentration step is completed. The concentration time is 1-5 hours. ② Set the temperature inside the reactor to 200-230℃, the reaction time to 0.5-3h, and the pressure inside the reactor to 1.4MPa-1.75MPa; ③ Set the temperature inside the reactor to 250-255℃, the reaction time to 0.5-3h, and the pressure inside the reactor to 1.70-1.80MPa; ④ Set the temperature inside the reactor to 265-270℃, open the pressure relief valve, and slowly release the pressure inside the reactor to atmospheric pressure. The pressure relief time should be controlled between 0.5 and 2 hours. ⑤ After the pressure inside the reactor is reduced to atmospheric pressure, close the pressure relief valve and the pressure gauge valve, and start the vacuum pump to evacuate the polymerization reactor. During this process, as the viscosity of the polymer continues to increase, the stirring speed gradually decreases from 60 to 100 rpm. When the stirring speed drops to 10 to 50 rpm, the reaction endpoint is reached. Turn off the vacuum pump, introduce nitrogen gas to restore the pressure inside the reactor to atmospheric pressure, and then discharge the material to obtain the novel semi-bio-based nylon 610 / 6T copolymer.

10. A semi-biological nylon 610 / 6T copolymer, characterized in that, The components include hexamethylenediamine, sebacic acid and terephthalic acid, wherein the molar ratio of sebacic acid and terephthalic acid is (9-6):(1-4), and the molar ratio of hexamethylenediamine to the molar ratio of sebacic acid + terephthalic acid is (1.0-1.25):1.

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