WO2020134735A1 - 半芳香族聚酰胺树脂及其制备方法 - Google Patents

半芳香族聚酰胺树脂及其制备方法 Download PDF

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WO2020134735A1
WO2020134735A1 PCT/CN2019/119738 CN2019119738W WO2020134735A1 WO 2020134735 A1 WO2020134735 A1 WO 2020134735A1 CN 2019119738 W CN2019119738 W CN 2019119738W WO 2020134735 A1 WO2020134735 A1 WO 2020134735A1
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acid
semi
aromatic polyamide
reaction
dibasic acid
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PCT/CN2019/119738
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English (en)
French (fr)
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陈志荣
尹红
邓杭军
周贵阳
朱丹琪
吴笑笑
洪文刚
邱贵生
李其川
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浙江大学
浙江新和成特种材料有限公司
浙江新和成股份有限公司
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Priority to US17/416,587 priority Critical patent/US20220025120A1/en
Priority to JP2021536345A priority patent/JP7186988B2/ja
Publication of WO2020134735A1 publication Critical patent/WO2020134735A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
    • C08G69/48—Polymers modified by chemical after-treatment
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
    • C08G69/02—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids
    • C08G69/26—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids derived from polyamines and polycarboxylic acids
    • C08G69/265—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids derived from polyamines and polycarboxylic acids from at least two different diamines or at least two different dicarboxylic acids
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
    • C08G69/02—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids
    • C08G69/26—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids derived from polyamines and polycarboxylic acids
    • C08G69/28—Preparatory processes
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L77/00—Compositions of polyamides obtained by reactions forming a carboxylic amide link in the main chain; Compositions of derivatives of such polymers
    • C08L77/06—Polyamides derived from polyamines and polycarboxylic acids

Definitions

  • the invention relates to a semi-aromatic polyamide resin and a preparation method thereof, in particular to provide a thermally stable semi-aromatic polyamide resin added with a specific blocking agent and a preparation method thereof, which can be applied to automobile parts and electrical appliances Parts, especially LED boards.
  • Polyamide is also known as nylon (Nylon), which refers to the general name of the polymer containing amide group (-NHCO-) in the repeating group of the main chain of the macromolecule; Variety.
  • Aliphatic polyamides such as nylon 6, nylon 66, etc., although their comprehensive performance is good, but the thermal performance can not meet the requirements of high temperature working environment, which limits its application in high-tech fields.
  • the semi-aromatic polyamide has an aromatic ring introduced into the polyamide molecular chain. Compared with the general PA6 and PA66, it has greatly improved heat resistance, mechanical properties, water absorption, and chemical resistance.
  • Semi-aromatic polyamides mainly have the following characteristics: (1) High glass transition temperature and good heat resistance; (2) Good heat and oxygen aging resistance; (3) Good electrical insulation properties; (4 ) The water absorption rate is small, and the dimensional stability of the product is good. Therefore, with the rapid development of modern high technology, the application of semi-aromatic polyamides is becoming more and more extensive. Semi-aromatic polyamides are widely used in electrical, electronic parts, and automotive parts.
  • the peripheral parts of the engine room ie, the components under the hood
  • a high temperature environment above 120°C
  • the polymer used should have sufficient heat resistance and can withstand reflow soldering without blistering, and should have high UV light stability and thermal stability, and good long-term stability under operating conditions.
  • Document EP0827976 reports a partially aromatic polyamide composition with improved thermal stability.
  • the thermal stabilizer is a mixture of an alkali metal halide and a copper (I) halide.
  • the weight ratio is most preferably about 8:1 to about 10:1, based on
  • the amount of polyamide containing copper stabilizers is from 50 to about 1000 ppm.
  • the 220°C heat aging test shows that the time required for the loss of 50% of the mechanical strength by adding a copper-containing heat stabilizer is 2 to 3 times longer than when no heat stabilizer is added.
  • Document CN107325548A reported that adding no more than 2% by mass of monovalent or divalent copper compounds, copper salts of aliphatic carboxylic acids, secondary aromatic amines, and sterically hindered phenols or mixtures of several of them as heat stabilizers to increase the heat of the resin stability.
  • Documents WO2018049808A1 and CN103694693A report the use of hindered phenols, hydroquinones, phosphites and substitutions, copper halides, iodine compounds, etc. as heat stabilizers for PA66 polyamide compositions to improve the thermal stability and resistance of PA66 compositions Aging.
  • Document WO2005/007727A1 reported that adding elemental iron thermal stabilizers to polyamides can show better retention of mechanical properties at high temperatures.
  • Document CN103890040A proposes to modify the polyamide resin by adding a metal oxide so that the polyamide composition maintains high mechanical strength, long-term oxidation resistance, and high heat resistance, and is mainly used in LED products.
  • Polyamide oligomers are composed of different structures and have non-reactive phenol or amine end groups with a molecular weight between 800 and 5000 g/mol , It is often used in blending with polyamide resin to improve the fluidity, viscosity stability and hydrolysis resistance of polyamide resin.
  • the catalysts used in the preparation of most polyamide resins are inorganic phosphorous acid, hypophosphorous acid and their metal salt compounds.
  • the thermal stability and aging resistance of polyamides are improved by the addition of heat stabilizers and antioxidants.
  • catalysts, heat stabilizers, antioxidants, etc. are likely to migrate, and long-term anti-oxidation and thermal stability cannot be achieved.
  • the added heat stabilizer contains heavy metal salts, which are potentially harmful to the environment.
  • the object of the present invention is to provide a semi-aromatic polyamide that can maintain long-term thermal stability and can avoid additives such as heat stabilizers and antioxidants from occurring during use Migration, at the same time, can also avoid the use of thermal stability additives that are potentially harmful to the environment.
  • Another object of the present invention is to provide a method for preparing a semi-aromatic polyamide capable of maintaining long-term thermal stability without migration of heat stabilizers, antioxidants, etc., and a resin composition containing the semi-aromatic polyamide and Its products.
  • the inventor has found through repeated research that the above problems can be solved by adding a specific end-capping agent during the polymerization reaction for preparing the semi-aromatic polyamide.
  • the blocking agent includes a reactive group-containing condensation catalyst represented by the following formula (I) and a reactive group-containing hindered phenolic antioxidant blocking agent represented by the formula (II).
  • the catalyst can not only participate in the polymerization process and increase the polymerization rate, but also can itself react with amine end groups. After the reaction is completed, it becomes a polymer-containing low-valent phosphine end group, and such a structure can Brings improved antioxidant effect; secondly, hindered phenolic antioxidants containing reactive groups can also react with amine end groups, so that the antioxidants can be evenly distributed and fixed in the polymer in an in-situ reaction, avoiding heat A phenomenon of failure due to migration to the surface.
  • the above-mentioned blocking agent of the present invention can maintain the long-term thermal stability of the polymer and can also avoid the problem of migration of the traditional small molecule additives (heat stabilizers, antioxidants, etc.) out of the resin matrix during processing and use.
  • the present invention first provides a semi-aromatic polyamide having structural units derived from a diamine, a dibasic acid, and a monobasic acid, and having a formula derived from the following formula (I) and formula (II )'S end cap structure,
  • the formula (I) is selected from the compounds represented by the following formula (I-1) and/or formula (I-2):
  • R 1 is a carboxyl group or a C 1 -C 10 alkyl group substituted with a carboxyl group, preferably a C 1 -C 4 alkyl group substituted with a carboxyl group
  • R 2 is a C 1 -C 4 alkyl group or H, preferably H
  • R 3 is selected from C 6 -C 9 aromatic groups or H, preferably C 6 -C 8 aromatic groups
  • M n+ is selected from +1, +2 valent metal cations
  • R 4 is selected from C 1 -C 10 alkyl groups, preferably C 1 -C 4 alkyl groups.
  • the semi-aromatic polyamide according to any one of [1] to [6], wherein the dibasic acid includes one of an aromatic dibasic acid and an optional aliphatic dibasic acid or In various types, the molar ratio of the aromatic dibasic acid and the aliphatic dibasic acid is 100:0 to 50:50, preferably 80:20 to 55:45.
  • the present invention also provides a method for preparing a semi-aromatic polyamide, the method using diamine, dibasic acid and monobasic acid as the main raw materials, and carried out in the presence of a blocking agent Polymerization, the end-capping agent has the structure of the following formula (I) and formula (II),
  • the formula (I) is selected from the compounds represented by the following formula (I-1) and/or formula (I-2):
  • R 1 is a carboxyl group or a C 1 -C 10 alkyl group substituted with a carboxyl group, preferably a C 1 -C 4 alkyl group substituted with a carboxyl group
  • R 2 is a C 1 -C 4 alkyl group or H, preferably H
  • R 3 is selected from C 6 -C 9 aromatic groups or H, preferably C 6 -C 8 aromatic groups
  • M n+ is selected from +1, +2 valent metal cations
  • R 4 is selected from C 1 -C 10 alkyl groups, preferably C 1 -C 4 alkyl groups.
  • Salt formation reaction the initial feeding of diamine and dibasic acid according to the amine/acid molar ratio is less than 1 to form a salt solution with water;
  • Prepolymerization reaction adjust the amine/acid molar ratio in the reaction system to greater than 1.03 with diamine, monobasic acid and end-capping agent, perform prepolymerization reaction to obtain prepolymerization reaction liquid;
  • Polycondensation reaction Use a pre-polymerization reaction solution for polycondensation reaction.
  • the molar ratio of amine acid initially charged is 0.90 to 0.99, preferably 0.92 to 0.98.
  • the salt-forming reaction further comprises: detecting the composition of the dibasic acid in the salt solution, by adding an aromatic dibasic acid and/or Aliphatic dibasic acid to maintain the composition/content of dibasic acid stable; the prepolymerization reaction also includes the detection of the composition in the prepolymerization reaction system, and the detection is performed by online Raman spectroscopy.
  • the present invention also provides a resin composition comprising:
  • the present invention also provides an article prepared from the composition according to [17].
  • the semi-aromatic polyamide resin of the present invention contains a specific blocking agent or is prepared by a specific blocking agent.
  • the blocking agent includes a reactive group-containing condensation catalyst represented by formula (I) and a reactive group-containing hindered phenolic antioxidant blocking agent represented by formula (II).
  • the above catalyst can not only participate in the polymerization process and increase the polymerization rate, but also can perform in-situ end-capping reaction with the amine end groups.
  • the reaction After the reaction is completed, it becomes a low-valent phosphine-containing end group of the polymer, which has a certain antioxidant effect;
  • the hindered phenolic antioxidants containing reactive groups can also perform in-situ end-capping reaction with amine end groups, so that the antioxidants can be evenly distributed and fixed in the polymer, avoiding the phenomenon of migration to the surface and failure when heated. Therefore, the special end-capping agent of the present invention can maintain the long-term thermal stability of the polymer.
  • the present invention can effectively control the reaction of the polymer with amine end groups when heated by controlling the content of the carboxyl functional group of the polymer, thereby improving the stability of the viscosity and molecular weight of the polymer when heated.
  • Figure 1 shows the normalized Raman spectra of various nylon salts (600 to 1200 cm -1 ).
  • Figure 2 shows the normalized Raman spectra of various nylon salts (1200-1800 cm -1 ).
  • Figure 3 shows a flow chart for the preparation of a polyamide of the present invention.
  • Figure 4 shows a flow chart of another polyamide preparation of the present invention.
  • the first aspect of the present invention is to provide a semi-aromatic polyamide, which is obtained by polymerizing a diamine, a dibasic acid and a monobasic acid as main raw materials and adding a blocking agent. That is, in addition to the terminal structure, the semi-aromatic polyamide structure of the present invention mainly contains structural units derived from the above-mentioned diamine, dibasic acid, and monobasic acid.
  • the diamine is not particularly limited, and a diamine commonly used in the preparation of polyamides in the art can be selected.
  • the diamine suitable for the present invention may be an aliphatic or aromatic diamine having 4 to 15 carbon atoms.
  • such a diamine may be selected from butanediamine, pentanediamine, hexamethylenediamine, heptanediamine, octanediamine, nonanediamine, decanediamine, 2-methylpentane
  • One or more of diamine, undecylmethylenediamine, dodecylmethylenediamine, and xylylenediaminediamine is preferably hexamethylenediamine , Decanediamine.
  • the dibasic acid includes one or more aromatic dibasic acids, and optionally one or more aliphatic dibasic acids.
  • the aromatic dibasic acid and aliphatic dibasic acid are not particularly limited, and dibasic acids conventional in the art can be used.
  • the aromatic dibasic acid is selected from aromatic dibasic acids having 8 to 20 carbon atoms, preferably among isophthalic acid, terephthalic acid and naphthalene dicarboxylic acid One or more kinds, more preferably any one of isophthalic acid and terephthalic acid, or any mixture of the two.
  • the aliphatic dibasic acid is selected from aliphatic dibasic acids having 4 to 15 carbon atoms, for example, it may be selected from succinic acid, glutaric acid, adipic acid, suberic acid One or more of acid, azelaic acid, sebacic acid, and dodecanedioic acid, more preferably adipic acid.
  • an aromatic dibasic acid is used as an essential component, and the above-mentioned aliphatic dibasic acid can be used when necessary.
  • the molar ratio of the aromatic dibasic acid and the aliphatic dibasic acid is 100:0 to 50:50, preferably 80:20 to 55:45.
  • the monocarboxylic acid is also not particularly limited, and may be selected from monobasic acids commonly used in the art for preparing polyamides. It is selected from monobasic acids with 2 to 30 carbon atoms, which may be aliphatic monoacids and/or aromatic monobasic acids, preferably selected from acetic acid, propionic acid, butyric acid, valeric acid, hexanoic acid, caprylic acid, capric acid , Lauric acid, palmitic acid, palmitic acid, stearic acid, benzoic acid or phenylacetic acid, one or more of them, further preferably acetic acid and benzoic acid.
  • the amount of various acids can be adjusted.
  • the number of moles of the monobasic acid relative to the total moles of the dibasic acid The number is 1 to 5%, preferably 2 to 3%.
  • the end-capping agent is used to produce an end-capping structure at the end of the polyamide molecule in the polycondensation reaction.
  • the blocking agent includes a reactive group-containing polycondensation reaction catalyst represented by formula (I) and a reactive group-containing hindered phenolic antioxidant represented by formula (II).
  • the reaction group-containing polycondensation reaction catalyst represented by the formula (I) is composed of a compound represented by the following formula (I-1) and/or formula (I-2):
  • R 1 is a carboxyl group or a C 1 -C 10 alkyl group substituted with a carboxyl group, including a C 5 -C 10 cycloalkyl group substituted with a carboxyl group or a carboxyl group, preferably a C 1 -C 4 alkyl group substituted with a carboxyl group;
  • R 2 C 1 -C 4 alkyl or H, preferably H;
  • R 3 is selected from C 6 -C 9 aromatic groups or H, preferably C 6 -C 8 aromatic groups;
  • M n+ is selected from +1, + Divalent metal cation, preferably Na + , K + ;
  • the compounds represented by the above formula (I-1) and the formula (I-2) may be used alone or in combination.
  • the compound of the above formula (I-1) is a necessary group Minute.
  • the molar ratio of the compounds represented by formula (I-1) and formula (I-2) is 10:0 to 2:8, more preferably 10:0 to 5:5.
  • the molar ratio of the compounds represented by formula (I-1) and formula (I-2) is 10:0 to 2:8, preferably 10:0 to 5:5.
  • the total phosphorus content in the semi-aromatic polyamide resin per unit mass is not higher than 200 ppm, preferably not higher than 150 ppm, and more preferably not higher than 90 ppm.
  • R 4 is selected from C 1 -C 10 alkyl groups, including C 5 -C 10 cycloalkyl groups, preferably C 1 -C 4 alkyl groups.
  • the molar amount of the reactive group-containing hindered phenolic antioxidant represented by formula (II) is 0.1 to 2.0% of the molar amount of the dibasic acid, preferably 0.3 to 1.5%.
  • phosphorus-based compounds other than the above formula (I) can be cited, including phosphoric acid, phosphorous acid, hypophosphorous acid, and their salt or ester derivatives, such as phosphoric acid, phosphorous acid, or hypophosphorous acid, or phosphoric acid, Sodium, potassium, magnesium, vanadium, calcium, zinc, cobalt, manganese, tin, tungsten, germanium, titanium or antimony salts of phosphorous acid or metal hypophosphite; ammonium phosphate, ammonium phosphite and ammonium diphosphate; phosphoric acid, phosphorous acid Or ethyl ester, isopropyl ester, butyl ester, hexyl ester, isodecyl ester, octadecyl ester, decyl ester, octadecanoyl ester, phenyl ester or the like of hypophosphorous acid.
  • the semi-aromatic polyamide of the present invention is a polymer having active end groups obtained after a polycondensation reaction.
  • the concentration of the active end groups satisfies: [NH 2 ]/[COOH]>5,
  • the [COOH] concentration is not higher than 20 mmol/kg, preferably not higher than 10 mmol/kg.
  • the semi-aromatic polyamide described in the present invention has improved thermal stability, excellent yellowing resistance, and high glass transition temperature and melting point relative to the prior art.
  • the semi-aromatic polyamide according to the present invention has a thermal stability index of MV 30 /MV 6 greater than 95%, preferably greater than 96%, and a yellowness index of less than 20, preferably less than 19,
  • the glass transition temperature is above 90°C, preferably above 95°C, and the melting point is above 300°C.
  • the second aspect of the present invention also provides a method for preparing a semi-aromatic polyamide.
  • the second object of the present invention is to provide a method for preparing the above heat-stable semi-aromatic polyamide, which may be a method existing in the prior art that can realize any of the technical solutions described in the present invention, for example, may be a melting method , Solution method and solid state method.
  • diamine, dibasic acid and monobasic acid are used as the main raw materials, and the special end-capping agent as described above is added to prepolymerization and polycondensation. It is further preferred that diamine, dibasic acid and monobasic acid are used as the main raw materials, and a special end-capping agent is added to form a salt, prepolymerization, and polycondensation reaction. Wherein the polycondensation is melt polycondensation or solid phase polycondensation, preferably melt polycondensation.
  • the monocarboxylic acid and special end-capping agent are added during the salt-forming, pre-polymerization or polycondensation reaction stage, preferably during the pre-polymerization reaction stage.
  • the method described in the present invention uses diamine, dibasic acid and monobasic acid as main raw materials, and performs polymerization in the presence of a blocking agent, which is of formula (I) and formula (II) Structure.
  • diamines dibasic acids, monobasic acids, and blocking agents are the same as the first aspect of the present invention.
  • the method for preparing the semi-aromatic polyamide specifically includes the following reactions, processes, or steps:
  • Salt formation reaction the initial feeding of diamine and dibasic acid according to the amine/acid molar ratio is less than 1 to form a salt solution with water;
  • Prepolymerization reaction Use diamine, monobasic acid and blocking agent to adjust the amine/acid molar ratio in the reaction system to greater than 1.03, perform prepolymerization reaction to obtain prepolymerization reaction liquid;
  • Polycondensation reaction Use a pre-polymerization reaction solution for polycondensation reaction.
  • the method for preparing the semi-aromatic polyamide may specifically be:
  • Salt formation reaction step 1: the initial feeding of the diamine and the dibasic acid according to the molar ratio of amine acid is less than 1, forming a slurry with water, the slurry is heated and dissolved to form a salt solution, wherein, preferably, the initial feeding
  • the molar ratio of amine acids is 0.90 to 0.99, and more preferably 0.92 to 0.98.
  • Step 2 After detecting the composition of the salt solution, dehydrate the salt solution, detect the content of diamine in the steam condensate water from the dehydration device, use diamine, molecular weight regulator monobasic acid And the end-capping agent adjusts the molar ratio of amine acid to greater than 1.03, and conducts the prepolymerization reaction;
  • step 3 The pre-polymerization reaction solution undergoes polycondensation reaction after flashing under reduced pressure.
  • the step 1 further includes: detecting the composition of the dibasic acid in the salt solution, and maintaining the dibasic by adding an aromatic dibasic acid and/or an aliphatic dibasic acid
  • the acid constitutes a stable step.
  • the composition of the dibasic acid in the salt solution is obtained by online Raman spectroscopy, and the composition of the dibasic acid in the salt solution is adjusted by using an aliphatic dibasic acid and/or aromatic dibasic acid slurry according to the detection result. Make it stable.
  • the molar ratio of amine acid in the salt solution before dehydration and the content of diamine in the steam condensate water from the dehydration device are detected by online Raman spectroscopy.
  • the molar ratio of the amino acid and the molecular weight regulator monobasic acid and the above-mentioned blocking agent is adjusted to be greater than 1.03.
  • diamine and molecular weight regulator monobasic acid and the above-mentioned blocking agent to adjust the molar ratio of amine acid to greater than 1.03 refers to the adjusted aliphatic diamine and aliphatic dibasic acid, aromatic dibasic acid, molecular weight
  • the molar ratio of the amino acid of the regulator monobasic acid and the blocking agent is controlled to be greater than 1.03, preferably 1.035 to 1.07, and more preferably 1.04 to 1.06.
  • the production method of semi-aromatic polyamide is a continuous production method.
  • the composition of the dibasic acid in the salt solution is obtained by online Raman spectroscopy, and the composition of the dibasic acid in the salt solution is adjusted by using an aliphatic dibasic acid and/or aromatic dibasic acid slurry according to the detection result. Make it stable.
  • the molar ratio of amine acid in the material before dehydration and the content of diamine in the steam condensate water from the dehydration device are detected.
  • the molar ratio of amine acid of the blocking agent is greater than 1.03.
  • the water vapor removed in the dehydration stage can be used as a heat source for the temperature rising and dissolving process of the slurry in the salt formation reaction (Step 1), and the excess water vapor can be combined with the condensed water generated in the temperature raising step after condensation It is a process for forming the slurry as additional water.
  • the water content of the system may be 10-50%, preferably 15-30%, and the temperature may be 50-95°C, preferably It is 60 ⁇ 90°C.
  • the temperature for dissolution into salt may be 120 to 170°C, preferably 130 to 160°C.
  • the dehydration temperature can be 180-240°C; the pressure can be 0.8-1.5 MPa; the dehydration time can be 10-30 min, preferably 15-30 min; the water content after dehydration is 5-20%, preferably 7 to 15%.
  • the prepolymerization reaction temperature may be 280-350°C, preferably 280-340°C; the pressure may be 15-30MPa, preferably 15-25MPa; and the reaction time may be 1 ⁇ 15min, preferably 2-10min.
  • the reduced pressure flash pressure after the prepolymerization reaction may be 0.15 to 0.9 MPa, preferably 0.2 to 0.6 MPa, and the temperature may be the same as the temperature of the prepolymerization reaction.
  • the prepolymer enters the twin-screw extruder in the form of a melt to carry out the polycondensation reaction.
  • the reaction temperature may be 290 to 350°C, preferably 310 to 340°C; the reaction time may be 0.5 to 7 min, preferably 1 to 6 min .
  • the device for implementing the above method of the present invention is not particularly limited, and various production equipment and auxiliary facilities in the art may be used to implement the above production method.
  • FIG. 3 may be used.
  • the resin composition of the present invention includes the semi-aromatic polyamide of the first aspect of the present invention or the semi-aromatic polyamide obtained by the production method of the second aspect of the present invention.
  • the composition of the present invention may further contain optional other resins, reinforcing components, additives, etc. as needed.
  • the other resin may be a thermoplastic resin or a thermosetting resin.
  • it may be a polyester resin, an epoxy resin, a polyacrylic resin, an olefin elastomer, or the like.
  • additional components may be used to improve the toughness of the polyamide resin, and these components may be elastomers as described above, such as copolymers based on ethylene and/or diene, etc. .
  • these elastomers can be modified by substituents with polar groups. Typically, these substituents can be derived from anhydride monomers, for example, maleic anhydride and the like.
  • the resin composition of the present invention can be reinforced with fiber reinforcement or inorganic filler
  • the fiber can be resin fiber, carbon fiber, inorganic fiber, mineral fiber, etc.
  • the inorganic filler can be silica, titania, Montmorillonite, etc.
  • the surface of the inorganic components in these components is preferably treated with a compatibilizer to enhance its compatibility with the polyamide matrix.
  • additives and the like without limitation, various processing aids, antioxidants, antistatic agents, ultraviolet absorbers, lubricants, etc. in the art can be used.
  • the mixing method of the resin composition of the present invention is not particularly limited, and may be melt-mixing of various components, which may be blended using an internal mixer or an open mixer, or directly blended and extruded using an extruder.
  • the composition in the case where a fiber-reinforced component is present in the composition, the composition can be obtained by a dipping method by means of a solvent, and the dipping method can use a method conventional in the art.
  • the present invention also provides products based on the above composition, and these products can be obtained by injection molding, extrusion, dipping and other methods.
  • these products may be automobile parts or parts in the electrical appliance industry, specifically, automobile fuel line parts or LED boards.
  • t 0 is the flow time (s) of the solvent
  • t is the flow time (s) of the solution
  • C is the concentration (g/dL) of the sample solution.
  • the thermal stability described in the present invention is represented by the melt viscosity retention rate.
  • the yellowness index YI is the yellow value of a polymer material measured when the standard of the International Illumination Commission is used as the light source and magnesium oxide is used as the reference.
  • the specific test method is: use the yellowness index meter to determine the yellowness index of the sample after being placed at different temperatures for 24h, and the yellowness index at 60°C for different times.
  • the calculation method is shown in the formula:
  • X, Y and Z are the measured tristimulus values.
  • the melting point was measured in accordance with HG/T2235-1991 (2012). In the temperature range of 20-330°C, the heating rate is 10°C/min, the temperature is raised to 330°C, and the temperature is maintained for 5min. The test is conducted at a temperature-lowering rate of 20°C/min.
  • the content of isophthalic acid (IA) and its salt (6I) is determined by the characteristic peaks at 1005 cm -1 and 762 cm -1 ;
  • TA terephthalic acid
  • 6T 6T
  • HDA hexamethylene diamine
  • Examples 1-4 and Comparative Examples 1-4 are implemented according to the flow of FIG. 3; the prepolymerization process of Example 5 is executed according to the flow of FIG. 3, and polycondensation adopts solid phase polycondensation; Example 6 is executed according to the flow of FIG. 4.
  • the preparation process all materials are deoxidized with high-purity nitrogen, and all devices in the preparation process are replaced and protected by high-purity nitrogen.
  • the ratio of the initial feeding amino acid molar ratio of 0.92, 4.66Kg/h (27.5mol/h) terephthalic acid, 3.29Kg/h (22.5mol/h) adipic acid, 5.34Kg/h (46.0mol/h ) Hexanediamine and 3.2Kg/h of water are put into the beating kettle 9, and beating is continued at 70°C to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 160°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19 The proportion of yuan acid remains stable.
  • the pump 24 is pressurized to 1.0 MPa, and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the materials sent by the circulation pump 28, and then heated up.
  • the dehydration temperature is controlled at 180°C
  • the water content is controlled at 13%
  • the dehydration residence time is 30 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the amount of molten hexamethylenediamine needed before pump 32 is determined by the controller 21; the dehydrated materials pass the molten hexamethylenediamine and 0.06Kg/h through pump 17, 30 respectively (1.0mol/h) molecular weight regulator acetic acid, 0.153Kg/h (0.5mol/h) 3-(3,5-di-tert-butyl-4-hydroxyphenyl) valeric acid, 0.0114Kg/h (90ppmP) P -(4-carboxybutylphenyl) and P-phenyl-phosphinic acid adjusted the molar ratio of amine acid to 1.04.
  • the pressure valve 35 is depressurized to 0.3 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 290-320°C, and the reaction residence time is 6 minutes.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 12.4 Kg/h.
  • the diacid, 8.43 Kg/h (49.0 mol/h) decanediamine and 5.0 Kg/h of water are put into the beating kettle 9 and are continuously beaten at 90° C. to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 170°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19
  • the proportion of yuan acid remains stable.
  • the above salt solution is detected by online Raman spectroscopy 20, it is boosted by pump 24 to 1.5 MPa and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the material sent by the circulation pump 28 and then heated up.
  • the dehydration temperature is controlled at 240°C
  • the water content is controlled at 10%
  • the dehydration residence time is 10 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the controller 21 determines the amount of molten decanediamine to be added before the pump 32; the dehydrated materials pass the molten decanediamine through the pump 17 and pump 30, 0.122Kg/h (1.0mol/h) molecular weight regulator benzoic acid, 0.0393Kg/h (0.15mol/h) 2-(3,5-di-tert-butyl-4-hydroxyphenyl) acetic acid, 0.0079Kg/h (70ppm P ) P-(4-carboxyethylphenyl) and P-(4-methylphenyl)phosphinic acid adjusted the molar ratio of amine acid to 1.06.
  • the pressure valve 35 is depressurized to 0.5 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 320-330°C, and the reaction residence time is 1 min.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 15.4 Kg/h.
  • the diamine and 4.0Kg/h of water are put into the beating kettle 9, and the beating is continued at 80°C to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 165°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19
  • the proportion of yuan acid remains stable.
  • the above salt solution is detected by online Raman spectroscopy 20, it is boosted by pump 24 to 1.3 MPa and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the material sent by the circulation pump 28 and then heated up.
  • the dehydration temperature is controlled at 220°C
  • the water content is controlled at 12%
  • the dehydration residence time is 20 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the controller 21 determines the amount of supplementary molten hexamethylenediamine before the pump 32; the dehydrated materials pass the pump 17, the pump 30 with molten hexamethylenediamine and 0.09Kg/h (1.5mol/h) molecular weight regulator acetic acid, 0.0725Kg/h (0.25mol/h) 2-(3,5-di-tert-butyl-4-hydroxyphenyl) butyric acid, 0.0063Kg/h (50ppm P ) P-(4-carboxybutylphenyl) and P-(3,4-dimethylphenyl)phosphinic acid adjusted the molar ratio of amine acid to 1.05.
  • the pressure valve 35 decompresses to 0.4 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 to perform polycondensation reaction.
  • the reaction temperature is 310-320°C, and the reaction residence time is 3 minutes.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 12.2 Kg/h.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19 The proportion of yuan acid remains stable.
  • the pump 24 is pressurized to 1.0 MPa, and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the materials sent by the circulation pump 28, and then heated up.
  • the dehydration temperature is controlled at 180°C
  • the water content is controlled at 13%
  • the dehydration residence time is 30 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the amount of molten hexamethylenediamine needed to be supplemented before the pump 32 is determined by the controller 21; the dehydrated materials pass the molten hexamethylenediamine, 0.045Kg/h through the pump 17 and pump 30 respectively (0.75mol/h) molecular weight regulator acetic acid, 0.153Kg/h (0.5mol/h) 3-(3,5-di-tert-butyl-4-hydroxyphenyl)valeric acid, 0.0118Kg/h (90ppmP)P -(4-carboxybutylphenyl) and P-phenyl-phosphinic acid (50% neutralized with NaOH) to adjust the molar ratio of amine acid to 1.04.
  • the pressure valve 35 is depressurized to 0.3 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 290-320°C, and the reaction residence time is 6 minutes.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 12.4 Kg/h.
  • the ratio of the initial feeding amino acid molar ratio of 0.92, 4.66Kg/h (27.5mol/h) terephthalic acid, 3.29Kg/h (22.5mol/h) adipic acid, 5.34Kg/h (46.0mol/h ) Hexanediamine and 3.2Kg/h of water are put into the beating kettle 9, and beating is continued at 70°C to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 160°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19 The proportion of yuan acid remains stable.
  • the pump 24 is pressurized to 1.0 MPa, and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the materials sent by the circulation pump 28, and then heated up.
  • the dehydration temperature is controlled at 180°C
  • the water content is controlled at 13%
  • the dehydration residence time is 30 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the amount of molten hexamethylenediamine needed before pump 32 is determined by the controller 21; the dehydrated materials pass the molten hexamethylenediamine and 0.06Kg/h through pump 17, 30 respectively (1.0mol/h) molecular weight regulator acetic acid, 0.153Kg/h (0.5mol/h) 3-(3,5-di-tert-butyl-4-hydroxyphenyl) valeric acid, 0.0118Kg/h P-(4 -Carboxybutylphenyl) and P-phenyl-phosphinic acid (50% neutralized with NaOH, 90 ppm of P) to adjust the molar ratio of amine acid to 1.04.
  • molecular weight regulator acetic acid 0.153Kg/h (0.5mol/h) 3-(3,5-di-tert-butyl-4-hydroxyphenyl) valeric acid, 0.0118Kg/h P-(4 -Carboxybutylphenyl) and P-phenyl-phosphin
  • dehydration temperature is controlled at 260°C, water content controlled at 5%, dehydration residence time is 10min; dehydration qualified material is pressurized to 27MPa with pump 48, the material is transferred to preheater 49 and preheated to 320°C, in prepolymerization reactor 50 Incubate at 320°C for 3min; pre-polymerization reaction liquid is reduced to 0.9MPa by pressure reducing valve 51 and enters into flash evaporator 52.
  • Flash molten liquid material is reduced to normal pressure by pressure reducing valve 53 to enter twin screw extrusion
  • the polycondensation reaction is carried out in the machine 54, the reaction temperature is 320-330 °C, the reaction residence time is 3min; the material after the polycondensation reaction is granulated in the underwater granulator 55, and then dried by the dryer 56, obtained at about 12.6Kg/h Semi-aromatic polyamide products.
  • the ratio of the initial feeding amino acid molar ratio of 0.92, 4.66Kg/h (27.5mol/h) terephthalic acid, 3.29Kg/h (22.5mol/h) adipic acid, 5.34Kg/h (46.0mol/h ) Hexanediamine, 0.0024Kg/h hypophosphorous acid (50% neutralized with NaOH, equivalent to 90ppmP) and 3.2Kg/h of water are put into the beating kettle 9, and continuous beating at 70°C to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 160°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19 The proportion of yuan acid remains stable.
  • the pump 24 is pressurized to 1.0 MPa, and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the materials sent by the circulation pump 28, and then heated up.
  • the dehydration temperature is controlled at 180°C
  • the water content is controlled at 13%
  • the dehydration residence time is 30 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the controller 21 determines the amount of molten hexamethylenediamine needed before the pump 32 is added; the dehydrated materials pass the pump 17, the pump 30 with molten hexamethylenediamine and 0.03Kg/h (0.5mol/h)
  • the molecular weight regulator acetic acid adjusted the molar ratio of amino acids to 1.04. Then pressurize the pump 32 to 15MPa, transfer the material to the preheater (heat exchanger) 33, preheat it and raise it to 290°C, keep it at 290°C for 15min in the prepolymerization reactor 34;
  • the pressure valve 35 is depressurized to 0.3 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 290-320°C, and the reaction residence time is 6 minutes.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 12.4 Kg/h.
  • the diacid, 8.43Kg/h (49.0mol/h) decanediamine, 0.0019Kg/h hypophosphorous acid (70ppm of P) and 5.0Kg/h of water are put into the beating kettle 9, which is continuously beaten at 90°C to form a slurry .
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 170°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19
  • the proportion of yuan acid remains stable.
  • the above salt solution is detected by online Raman spectroscopy 20, it is boosted by pump 24 to 1.5 MPa and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the material sent by the circulation pump 28 and then heated up.
  • the dehydration temperature is controlled at 240°C
  • the water content is controlled at 10%
  • the dehydration residence time is 10 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the controller 21 determines the amount of molten decanediamine to be added before the pump 32; the dehydrated materials pass the molten decanediamine and 0.122Kg/h through the pump 17, 30 respectively (1.0mol/h)
  • the molecular weight regulator benzoic acid adjusted the molar ratio of amino acids to 1.06.
  • the pressure valve 35 is depressurized to 0.5 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 320-330°C, and the reaction residence time is 1 min.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 15.3 Kg/h.
  • the ratio of the initial feeding amino acid molar ratio of 0.92, 4.66Kg/h (27.5mol/h) terephthalic acid, 3.29Kg/h (22.5mol/h) adipic acid, 5.34Kg/h (46.0mol/h ) Hexanediamine and 3.2Kg/h of water are put into the beating kettle 9, and beating is continued at 70°C to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 160°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19 The proportion of yuan acid remains stable.
  • the pump 24 is pressurized to 1.0 MPa, and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the materials sent by the circulation pump 28, and then heated up.
  • the dehydration temperature is controlled at 180°C
  • the water content is controlled at 13%
  • the dehydration residence time is 30 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the controller 21 determines the amount of molten hexamethylenediamine needed before the pump 32 is added; the dehydrated materials pass the pump 17, the pump 30 with molten hexamethylenediamine and 0.03Kg/h (0.5mol/h) molecular weight regulator acetic acid, 0.153Kg/h (0.5mol/h) 3-(3,5-di-tert-butyl-4-hydroxyphenyl)pentanoic acid adjusted the molar ratio of amino acids to 1.04.
  • the pressure valve 35 is depressurized to 0.3 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 290-320°C, and the reaction residence time is 6 minutes.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 12.4 Kg/h.
  • the ratio of the initial feeding amino acid molar ratio of 0.92, 4.66Kg/h (27.5mol/h) terephthalic acid, 3.29Kg/h (22.5mol/h) adipic acid, 5.34Kg/h (46.0mol/h ) Hexanediamine and 3.2Kg/h of water are put into the beating kettle 9, and beating is continued at 70°C to form a slurry.
  • the slurry is transported by the pump 10 to the multi-stage stirring and dissolving kettle 14 and heated to 160°C with steam generated in the dehydration process to dissolve into salts.
  • the composition of the dibasic acid in the salt solution is detected according to online Raman spectroscopy 18, and the amount of the aliphatic dibasic acid is adjusted by the metering pump 23 using molten adipic acid to dissolve the aromatic dibasic acid and the aliphatic dibasic acid in the salt kettle 19 The proportion of yuan acid remains stable.
  • the pump 24 is pressurized to 1.0 MPa, and then sent to the preheater (heat exchanger) 27 of the dehydrator before being mixed with the materials sent by the circulation pump 28, and then heated up.
  • the dehydration temperature is controlled at 180°C
  • the water content is controlled at 13%
  • the dehydration residence time is 30 minutes.
  • the steam from the dehydrator is used as the heat source of the multi-stage stirring and dissolving kettle 14, and after cooling through the heat exchanger 15, the amine content in the online Raman spectroscopy 16 is detected.
  • the controller 21 determines the amount of molten hexamethylenediamine needed before the pump 32 is added; the dehydrated materials pass the pump 17, the pump 30 with molten hexamethylenediamine and 0.03Kg/h (0.5mol/h) molecular weight regulator acetic acid, 0.0118Kg/h P-(4-carboxybutylphenyl), P-phenyl-phosphinic acid (50% neutralized with NaOH, 90ppm of P) to adjust the amino acid The molar ratio is 1.04.
  • the pressure valve 35 is depressurized to 0.3 MPa and enters the flasher 36.
  • the molten liquid material is decompressed to normal pressure through the pressure reducing valve 37, and then enters the twin-screw extruder 38 for polycondensation reaction.
  • the reaction temperature is 290-320°C, and the reaction residence time is 6 minutes.
  • the polycondensation-reacted material is granulated in an underwater granulator 39 and then dried by a dryer 40 to obtain a semi-aromatic polyamide product at about 12.4 Kg/h.
  • the polyamide obtained by adding the terminal blocking agent of the present invention can maintain good thermal stability and the yellowness index is relatively low compared to the semi-aromatic polyamide obtained by adding the hypophosphorous acid catalyst alone or without the phosphorus-containing catalyst.
  • adding a special end-capping agent and a hindered phenolic antioxidant containing reactive groups can provide a polyamide with better thermal stability than just adding one of them.

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Abstract

本发明公开了一种半芳香族聚酰胺及其制备方法，所述半芳香族聚酰胺是以二元胺、二元酸、一元酸为主要原料，同时加入特定封端剂经聚合反应得到。按本发明制备的半芳香聚酰胺热稳定性良好，黄度指数小于20，玻璃化转变温度在90℃以上，熔点在300℃以上，可应用于汽车燃油管路等零部件、LED板等电子电气行业。

Description

半芳香族聚酰胺树脂及其制备方法 技术领域
本发明涉及一种半芳香族聚酰胺树脂及其制备方法，尤其是提供一种添加特定封端剂的热稳定性半芳香族聚酰胺树脂及其制备方法，其可应用于汽车零部件以及电器零部件，尤其是LED板。
背景技术
聚酰胺又称作尼龙(Nylon)，是指大分子主链重复基团中含有酰胺基团(-NHCO-)的高聚物的总称；是工程塑料中产量最大、品种最多、用途最广的品种。脂肪族聚酰胺，例如尼龙6、尼龙66等，虽然其各项综合性能不错，但热性能无法满足高温工作环境的要求，限制了它在高新技术领域的应用。
半芳香族聚酰胺由于在聚酰胺分子链中引入了芳香环，相比较于通用的PA6和PA66，在耐热性、力学性能和吸水率、耐化学性等方面有了长足的提高。半芳香族聚酰胺主要有以下特征：(1)玻璃化转变温度高，具有良好的耐热性能；(2)具有良好的耐热氧老化性能；(3)具有良好的电绝缘性能；(4)吸水率小，制品的尺寸稳定性好。因此，随着近代高科技的迅速发展，半芳香族聚酰胺的应用越来越广泛。半芳香族聚酰胺广泛应用于电气、电子部件、以及汽车部件等领域。具体地，在汽车行业中，发动机室的周边部件(即引擎盖下组件)长期暴露于高温环境(高于120℃)，对聚酰胺的长期热稳定性提出了更高的要求；在LED外壳制造过程中，通常需要借助回流焊(SMT)的方法在约260℃下焊接电路板，因此所用聚合物应具有足够的耐热性并能耐受回流焊接而不会起泡，还应具有高UV光稳定性和热稳定性，以及运行条件下良好的长期稳定性。
关于合成聚酰胺的报道已有很多，例如文献GB543843A、US3173898报道了将磷酸、二价磷酸盐类作为聚合过程的催化剂。文献CN1238790报道了采用低于露点30℃的超级干燥气体与含磷的SPP催化剂(2(2’-吡啶基)乙基膦酸或次磷酸盐)一起使用在较低反应温度下显著地提高固相聚合速率，获得PA66高聚物。
文献EP0475400、CA2248123、US2010055455A1报道了通过添加目前公知的热稳定剂、抗氧化剂如受阻酚类制备聚酰胺组合物，提高聚酰胺的热稳定性和抗氧化性，并将其应用于飞机发动机复合部件。
文献EP0827976报道了改进热稳定性的部分芳族聚酰胺组合物，热稳定剂为碱金属卤化物与铜(I)卤化物的混合物，重量比最优选约8:1至约10:1，基于聚酰胺，含铜稳定剂的量为50至约1000ppm。220℃热老化试验表明，添加含铜热稳定剂，机械强度损失50％所需时间相较未添加热稳定剂时延长2～3倍。
文献CN107325548A报道了加入不大于2％质量份的一价或二价铜化合物、脂肪族羧酸铜盐、仲芳香胺以及空间位阻酚类或其中几类混合物做热稳定剂以提高树脂的热稳定性。文献WO2018049808A1、CN103694693A报道了采用受阻酚系、氢醌系、亚磷酸酯系以及取代体、卤化铜、碘化合物等作为PA66聚酰胺组合物的热稳定剂，提高PA66组合物的热稳定性和耐老化性。
文献WO2005/007727A1报道了在聚酰胺中添加单质铁热稳定剂，可在高温下表现出更好的机械性能保留率。文献CN103890040A提出通过添加金属氧化物的方法改性聚酰胺树脂，使得聚酰胺组合物 保持高机械强度、长期耐氧化性、以及高耐热性，主要应用于LED制品。
文献CN101180342A、WO02083345A1、US5744433A和US5154881A报道了常见的聚酰胺低聚物，该聚酰胺低聚物由不同的结构构成，其具有非反应性酚或胺端基，分子量在800～5000g/mol之间，常被用于与聚酰胺树脂共混，可提高聚酰胺树脂的流动性、粘度稳定性、耐水解稳定性。
尽管如此，现有热稳定聚酰胺制备过程仍存在以下问题：
(1)大多数聚酰胺树脂制备所使用的催化剂为无机类亚磷酸、次磷酸及其金属盐化合物，提升聚酰胺热稳定性、耐老化性主要通过添加热稳定剂、抗氧化剂等进行共混制备聚酰胺组合物，制成的制件长时间在高温条件下使用时，催化剂、热稳定剂、抗氧化剂等容易发生迁移，无法实现长期抗氧化、热稳定的目的。
(2)所添加的热稳定剂含有重金属盐，对环境有潜在危害。
(3)添加聚酰胺低聚物会使聚酰胺树脂组合物热变形温度降低，影响其在耐高温领域的使用范围。
因此，可以看出本领域中对于具有优异特性的聚酰胺的研究仍然存在进一步提高的余地。
发明内容
发明要解决的问题
为了解决上述现有技术中存在的问题，本发明的目的在于提供一种半芳香族聚酰胺，其能够保持长期的热稳定性，并且能够避免热稳定剂、抗氧化剂等添加剂在使用过程中发生迁移，同时，也能够避免使用对环境有潜在危害的热稳定性添加剂。
本发明的另一目的在于提供一种能够保持长期热稳定性且热稳定剂、抗氧化剂等不发生迁移的半芳香族聚酰胺的制备方法以及包含所述半芳香族聚酰胺的树脂组合物及其制品。
用于解决问题的方案
本发明人经反复研究发现，在制备半芳香族聚酰胺的聚合反应过程中通过添加特定的封端剂可以解决上述问题。
该封端剂包含下述式(I)表示的含反应基团的缩合催化剂和式(II)表示的含反应基团的受阻酚类抗氧化剂的封端剂。其中，发明人发现了，该催化剂不仅能够参与聚合反应过程，提高聚合反应速率，而且自身能够与胺端基反应，反应完成后成为聚合物的含低价膦端基，并且，这样的结构能够带来改进的抗氧化作用；其次，含反应基团的位阻酚抗氧化剂也可与胺端基反应，使得抗氧化剂能够以原位反应的方式均匀分布以及固定在聚合物中，避免受热时产生向表面的迁移而失效的现象。因此，本发明的上述封端剂能够保持聚合物的长期热稳定性也能够避免传统小分子添加剂(热稳定剂、抗氧剂等)在加工、使用过程中迁移出树脂基体的问题。
本发明的概要如以下[1]～[20]所示。
[1].本发明首先提供了一种半芳香族聚酰胺，其具有源自于二元胺、二元酸和一元酸的结构单元，及其具有源自下式(I)和式(II)的封端结构，
其中：
所述式(I)选自下述式(I-1)和/或式(I-2)所示化合物：
Figure PCTCN2019119738-appb-000001
其中R 1为羧基或羧基取代的C 1～C 10的烷基，优选为羧基取代的C 1～C 4的烷基；R 2为C 1～C 4的烷基或H，优选为H；R 3选自C 6～C 9的芳香基或H，优选为C 6～C 8的芳香基；M n+选自+1、+2价金属阳离子；
所述式(II)为：
Figure PCTCN2019119738-appb-000002
其中R 4选自C 1～C 10的烷基，优选为C 1～C 4的烷基。
[2].根据[1]所述的半芳香族聚酰胺，其中，所述金属阳离子为Na +或K +。
[3].根据[1]或[2]所述的半芳香族聚酰胺，其中，单位质量所述半芳香族聚酰胺树脂中总磷量不高于200ppm，优选不高于150ppm，更优选不高于90ppm。
[4].根据[1]～[3]任一项所述的半芳香族聚酰胺，其中，式(I-1)和式(I-2)所示化合物的摩尔比为10:0～2:8，优选为10:0～5:5。
[5].根据[1]～[4]任一项所述的半芳香族聚酰胺，其中，源自所述式(II)结构的摩尔量为源自二元酸结构的摩尔量的0.1～2.0％，优选为0.3～1.5％。
[6].根据[1]～[5]任一项所述的半芳香族聚酰胺，其中，源自所述一元酸结构的摩尔数相对于源自所述二元酸结构的总摩尔数为1～5％，优选为2～3％。
[7].根据[1]～[6]任一项所述的半芳香族聚酰胺，其中，所述二元酸包括芳香族二元酸、任选的脂肪族二元酸的一种或多种，所述芳香族二元酸和脂肪族二元酸的摩尔比为100:0～50:50，优选为80:20～55:45。
[8].根据[1]～[7]任一项所述的半芳香族聚酰胺，其中，所述半芳香族聚酰胺树脂具有活性端基，且活性端基浓度满足：[NH 2]/[COOH]＞5，并且，所述半芳香族聚酰胺树脂中，[COOH]浓度不高于20mmol/kg，优选不高于10mmol/kg。
[9].根据[1]～[8]任一项所述的半芳香族聚酰胺，其具有MV 30/MV 6大于95％的热稳定性指数，黄度指数小于20，玻璃化转变温度在90℃以上，熔点在300℃以上。
[10].进一步地，本发明还提供了一种半芳香族聚酰胺的制备方法，所述方法以二元胺、二元酸和一元酸为主要原料，并在封端剂的存在下进行聚合，所述封端剂为以下式(I)和式(II)的结构，
其中：
所述式(I)选自下述式(I-1)和/或式(I-2)所示化合物：
Figure PCTCN2019119738-appb-000003
其中R 1为羧基或羧基取代的C 1～C 10的烷基，优选为羧基取代的C 1～C 4的烷基；R 2为C 1～C 4的烷基或H，优选为H；R 3选自C 6～C 9的芳香基或H，优选为C 6～C 8的芳香基；M n+选自+1、+2价金属阳离子；
所述式(II)为：
Figure PCTCN2019119738-appb-000004
其中R 4选自C 1～C 10的烷基，优选为C 1～C 4的烷基。
[11].根据[10]所述的方法，其包括：
成盐反应：将二元胺与二元酸按照胺/酸摩尔比小于1的初始投料，与水形成盐溶液；
预聚反应：用二元胺、一元酸及封端剂调反应体系中整胺/酸摩尔比至大于1.03，进行预聚反应，得到预聚反应液；
缩聚反应：使用预聚反应液进行缩聚反应。
[12].根据[11]所述的方法，所述成盐反应中，初始投料的胺酸摩尔比为0.90～0.99，优选为0.92～0.98。
[13].根据[11]或[12]所述的方法，其中，所述成盐反应中还包括：检测所述盐溶液中二元酸的组成，通过添加芳香族二元酸和/或脂肪族二元酸以维持二元酸组成/含量稳定；所述预聚反应中还包括所述检测预聚反应体系中组成，所述检测均采用在线拉曼光谱进行。
[14].根据[11]～[13]任一项所述的方法，其中，所述预聚反应中的胺/酸摩尔比为1.03～1.07，优选为1.04～1.06。
[15].根据[11]～[14]任一项所述的方法，其中，所述预聚反应前还包括对所述成盐溶液进行脱水处理，所述脱水的温度为180～240℃，压力为0.8～1.5MPa，脱水时间为10～30min；所述预聚反应的温 度为280～350℃，压力为15～30MPa，反应时间为1～15min；缩聚反应的反应温度为290～350℃，反应时间为0.5～7min。
[16].根据[15]所述的方法，其中，所述脱水处理产生的水蒸汽可作为热源用于所述浆料的升温、溶解，多余水蒸汽可在冷凝后与升温工序中产生的冷凝水合并作为补加水用于形成所述浆料的工序。
[17].进一步地，本发明还提供了一种树脂组合物，其包括：
根据[1]～[9]任一项所述的半芳香族聚酰胺，或者根据[10]～[16]任一项所述的方法得到的半芳香族聚酰胺，以及任选的其它树脂、增强组分或添加剂。
[18].另外本发明还提供了一种制品，其由根据[17]所述的组合物制备而得到。
[19].根据[18]所述的制品，其为汽车部件或电器行业用部件。
[20].根据[18]所述的制品，其为汽车燃油管路零部件或LED板。
发明的效果
本发明的半芳香聚酰胺树脂中含有特定的封端剂或者通过特定的封端剂制备而得到。该封端剂包含式(I)所表示的含反应基团的缩合催化剂和式(II)所表示的含反应基团的受阻酚类抗氧化剂的封端剂。上述催化剂不仅能够参与聚合反应过程，提高聚合反应速率，而且自身能够与胺端基进行原位封端反应，反应完成后成为聚合物的含低价膦端基，具有一定的抗氧化作用；其次，含反应基团的位阻酚抗氧化剂也可与胺端基进行原位封端反应，使得抗氧化剂能够均匀分布并固定在聚合物中，避免受热时产生向表面的迁移而失效的现象。因此，本发明的特殊封端剂能够保持聚合物的长期热稳定性。
此外，本发明通过控制聚合物的羧基官能团的含量，可有效控制聚合物在受热时与胺端基的反应，从而改进了聚合物受热时粘度和分子量的稳定性。
附图说明
图1显示各种尼龙盐的归一化拉曼光谱(600～1200cm -1)。
图2显示各种尼龙盐的归一化拉曼光谱(1200～1800cm -1)。
图3显示本发明的一种聚酰胺制备的流程图。
图4显示本发明的另一种聚酰胺制备的流程图。
附图标记说明
1 脂肪酸二元酸料仓
2、4、6 进料螺杆输送器
3 对苯二甲酸料仓
5 间苯二甲酸(或其他二元酸)料仓
7 催化剂水溶液储罐
8、10、12、13、17、23、24、26、28、30、32 泵
9 打浆釜
11 熔融二元胺储罐
14 多级搅拌溶解釜
15、27、33、44、49 热交换器
16、18、20 在线拉曼光谱检测器
19 溶解成盐釜
21 控制器
22 熔融脂肪族二元酸储罐
25 间苯二甲酸(或其他二元酸)料浆储罐
29、46 脱水器
31 熔融一元酸储罐
34、50 预聚反应器
35、37、51、53 减压阀
36、52 闪蒸器
38、54 缩聚反应器(双螺杆挤出机)
39、55 造粒机
40、56 干燥机
41、42 成盐釜
43 盐溶液输送泵
45 循环泵
47 冷凝器
48 脱水物料进料泵
具体实施方式
以下将对本发明所述的聚酰胺及其制备方法和应用进行详细说明。需要说明的是，除非特殊声明，本发明所使用的单位名称均为本领域通用的国际单位名称。此外，本发明以下出现的数值的点值或者数值范围均应当理解为包括了工业上允许的误差。
<本发明的第一方面>
本发明的第一方面是提供了一种半芳香族聚酰胺，其是以二元胺、二元酸和一元酸为主要原料，加入封端剂聚合得到。即本发明的半芳香族聚酰胺结构中除了封端结构以外，主要含有源自于上述二元胺、二元酸以及一元酸的结构单元。
二元胺/二元酸/一元酸
对于所述二元胺，没有特别限定，可以选择本领域通常制备聚酰胺所使用的二元胺。例如，适合本发明的二元胺可以为碳原子数为4～15的脂肪族或芳香族二胺。在本发明一些优选的实施方案中，这样的二胺可以选自丁二胺、戊二胺、己二胺、庚二胺、辛二胺、壬二胺、癸二胺、2-甲基戊二胺、十一亚甲基二胺、十二亚甲基二胺、苯二亚甲基二胺中的一种或几种，从合成效率方面考虑，本发明的二胺优选为己二胺、癸二胺。
所述二元酸包括一种或多种的芳香族二元酸，以及任选的包括一种或多种脂肪族二元酸。对于芳香族二元酸以及脂肪族二元酸没有特别的限定，可以使用本领域中常规的二元酸。在本发明一些优选的实施方案中，所述芳香族二元酸选自碳原子数为8～20的芳香族二元酸，优选为间苯二甲酸、对苯二甲酸、萘二甲酸中的一种或几种，更优选为间苯二甲酸、对苯二甲酸的任一种或二者的任意混合。在本发明一些优选的实施方案中，所述脂肪族二元酸选自碳原子数为4～15脂肪族二元酸，例如可以选自丁二酸、戊二酸、己二酸、辛二酸、壬二酸、癸二酸、十二烷二酸中的一种或几种，更优选为己二酸。本发明中，芳香族二元酸作为必要的组分，并且，在任意需要时，可以使用上述脂肪族二元酸。
在本发明一些优选的事实方案中，所述芳香族二元酸和脂肪族二元酸的摩尔比为100:0～50:50，优选为80:20～55:45。
所述一元羧酸，也没有特别的限定，可以选自本领域制备聚酰胺常用的一元酸。选自碳原子数为2～30的一元酸，其可以为脂肪族一元酸和/或芳香族一元酸，优选为选自乙酸、丙酸、丁酸、戊酸、己酸、辛酸、癸酸、月桂酸、棕榈酸、软脂酸、硬脂酸、苯甲酸或苯乙酸中的一种或几种，进一步优选为乙酸、苯甲酸。
本发明中，对于各种酸的用量，可以进行调节，在本发明一些优选的实施方案中，从提高聚酰胺的热稳定方面考虑，所述一元酸的摩尔数相对于二元酸的总摩尔数为1～5％，优选为2～3％。
封端剂
本发明中使用所述封端剂在能够在缩聚反应中在聚酰胺分子末端产生封端结构。
本发明中，所述封端剂包括由式(I)表示的含有反应基团的缩聚反应催化剂和由式(II)表示的含有反应基团的受阻酚类抗氧化剂。
所述式(I)表示的含有反应基团的缩聚反应催化剂由下述式(I-1)和/或式(I-2)所示化合物组成：
Figure PCTCN2019119738-appb-000005
其中R 1为羧基或羧基取代的C 1～C 10的烷基，包括羧基或羧基取代的C 5～C 10的环烷基，优选为羧基取代的C 1～C 4的烷基；R 2为C 1～C 4的烷基或H，优选为H；R 3选自C 6～C 9的芳香基或H，优选为C 6～C 8的芳香基；M n+选自+1、+2价金属阳离子，优选为Na +、K +；
上述式(I-1)与式(I-2)所示的化合物可以使用一种或同时使用两种，在本发明优选的实施方案中，上述式(I-1)的化合物作为必要的组分。在进一步优选的实施方案中，式(I-1)和式(I-2)所示化合物的摩尔比为10:0～2:8，更优选为10:0～5:5。
式(I-1)和式(I-2)所示化合物的摩尔比为10:0～2:8，优选为10:0～5:5。
对于式(I)结构的化合物的用量，满足单位质量所述半芳香族聚酰胺树脂中总含磷量不高于 200ppm，优选不高于150ppm，更优选不高于90ppm。
所述由式(II)表示的含有反应基团的受阻酚类抗氧化剂的结构为下述所示：
Figure PCTCN2019119738-appb-000006
其中，R 4选自C 1～C 10的烷基，包括C 5～C 10的环烷基，优选为C 1～C 4的烷基。
所述由式(II)表示的含有反应基团的受阻酚类抗氧剂摩尔量为二元酸摩尔量的0.1～2.0％，优选为0.3～1.5％。
其它成分
在不影响本发明效果的情况下，除了上述所公开的组分以外，还可以使用催化剂、各种缩聚助剂、功能性成分或者分子量调节剂等。
对于其它可用的催化剂，可以列举：除了上述式(I)之外的磷基化合物，包括磷酸、亚磷酸、次磷酸和其盐或酯衍生物，如磷酸、亚磷酸或次磷酸，或者磷酸、亚磷酸或次磷酸金属的钠、钾、镁、钒、钙、锌、钴、锰、锡、钨、锗、钛或锑盐；磷酸铵、亚磷酸铵和连二磷酸铵；磷酸、亚磷酸或次磷酸的乙基酯、异丙基酯、丁基酯、己基酯、异癸基酯、十八烷基酯、癸基酯、十八酰基酯或苯基酯等。在优选的实施方案中，对于催化剂，优选地仅使用本发明上述式(I)所表示的催化剂。
聚合物物性
本发明的半芳香族聚酰胺为在缩聚反应后得到的具有活性端基的聚合物，在一些优选的实施方案中，所述活性端基浓度满足：[NH 2]/[COOH]＞5，并且，所述半芳香族聚酰胺树脂中，[COOH]浓度不高于20mmol/kg，优选不高于10mmol/kg。
另外，本发明所述的半芳香族聚酰胺相对于现有技术，具有改进的热稳定性、优异的耐黄变性、以及高的玻璃化转变温度以及熔点。在本发明一些优选的实施方案中，本发明所述的半芳香族聚酰胺具有MV 30/MV 6大于95％，优选大于96％的热稳定性指数，黄度指数小于20，优选小于19，玻璃化转变温度在90℃以上，优选大于95℃，并且熔点在300℃以上。
<第二方面>
本发明的第二方面还提供了一种半芳香族聚酰胺的制备方法。
本发明的第二个目的是提供一种制备上述热稳定半芳香聚酰胺的方法，可以是能实现本发明所述技术方案的任一种的现有技术中存在的方法，例如可以是熔融法、溶液法和固态法等。
优选是以二元胺、二元酸和一元酸为主要原料，加入如上所述的特殊封端剂经过预聚、缩聚而成。再优选是以二元胺、二元酸和一元酸为主要原料，加入特殊封端剂经过成盐、预聚、缩聚反应而成。其中所述缩聚为熔融缩聚或固相缩聚，优选熔融缩聚。
所述一元羧酸和特殊封端剂在成盐、预聚或缩聚反应阶段加入，优选在预聚反应阶段加入。
更具体而言，在本发明所述的方法以二元胺、二元酸和一元酸为主要原料，并在封端剂的存在下进行聚合，所述封端剂为式(I)和式(II)的结构。
对于上述二元胺、二元酸、一元酸以及封端剂的结构与种类与本发明上述第一方面是相同的。
在本发明优选的实施方案中，所述半芳香族聚酰胺的制备方法具体包括以下的反应、过程或步骤：
成盐反应：将二元胺与二元酸按照胺/酸摩尔比小于1的初始投料，与水形成盐溶液；
预聚反应：用二元胺、一元酸以及封端剂来调整反应体系中胺/酸摩尔比至大于1.03，进行预聚反应，得到预聚反应液；
缩聚反应：使用预聚反应液进行缩聚反应。
在本发明进一步优选的实施方案中，所述半芳香族聚酰胺的制备方法具体可以为：
成盐反应(步骤1)：将二元胺与二元酸按照胺酸摩尔比小于1的初始投料，与水形成浆料，浆料经升温、溶解形成盐溶液，其中，优选地，初始投料中胺酸摩尔比为0.90～0.99，更优选为0.92～0.98。
预聚反应(步骤2)：检测所述盐溶液的组成之后，将所述盐溶液脱水，检测脱水装置中出来的蒸汽冷凝水中的二元胺的含量，用二元胺、分子量调节剂一元酸以及封端剂调整胺酸摩尔比至大于1.03，进行预聚反应；
缩聚反应(步骤3)：预聚反应液经减压闪蒸后进行缩聚反应。
在本发明的一个优选的实施方案中，所述步骤1中还包括：检测所述盐溶液中二元酸的组成，通过添加芳香族二元酸和/或脂肪族二元酸以维持二元酸组成稳定的步骤。比如，采用在线拉曼光谱检测得到盐溶液中二元酸的组成，根据检测结果，采用脂肪族二元酸和/或芳香族二元酸浆料来调节盐溶液中的二元酸的组成，使之维持稳定。
在本发明的一个优选的实施方案中，通过在线拉曼光谱检测脱水前的盐溶液中的胺酸摩尔比和脱水装置中出来的蒸汽冷凝水中的二元胺的含量，根据检测结果，用二元胺和分子量调节剂一元酸以及上述封端剂来调整胺酸摩尔比至大于1.03。所述用二元胺和分子量调节剂一元酸以及上述封端剂来调整胺酸摩尔比至大于1.03是指调整后的脂肪族二元胺与脂肪族二元酸、芳香族二元酸、分子量调节剂一元酸以及封端剂之和的胺酸摩尔比控制在大于1.03，优选为1.035～1.07，更优选为1.04～1.06。
在本发明的一个具体实施方案中，半芳香族聚酰胺的生产方法为连续生产方法。比如，采用在线拉曼光谱检测得到盐溶液中二元酸的组成，根据检测结果，采用脂肪族二元酸和/或芳香族二元酸浆料来调节盐溶液中的二元酸的组成，使之维持稳定。并且，通过在线拉曼光谱检测脱水前的物料中的胺酸摩尔比和脱水装置中出来的蒸汽冷凝水中的二元胺的含量，根据检测结果，用二元胺、分子量调节剂一元酸调以及封端剂整胺酸摩尔比至大于1.03。
另外，预聚反应中，脱水阶段脱出的水蒸汽可作为热源用于成盐反应(步骤1)中浆料的升温溶解过程，多余的水蒸汽可在冷凝后与升温工序中产生的冷凝水合并作为补加水用于形成所述浆料的工序。
在本发明的一个优选的实施方案中，在形成成盐反应中所述浆料中，体系的含水量可以为10～50％，优选为15～30％，温度可以为50～95℃，优选为60～90℃。溶解成盐的温度可以为120～170℃，优选为130～160℃。在脱水工序中，脱水的温度可以为180～240℃；压力可以为0.8～1.5MPa；脱水时 间可以为10～30min，优选为15～30min；脱水后的含水量为5～20％，优选为7～15％。
在本发明的一个优选的实施方案中，所述预聚反应温度可以为280～350℃，优选为280～340℃；压力可以为15～30MPa，优选为15～25MPa；反应时间可以为1～15min，优选为2～10min。预聚反应后减压闪蒸压力可以为0.15～0.9MPa，优选为0.2～0.6MPa，温度可以与预聚反应的温度相同。闪蒸后预聚体以熔体方式进入双螺杆挤出机，进行缩聚反应，反应温度可以为290～350℃，优选为310～340℃；反应时间可以为0.5～7min，优选为1～6min。
另外，对于实施本发明上述方法的装置没有特别的限定，可以使用本领域中已有的各种设备以及辅助设施而实现上述生产方法，例如在本发明一些实施方案中，可以使用例如附图3或附图4那样的流程或装置。
<第三方面>
本发明的第三方面中，提供了一种树脂组合物、其制品以及该制品的应用。
本发明的树脂组合物，包括了本发明第一方面的半芳香族聚酰胺或者根据本发明第二方面制备方法而得到的半芳香族聚酰胺。另外，不受限制地，本发明的组合物还可以根据需要包含任选的其他树脂、增强组分、添加剂等。
对于其它树脂，可以为热塑性树脂或热固性树脂，例如可以为聚酯树脂、环氧树脂、聚丙烯酸系树脂、烯烃类弹性体等。尤其地，对于以聚酰胺树脂基体的树脂组合物，可以使用另外的成分以改进聚酰胺树脂的韧性，这些成分可以是如上所述的弹性体，例如基于乙烯和/或二烯烃的共聚物等。并且在一些情况下这些弹性体可以被具有极性基团的取代基所改性。典型地，这些取代基可以源自于酸酐类单体，例如，马来酸酐等。
对于增强组分，本发明的树脂组合物可以使用纤维增强或者无机填料进行增强，所述纤维可以为树脂纤维、碳纤维、无机纤维、矿物纤维等，所述无机填料可以为二氧化硅、二氧化钛、蒙脱土等。并且上述这些组分中的无机成分表面优选通过相容剂进行处理，以增强其与聚酰胺基体的相容性。
对于其它的添加剂等，不受限制地，可以使用本领域中各种加工助剂、抗氧剂、抗静电剂、紫外线吸收剂、润滑剂等。
对于本发明树脂组合物的混合方式，没有特别的限定，可以为各种组分的熔融混合，可以使用密炼机或者开炼机进行共混，或者直接使用挤出机进行共混挤出。
另外，在组合物中存在纤维增强成分的情况下，组合物可以借助溶剂通过浸渍的方法而得到，所述浸渍方法可以使用本领域常规的方法。
进一步，本发明还提供了基于上述组合物的制品，这些制品可以通过注塑、挤出、浸渍等方法得到。优选地，这些制品可以是汽车部件或者电器行业中的部件，具体而言可以是汽车燃油管路部件或者是LED板等。
实施例
为了使本技术领域的技术人员能够更好地理解本发明的技术方案，下面结合实施例，进一步阐述本发明。但应当理解的是，所述实施例仅是本发明的具体方案，不应将其理解为对本发明的限制。实 施例中的百分数，如果没有特殊规定，则为质量百分数。
在实施例和比较例中的诸特性，均是按以下方法测定：
1、特性粘度(Intrinsic Viscosity)
将样品溶解在苯酚-四氯乙烷(质量比3:2)的混合溶解中，得到浓度分别为0.1、0.5、1.0g/dL的溶液，在30℃的恒温水浴环境中，采用乌氏粘度计测量样品的比浓对数粘数η ln。
η ln＝[ln(t/t 0)]/C  (dL/g)
其中t 0为溶剂的流经时间(s)，t为溶液的流经时间(s)，C为样品溶液的浓度(g/dL)。
将η ln的数据外推到浓度为0，即可得到样品的特性粘度[η]。
2、热稳定性表征
本发明所述的热稳定性通过熔体粘度保持率表示，熔体粘度保持率越高，表明树脂热稳定性越好；相反，若熔体粘度保持率越低，则表明树脂热稳定性越差。
(1)熔体粘度保持率
熔体粘度测试在Dynisco公司LCR-7000型毛细管流变仪上进行，口模采用CZ394-20型口模。剪切速率1000s -1，测试温度＝(T m+15)℃。分别测试熔融时间6min和30min时的熔体粘度，记为MV 6和MV 30，则熔体粘度保持率＝MV 30/MV 6。
(2)黄变测试
黄度指数YI是以国际照明委员会的标准为光源、以氧化镁为基准时测得的高分子材料的黄色值。具体测试方法为：用黄度指数仪测定样品在不同温度下放置24h后的黄度指数，以及在60℃放置不同时间的黄度指数，其计算方法如公式所示：
YI＝100(1.28X-1.06Z)/Y
式中，X、Y、Z分别为所测得的三刺激值。
3、熔点测试
熔点测定按照HG/T2235-1991(2012)进行。在20～330℃的温度范围内以10℃/min的加热速率，升温至330℃，保持5min，以20℃/min的降温速率进行测试，将升温时吸热峰的顶点温度作为熔点。
4、末端活性氨基浓度测试
用全自动电位滴定仪滴定样品端胺基含量。取0.5g聚合物，加苯酚45ml及无水甲醇3ml，加热回流，观察试样完全溶解后，冷至室温，用已标定的0.1N盐酸标准溶液滴定端胺基含量。
5、末端活性羧基含量
用全自动电位滴定仪滴定样品端羧基含量。取0.5g聚合物，加入邻甲酚50ml，回流溶解，放冷后迅速加入400μL甲醛溶液，用已标定的KOH-乙醇溶液滴定端羧基含量。
6、拉曼光谱
通过对对苯二甲酸(TA)、间苯二甲酸(IA)、己二酸(AA)、己二胺(HDA)混合成盐后拉曼光谱(附图1、2)的分析研究，本发明采用以下拉曼光谱信息确定各组分的含量：
(1)间苯二甲酸(IA)及其盐(6I)的含量由位于1005cm -1和762cm -1的特征峰确定；
(2)对苯二甲酸(TA)及其盐(6T)的含量由位于1128cm -1和854cm -1的特征峰确定；
(3)已二酸(AA)及其盐(66)的含量由位于920cm -1和936cm -1的特征峰确定；
(4)已二胺(HDA)的含量由位于1485cm -1的特征峰确定。
实施例1-4、比较例1-4均按附图3流程进行实施；实施例5预聚过程按附图3流程进行，缩聚采用固相缩聚；实施例6按附图4流程进行实施。制备过程中，所有物料均采用高纯氮气进行脱氧处理，制备过程的所有装置均由高纯氮气置换并保护。
实施例1
按初始投料胺酸摩尔比0.92的比例，将4.66Kg/h(27.5mol/h)对苯二甲酸、3.29Kg/h(22.5mol/h)己二酸、5.34Kg/h(46.0mol/h)己二胺与3.2Kg/h的水一起投入打浆釜9中，于70℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至160℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.0MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在180℃，含水量控制在13％，脱水停留时间为30min。脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺和0.06Kg/h(1.0mol/h)分子量调节剂乙酸、0.153Kg/h(0.5mol/h)3-(3,5-二叔丁基-4-羟基苯基)戊酸、0.0114Kg/h(90ppmP)P-(4-羧丁基苯基)和P-苯基-次膦酸调整胺酸摩尔比至1.04。然后用泵32增压到15MPa，将物料输送到预热器(热交换器)33中预热升温到290℃，在预聚反应器34中于290℃保温反应15min；预聚反应液经减压阀35减压到0.3MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度290-320℃，反应停留时间6min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约12.4Kg/h得到半芳香族聚酰胺产品。
实施例2
按初始投料胺酸摩尔比0.98的比例，将4.98Kg/h(30mol/h)对苯二甲酸、1.66Kg/h(10mol/h)间苯二甲酸、1.46Kg/h(10mol/h)己二酸、8.43Kg/h(49.0mol/h)癸二胺与5.0Kg/h的水一起投入打浆釜9中，于90℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至170℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.5MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在240℃，含水量控制在10％，脱水停留时间为10min。脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融癸二胺的量；脱水合格的物料分别通过泵17、泵30用熔融癸二胺、0.122Kg/h(1.0mol/h)分子量调节剂苯甲酸、0.0393Kg/h(0.15mol/h)2-(3,5-二叔丁基-4-羟基苯基) 乙酸、0.0079Kg/h(70ppm的P)P-(4-羧乙基苯基)和P-(4-甲基苯基)次膦酸调整胺酸摩尔比至1.06。然后用泵32增压到30MPa，将物料输送到预热器(热交换器)33中预热升温到350℃，在预聚反应器34中于350℃保温反应1min；预聚反应液经减压阀35减压到0.5MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度320-330℃，反应停留时间1min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约15.4Kg/h得到半芳香族聚酰胺产品。
实施例3
按初始投料胺酸摩尔比0.96的比例，将4.98Kg/h(30mol/h)对苯二甲酸、2.92Kg/h(20mol/h)己二酸、5.57Kg/h(48.0mol/h)己二胺与4.0Kg/h的水一起投入打浆釜9中，于80℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至165℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.3MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在220℃，含水量控制在12％，脱水停留时间为20min。脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺和0.09Kg/h(1.5mol/h)分子量调节剂乙酸、0.0725Kg/h(0.25mol/h)2-(3,5-二叔丁基-4-羟基苯基)丁酸、0.0063Kg/h(50ppm的P)P-(4-羧丁基苯基)和P-(3,4-二甲基苯基)次膦酸调整胺酸摩尔比至1.05。然后用泵32增压到25MPa，将物料输送到预热器(热交换器)33中预热升温到320℃，在预聚反应器34中于320℃保温反应3min；预聚反应液经减压阀35减压到0.4MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度310-320℃，反应停留时间3min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约12.2Kg/h得到半芳香族聚酰胺产品。
实施例4
按初始投料胺酸摩尔比0.94的比例，将4.66Kg/h(27.5mol/h)对苯二甲酸、3.29Kg/h(22.5mol/h)己二酸、5.45Kg/h(47.0mol/h)己二胺与3.2Kg/h的水一起投入打浆釜9中，于70℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至160℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.0MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在180℃，含水量控制在13％，脱水停留时间为30min。脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺、0.045Kg/h(0.75mol/h)分子量调节剂乙酸、0.153Kg/h(0.5mol/h)3-(3,5-二叔丁基-4-羟基苯基)戊酸，0.0118Kg/h(90ppmP)P-(4-羧丁基苯基)和 P-苯基-次膦酸(用NaOH中和50％)调整胺酸摩尔比至1.04。然后用泵32增压到15MPa，将物料输送到预热器(热交换器)33中预热升温到290℃，在预聚反应器34中于290℃保温反应15min；预聚反应液经减压阀35减压到0.3MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度290-320℃，反应停留时间6min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约12.4Kg/h得到半芳香族聚酰胺产品。
实施例5
按初始投料胺酸摩尔比0.92的比例，将4.66Kg/h(27.5mol/h)对苯二甲酸、3.29Kg/h(22.5mol/h)己二酸、5.34Kg/h(46.0mol/h)己二胺与3.2Kg/h的水一起投入打浆釜9中，于70℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至160℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.0MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在180℃，含水量控制在13％，脱水停留时间为30min。脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺和0.06Kg/h(1.0mol/h)分子量调节剂乙酸、0.153Kg/h(0.5mol/h)3-(3,5-二叔丁基-4-羟基苯基)戊酸、0.0118Kg/h P-(4-羧丁基苯基)和P-苯基-次膦酸(用NaOH中和50％，90ppm的P)调整胺酸摩尔比至1.04。然后用泵32增压到15MPa，将物料输送到预热器(热交换器)33中预热升温到290℃，在预聚反应器34中于290℃保温反应15min；预聚反应液经减压阀35减压到0.7MPa后进入闪蒸器36中。闪蒸后熔融液体物料经喷雾干燥，得到预聚体，预聚体在耙式干燥机中于200～250℃进行固相缩聚反应20h，以约12.4Kg/h得到半芳香族聚酰胺产品。
实施例6
按初始投料胺酸摩尔比1.04的比例，将49.8Kg(300mol)对苯二甲酸、16.6Kg(100mol)间苯二甲酸、14.6Kg(100mol)己二酸、92.2Kg(536mol)癸二胺、0.6Kg(10mol)分子量调节剂乙酸、1.53Kg(5mol)3-(3,5-二叔丁基-4-羟基苯基)戊酸、0.118Kg P-(4-羧丁基苯基)和P-苯基-次膦酸(用NaOH中和50％，90ppm的P)与50Kg的水一起投入成盐釜41或42(每5小时切换一次)中加热升温至170℃溶解成盐；上述盐溶液以19.0Kg/h流量由泵43增压到2.0MPa后输送到脱水器的预热器44之前与循环泵45输送的物料混合后进行升温，在脱水器46中脱水，脱水温度控制在260℃，含水量控制在5％，脱水停留时间为10min；脱水合格的物料用泵48增压到27MPa，将物料输送到预热器49中预热升温到320℃，在预聚反应器50中于320℃保温反应3min；预聚反应液经减压阀51减压到0.9MPa后进入闪蒸器52中，闪蒸熔融液体物料经减压阀53减压到常压后进入双螺杆挤出机54中进行缩聚反应，反应温度320-330℃，反应停留时间3min；经缩聚反应的物料在水下造粒机55中进行造粒，再经干燥机56干燥，以约12.6Kg/h得到半芳香族聚酰胺产品。
对比例1
按初始投料胺酸摩尔比0.92的比例，将4.66Kg/h(27.5mol/h)对苯二甲酸、3.29Kg/h(22.5mol/h)己二酸、5.34Kg/h(46.0mol/h)己二胺、0.0024Kg/h次磷酸(用NaOH中和50％，折合90ppmP)与3.2Kg/h的水一起投入打浆釜9中，于70℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至160℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.0MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在180℃，含水量控制在13％，脱水停留时间为30min。将从脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺和0.03Kg/h(0.5mol/h)分子量调节剂乙酸调整胺酸摩尔比至1.04。然后用泵32增压到15MPa，将物料输送到预热器(热交换器)33中预热升温到290℃，在预聚反应器34中于290℃保温反应15min；预聚反应液经减压阀35减压到0.3MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度290～320℃，反应停留时间6min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约12.4Kg/h得到半芳香族聚酰胺产品。
对比例2
按初始投料胺酸摩尔比0.98的比例，将4.98Kg/h(30mol/h)对苯二甲酸、1.66Kg/h(10mol/h)间苯二甲酸、1.46Kg/h(10mol/h)己二酸、8.43Kg/h(49.0mol/h)癸二胺、0.0019Kg/h次磷酸(70ppm的P)与5.0Kg/h的水一起投入打浆釜9中，于90℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至170℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.5MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在240℃，含水量控制在10％，脱水停留时间为10min。将从脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融癸二胺的量；脱水合格的物料分别通过泵17、泵30用熔融癸二胺和0.122Kg/h(1.0mol/h)分子量调节剂苯甲酸调整胺酸摩尔比至1.06。然后用泵32增压到30MPa，将物料输送到预热器(热交换器)33中预热升温到350℃，在预聚反应器34中于350℃保温反应1min；预聚反应液经减压阀35减压到0.5MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度320～330℃，反应停留时间1min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约15.3Kg/h得到半芳香族聚酰胺产品。
对比例3
按初始投料胺酸摩尔比0.92的比例，将4.66Kg/h(27.5mol/h)对苯二甲酸、3.29Kg/h(22.5mol/h)己二酸、5.34Kg/h(46.0mol/h)己二胺与3.2Kg/h的水一起投入打浆釜9中，于70℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至160℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.0MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在180℃，含水量控制在13％，脱水停留时间为30min。将从脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺和0.03Kg/h(0.5mol/h)分子量调节剂乙酸、0.153Kg/h(0.5mol/h)3-(3,5-二叔丁基-4-羟基苯基)戊酸调整胺酸摩尔比至1.04。然后用泵32增压到15MPa，将物料输送到预热器(热交换器)33中预热升温到290℃，在预聚反应器34中于290℃保温反应15min；预聚反应液经减压阀35减压到0.3MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度290～320℃，反应停留时间6min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约12.4Kg/h得到半芳香族聚酰胺产品。
对比例4
按初始投料胺酸摩尔比0.92的比例，将4.66Kg/h(27.5mol/h)对苯二甲酸、3.29Kg/h(22.5mol/h)己二酸、5.34Kg/h(46.0mol/h)己二胺与3.2Kg/h的水一起投入打浆釜9中，于70℃连续打浆形成浆料。浆料经泵10输送到多级搅拌溶解釜14中用脱水过程中产生的蒸汽加热升温至160℃溶解成盐。根据在线拉曼光谱18检测盐溶液中二元酸的组成，通过计量泵23采用熔融己二酸调节脂肪族二元酸的量，使溶解成盐釜19中芳香族二元酸与脂肪族二元酸的比例维持稳定。上述盐溶液经在线拉曼光谱20检测组成后，由泵24增压到1.0MPa后输送到脱水器的预热器(热交换器)27之前与循环泵28输送的物料混合后进行升温，在脱水器29中脱水，脱水温度控制在180℃，含水量控制在13％，脱水停留时间为30min。将从脱水器出来的蒸汽作为多级搅拌溶解釜14的热源，通过热交换器15冷却后，由在线拉曼光谱16检测其中的胺含量。结合拉曼光谱16及20的检测结果，通过控制器21确定泵32之前所需补充熔融己二胺的量；脱水合格的物料分别通过泵17、泵30用熔融己二胺和0.03Kg/h(0.5mol/h)分子量调节剂乙酸、0.0118Kg/h P-(4-羧丁基苯基),P-苯基-次膦酸(用NaOH中和50％，90ppm的P)调整胺酸摩尔比至1.04。然后用泵32增压到15MPa，将物料输送到预热器(热交换器)33中预热升温到290℃，在预聚反应器34中于290℃保温反应15min；预聚反应液经减压阀35减压到0.3MPa后进入闪蒸器36中。闪蒸后熔融液体物料经减压阀37减压到常压后进入双螺杆挤出机38中进行缩聚反应，反应温度290～320℃，反应停留时间6min。经缩聚反应的物料在水下造粒机39中进行造粒，再经干燥机40干燥，以约12.4Kg/h得到半芳香族聚酰胺产品。
表1
Figure PCTCN2019119738-appb-000007
由表1的结果可知，相比单独添加次磷酸催化剂或不加含磷催化剂所获得的半芳香聚酰胺，添加本发明封端剂所得聚酰胺能够保持良好的热稳定性，黄度指数比较低，且同时添加特殊封端剂和含反应基团的受阻酚类抗氧化剂比仅仅添加其中一种能够得到热稳定性能更好的聚酰胺。

Claims (20)

  1. 一种半芳香族聚酰胺，其特征在于，具有源自于二元胺、二元酸和一元酸的结构单元，及其具有源自下式(I)和式(II)的封端结构，
    其中：
    所述式(I)选自下述式(I-1)和/或式(I-2)所示化合物：
    Figure PCTCN2019119738-appb-100001
    其中R 1为羧基或羧基取代的C 1～C 10的烷基，优选为羧基取代的C 1～C 4的烷基；R 2为C 1～C 4的烷基或H，优选为H；R 3选自C 6～C 9的芳香基或H，优选为C 6～C 8的芳香基；M n+选自+1、+2价金属阳离子；
    所述式(II)为：
    Figure PCTCN2019119738-appb-100002
    其中R 4选自C 1～C 10的烷基，优选为C 1～C 4的烷基。
  2. 根据权利要求1所述的半芳香族聚酰胺，其特征在于，所述金属阳离子为Na +或K +。
  3. 根据权利要求1或2所述的半芳香族聚酰胺，其特征在于，单位质量所述半芳香族聚酰胺树脂中总磷量不高于200ppm，优选不高于150ppm，更优选不高于90ppm。
  4. 根据权利要求1～3任一项所述的半芳香族聚酰胺，其特征在于，所述式(I-1)和式(I-2)所示化合物的摩尔比为10:0～2:8，优选为10:0～5:5。
  5. 根据权利要求1～4任一项所述的半芳香族聚酰胺，其特征在于，源自所述式(II)结构的摩尔量为源自二元酸结构的摩尔量的0.1～2.0％，优选为0.3～1.5％。
  6. 根据权利要求1～5任一项所述的半芳香族聚酰胺，其特征在于，源自所述一元酸结构的摩尔数相对于源自所述二元酸结构的总摩尔数为1～5％，优选为2～3％。
  7. 根据权利要求1～6任一项所述的半芳香族聚酰胺，其特征在于，所述二元酸包括芳香族二元酸、以及任选的脂肪族二元酸的一种或多种，所述芳香族二元酸和脂肪族二元酸的摩尔比为100:0～50:50，优选为80:20～55:45。
  8. 根据权利要求1～7任一项所述的半芳香族聚酰胺，其特征在于，所述半芳香族聚酰胺树脂具 有活性端基，且活性端基浓度满足：[NH 2]/[COOH]＞5，并且，所述半芳香族聚酰胺树脂中，[COOH]浓度不高于20mmol/kg，优选不高于10mmol/kg。
  9. 根据权利要求1～8任一项所述的半芳香族聚酰胺，其特征在于，具有MV 30/MV 6大于95％的热稳定性指数，黄度指数小于20，玻璃化转变温度在90℃以上，熔点在300℃以上。
  10. 一种半芳香族聚酰胺的制备方法，其特征在于，所述方法以二元胺、二元酸和一元酸为主要原料，并在封端剂的存在下进行聚合，所述封端剂为以下式(I)和式(II)的结构，
    其中：
    所述式(I)选自下述式(I-1)和/或式(I-2)所示化合物：
    Figure PCTCN2019119738-appb-100003
    其中R 1为羧基或羧基取代的C 1～C 10的烷基，优选为羧基取代的C 1～C 4的烷基；R 2为C 1～C 4的烷基或H，优选为H；R 3选自C 6～C 9的芳香基或H，优选为C 6～C 8的芳香基；M n+选自+1、+2价金属阳离子；
    所述式(II)为：
    Figure PCTCN2019119738-appb-100004
    其中，R 4选自C 1～C 10的烷基，优选为C 1～C 4的烷基。
  11. 根据权利要求10所述的方法，其特征在于，包括：
    成盐反应：将二元胺与二元酸按照胺/酸摩尔比小于1的初始投料，与水形成盐溶液；
    预聚反应：用二元胺、一元酸以及封端剂调整反应体系中胺/酸摩尔比至大于1.03，进行预聚反应，得到预聚反应液；
    缩聚反应：使用预聚反应液进行缩聚反应。
  12. 根据权利要求11所述的方法，其特征在于，所述成盐反应中，初始投料的胺酸摩尔比为0.90～0.99，优选为0.92～0.98。
  13. 根据权利要求11或12所述的方法，其特征在于，所述成盐反应中还包括：检测所述盐溶液中二元酸的组成，通过添加芳香族二元酸和/或脂肪族二元酸以维持二元酸组成稳定；所述预聚反应中还包括所述检测预聚反应体系组成，所述检测均采用在线拉曼光谱进行。
  14. 根据权利要求11～13任一项所述的方法，其特征在于，所述预聚反应中的胺/酸摩尔比为1.03～1.07，优选为1.04～1.06。
  15. 根据权利要求11～14任一项所述的方法，其特征在于，所述预聚反应前还包括对所述成盐溶液进行脱水处理，所述脱水的温度为180～240℃，压力为0.8～1.5MPa，脱水时间为10～30min；预聚反应的温度为280～350℃，压力为15～30MPa，反应时间为1～15min；缩聚反应的反应温度为290～350℃，反应时间为0.5～7min。
  16. 根据权利要求15所述的方法，其特征在于，所述脱水处理产生的水蒸汽可作为热源用于所述浆料的升温、溶解，多余水蒸汽可在冷凝后与升温工序中产生的冷凝水合并作为补加水用于形成所述浆料的工序。
  17. 一种树脂组合物，其特征在于，其包括：
    根据权利要求1～9任一项所述的半芳香族聚酰胺，或者根据权利要求10～16任一项所述的方法得到的半芳香族聚酰胺，以及任选的其它树脂、增强组分或添加剂。
  18. 一种制品，其特征在于，其由根据权利要求17所述的组合物制备而得到。
  19. 根据权利要求18所述的制品，其为汽车部件或电器行业用部件。
  20. 根据权利要求18所述的制品，其为汽车燃油管路零部件或LED板。
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