Polyphenyl ether polymerization reaction process

Abstract

The invention belongs to the technical field of polyphenyl ether polymerization reaction, particularly relates to a polyphenyl ether polymerization reaction process, and provides the following scheme aiming at the problems that stirring is needed in the polyphenyl ether polymerization reaction in the prior art, the explosion risk is easily caused by stirring in a polymerization sleeve, the tail gas treatment effect is poor, and air pollution is caused by emission. The method comprises the following steps: S1, preparing reaction equipment and raw materials; the reaction equipment comprises a catalyst batching kettle, a catalyst metering pump, a raw material batching kettle, a raw material conveying pump, a polymerization sleeve reactor, a tail gas cooler, a gas-liquid separation tank, an extraction tower feeding pump, a turntable extraction tower and a tail gas processor. No stirrer is arranged in the polymerization sleeve reactor, the explosion risk of materials caused by mechanical friction of the stirrer is completely eradicated, tail gas is sequentially subjected to cooling, acid-base neutralization reaction and peculiar smell removal treatment, the tail gas can be further treated, and air pollution is avoided.

Description

Technical Field

[0001] The invention relates to the technical field of polyphenylene ether polymerization reaction, in particular to a polyphenylene ether polymerization reaction process. Background Art

[0002] The synthesis of polyphenylene ether by precipitation polycondensation is that 2,6-dimethylphenol is catalyzed by copper-amine complex, and then oxidized, coupled, and polymerized in toluene solvent to obtain a crude product, and then extracted, precipitated, washed powder, dried, etc. to obtain a polypropyl ether product.

[0003] Oxidation, coupling and polymerization reactions are carried out in an intermittent reactor. The raw material 2,6-dimethylphenol is heated to become a liquid phase and then fully mixed with the toluene solution, and then slowly injected into the reactor with a metering pump. The catalyst copper chloride and complex amine are fully mixed with the toluene solution in the mixing tank and added to the reactor. At the same time, oxygen is bubbled into the bottom of the reactor, and stirring is turned on to allow the materials to fully react. After reacting for 3-4 hours, the materials are discharged. Since the oxidative coupling reaction is an exothermic reaction, in order to suppress side reactions, the polymerization reaction temperature is controlled to be maintained at about 25°C, and an external circulation heat extraction method is adopted, that is, part of the reaction mixture is extracted from the bottom of the kettle and returned from the top of the reactor after being heated with cold water. The extraction and separation of the reaction product is carried out in an extraction kettle, which is an intermittent operation equipment with a stirrer. The extractant and the reaction product are added to the extraction kettle respectively, stirred and then allowed to stand, and then the crude polyphenylene ether product without solvent is obtained by phase separation.

[0004] The prior art polyphenylene ether polymerization reaction requires stirring, and stirring in the polymerization casing is prone to explosion risk, and the exhaust gas treatment effect is poor, and the emission will cause air pollution. Summary of the invention

[0005] The purpose of the present invention is to solve the shortcomings of the prior art that the polymerization reaction of polyphenylene ether requires stirring, stirring in a polymerization sleeve is prone to explosion risk, the treatment effect of tail gas is poor, and the discharge will cause air pollution, and a polyphenylene ether polymerization reaction process is proposed.

[0006] In order to achieve the above object, the present invention adopts the following technical solutions:

[0007] A polyphenylene ether polymerization process comprises the following steps:

[0008] S1: Prepare reaction equipment and raw materials; the reaction equipment includes: catalyst batching kettle, catalyst metering pump, raw material batching kettle, raw material delivery pump, polymerization sleeve reactor, tail gas cooler, gas-liquid separation tank, extraction tower feed pump, rotary extraction tower, tail gas processor; reaction raw materials include: 2-6-dimethylphenol, toluene, catalyst;

[0009] S2: The device is connected and powered on;

[0010] S3: start reaction work;

[0011] S4: Product testing;

[0012] S5: Equipment cleaning and maintenance.

[0013] Preferably, in S2, an outer ring tube is provided on the outer side of the polymerization jacket reactor.

[0014] Preferably, in S2, the catalyst batching kettle is connected to the polymerization jacket reactor via a catalyst metering pump and an outer ring pipe, and the raw material batching kettle is connected to the polymerization jacket reactor via a raw material delivery pump and an outer ring pipe.

[0015] Preferably, in S2, the polymerization tube reactor is connected with the tail gas cooler and the gas-liquid separation tank, the gas-liquid separation tank is connected with the rotary disc extraction tower through the extraction tower feed pump, and the tail gas cooler is connected with the tail gas processor.

[0016] Preferably, in S3, the reaction comprises the following steps:

[0017] First, 2-6-dimethylphenol and toluene are mixed in a raw material batching kettle, and the mixed raw materials are pumped to the bottom of the outer ring tube of the polymerization tube reactor through a raw material delivery pump, and enter the outer ring tube in the direction of the circulation;

[0018] Second, the catalyst is added to the catalyst batching kettle for mixing, the prepared catalyst is injected into the mixed raw materials through the catalyst metering pump, and oxygen is injected into the rising section of the outer ring tube. The medium in the outer ring tube forms a fluid under the pressure of the injected medium and returns to the polymerization sleeve reactor;

[0019] Third, oxidation, coupling and polymerization reactions are carried out in the outer loop and the reactor. The reaction products enter the polymerization tube reactor from the outer loop in a tangential direction. After rotation and separation, the reaction products with high density are deposited at the bottom of the reactor, and the materials with low density re-enter the outer loop of the reactor in the middle of the reactor to form a circulating flow.

[0020] Fourth, the outer ring tube is wrapped with a tube sleeve, and a cooling medium is passed into the tube sleeve to maintain the reaction temperature at about 25°C and inhibit the occurrence of side reactions;

[0021] Fifth, the tail gas from the polymerization tube reactor enters the tail gas cooler for cooling, and the uncooled tail gas is sent to the tail gas processor for treatment;

[0022] Sixth, the reaction product flows from the bottom of the polymerization sleeve reactor to the gas-liquid separation tank, stands in the gas-liquid separation tank, and after the dissolved oxygen is separated, the reaction product is pumped to the upper part of the rotary extraction tower through the extraction tower feed pump. Before entering the rotary extraction tower, the inhibitor solution is injected, and the extractant is injected into the lower part of the rotary extraction tower. The extractant dissolved with toluene is discharged from the top of the rotary extraction tower, and the final product PPE is discharged from the bottom of the rotary extraction tower.

[0023] Preferably, the catalyst batching kettle and the raw material batching kettle are both provided with a stirrer, the working time of the stirrer is 20-30min, the speed of the stirrer is 200-300r / min, and the stirring temperature is 20-25°C.

[0024] Preferably, the exhaust gas processor includes an exhaust gas treatment box, and a plurality of partitions are arranged in the exhaust gas treatment box. The plurality of partitions divide the treatment box into a cooling zone, an acid liquid zone, an alkaline liquid zone, and an odor adsorption zone. The cooling zone is connected with an exhaust gas inlet pipe, and the exhaust gas inlet pipe is connected with the exhaust gas cooler. The cooling zone, the acid liquid zone, the alkaline liquid zone, and the odor adsorption zone are connected to each other through a bend pipe, and an exhaust pipe is arranged on the right side of the exhaust gas treatment box.

[0025] Preferably, coolant, acid, alkali and activated carbon particles are arranged in sequence inside the cooling zone, acid zone, alkali zone and odor adsorption zone; a metal mesh is arranged in the odor adsorption zone, and the activated carbon particles are placed on the top of the metal mesh; a box cover is reserved for the exhaust gas treatment box located in the odor adsorption zone; three discharge pipes are arranged on the outside of the exhaust gas treatment box, and the three discharge pipes are respectively connected to the cooling zone, acid zone and alkali zone.

[0026] Preferably, in S4, the obtained product is tested, and the reaction time or the amount of raw materials or catalyst added is adjusted according to the test result.

[0027] Preferably, in S5, the catalyst batching kettle, catalyst metering pump, raw material batching kettle, raw material delivery pump, polymerization sleeve reactor, tail gas cooler, gas-liquid separation tank, extraction tower feed pump, turntable extraction tower, and tail gas processor are cleaned and maintained.

[0028] In the present invention, the beneficial effects of the polyphenylene ether polymerization process are:

[0029] The reaction process of the present invention is a continuous feeding and continuous discharging process, which eliminates the loading and unloading procedures of the traditional intermittent reactor and greatly improves the production efficiency.

[0030] The polymerization sleeve reactor of the present invention does not have an agitator. In the sleeve rising section, as oxygen is introduced, the materials are fully mixed while reacting in the sleeve, eliminating the risk of explosion of the materials due to mechanical friction of the agitator. The reaction product is finally deposited at the bottom of the reactor and flows to the gas-liquid separation tank by gravity, and oxygen is separated by standing, eliminating the transportation of oxygen-containing materials and reducing the explosion risk of the process. This process does not require the setting of a reaction product circulation pump and a cooler, simplifying the production process. The sleeve heat exchange process adopted in this process can accurately control the reaction temperature, prevent the reactor from overheating, and effectively inhibit the occurrence of side reactions.

[0031] The present invention realizes the preliminary separation of reaction products inside the reactor, and the unreacted materials circulate between the outer ring pipe of the reactor and the reactor, thereby improving the conversion rate of the reaction, greatly reducing the catalyst and unreacted materials carried by the reaction products entering the gas-liquid separator, and reducing the load of subsequent processing steps.

[0032] The extraction and separation of the reaction product of the present invention is a continuous process. The rotary disc extraction tower can realize the continuous addition of the reaction product and the extractant, and the continuous discharge of the extracted product, thereby ensuring the continuity and stability of the production process. The rotary disc extraction tower significantly improves the mass transfer efficiency of the extraction process by increasing the interphase contact area and the mass transfer coefficient, which enables the extraction process to be completed faster under the same conditions and improves the production efficiency.

[0033] The present invention sequentially cools the tail gas, performs acid-base neutralization reaction and removes odor, and can further process the tail gas to avoid air pollution. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 This is a schematic diagram of equipment connection for a polyphenylene ether polymerization process proposed by the present invention;

[0035] Figure 2 This is a schematic diagram of the structure of the exhaust gas treatment box proposed by the present invention;

[0036] Figure 3 This is a schematic cross-sectional view of the exhaust gas treatment box proposed by the present invention;

[0037] Figure 4 The present invention provides a flow chart of a polyphenylene ether polymerization process.

[0038] In the figure: 1. catalyst batching kettle; 2. catalyst metering pump; 3. raw material batching kettle; 4. raw material delivery pump; 5. polymerization sleeve reactor; 6. tail gas cooler; 7. gas-liquid separation tank; 8. extraction tower feed pump; 9. turntable extraction tower; 10. tail gas processor; 101. tail gas treatment box; 102. tail gas inlet pipe; 103. partition; 104. cooling zone; 105. acid zone; 106. alkali zone; 107. odor adsorption zone; 108. metal mesh; 109. piston carbon particles; 112. exhaust pipe; 113. discharge pipe; 114. box cover. DETAILED DESCRIPTION

[0039] The technical solution of this embodiment will be clearly and completely described below in conjunction with the drawings in this embodiment. Obviously, the described embodiment is only a part of this embodiment, rather than all of the embodiments.

[0040] Embodiment 1

[0041] Reference Figure 1 and Figure 4 , a polyphenylene ether polymerization process, comprising the following steps:

[0042] S1: Prepare reaction equipment and raw materials; the reaction equipment includes: catalyst batching kettle 1, catalyst metering pump 2, raw material batching kettle 3, raw material delivery pump 4, polymerization sleeve reactor 5, tail gas cooler 6, gas-liquid separation tank 7, extraction tower feed pump 8, rotary disc extraction tower 9, tail gas processor 10; reaction raw materials include: 2-6-dimethylphenol, toluene, catalyst;

[0043] S2: The device is connected and powered on;

[0044] S3: start reaction work;

[0045] S4: Product testing;

[0046] S5: Equipment cleaning and maintenance.

[0047] In this embodiment, in S2, an outer ring tube is arranged on the outer side of the polymerization tube reactor 5.

[0048] In this embodiment, in S2, the catalyst batching kettle 1 is connected to the polymerization jacket reactor 5 through the catalyst metering pump 2 and the outer ring pipe, and the raw material batching kettle 3 is connected to the polymerization jacket reactor 5 through the raw material delivery pump 4 and the outer ring pipe.

[0049] In this embodiment, in S2, the polymerization shell and tube reactor 5 is connected with the tail gas cooler 6 and the gas-liquid separation tank 7, the gas-liquid separation tank 7 is connected with the rotary disc extraction tower 9 through the extraction tower feed pump 8, and the tail gas cooler 6 is connected with the tail gas processor 10.

[0050] In this embodiment, in S3, the reaction work includes the following steps:

[0051] First, 2-6-dimethylphenol and toluene are mixed in a raw material batching kettle 3, and the mixed raw materials are delivered to the bottom of the outer ring tube of the polymerization sleeve reactor 5 through a raw material delivery pump 4, and enter the outer ring tube in the direction of the circulation;

[0052] Second, the catalyst is added to the catalyst batching kettle 1 for mixing, the prepared catalyst is injected into the mixed raw materials through the catalyst metering pump 2, and oxygen is injected into the rising section of the outer ring tube. The medium in the outer ring tube forms a fluid under the pressure of the injected medium and returns to the polymerization sleeve reactor 5;

[0053] Third, oxidation, coupling and polymerization reactions are carried out in the outer loop and the reactor. The reaction products enter the polymerization sleeve reactor 5 from the outer loop in a tangential direction, and after rotational separation, the reaction products with high density are deposited at the bottom of the reactor, and the materials with low density re-enter the outer loop of the reactor in the middle of the reactor to form a circulating flow.

[0054] Fourth, the outer ring tube is wrapped with a tube sleeve, and a cooling medium is passed into the tube sleeve to maintain the reaction temperature at about 25°C and inhibit the occurrence of side reactions;

[0055] Fifth, the tail gas from the polymerization tube reactor 5 enters the tail gas cooler 6 for cooling, and the uncooled tail gas is sent to the tail gas processor 10 for treatment;

[0056] Sixth, the reaction product flows from the bottom of the polymerization sleeve reactor to the gas-liquid separation tank 7, stands in the gas-liquid separation tank 7, and after the dissolved oxygen is separated, the reaction product is sent to the upper part of the rotary extraction tower 9 through the extraction tower feed pump 8. Before entering the rotary extraction tower 9, the inhibitor solution is injected, and the extractant is injected into the lower part of the rotary extraction tower 9. The extractant dissolved with toluene is discharged from the top of the rotary extraction tower 9, and the final product PPE is discharged from the bottom of the rotary extraction tower 9.

[0057] In this embodiment, a stirrer is provided in the catalyst batching kettle 1 and the raw material batching kettle 3. The working time of the stirrer is 20 min, the speed of the stirrer is 200 r / min, and the stirring temperature is 20°C.

[0058] In this embodiment, in S4, the obtained product is tested, and the reaction time or the amount of raw materials and catalyst added is adjusted according to the test results.

[0059] In this embodiment, in S5, the catalyst batching kettle 1, the catalyst metering pump 2, the raw material batching kettle 3, the raw material delivery pump 4, the polymerization sleeve reactor 5, the exhaust gas cooler 6, the gas-liquid separation tank 7, the extraction tower feed pump 8, the turntable extraction tower 9, and the exhaust gas processor 10 are cleaned and maintained.

[0060] Embodiment 2

[0061] Reference Figure 2 and Figure 3 The rest of the second embodiment is the same as the first embodiment, except that:

[0062] In this embodiment, the exhaust gas processor 10 includes an exhaust gas treatment box 101, and a plurality of partitions 103 are arranged in the exhaust gas treatment box 101. The plurality of partitions 103 divide the treatment box 101 into a cooling zone 104, an acid liquid zone 105, an alkaline liquid zone 106, and an odor adsorption zone 107. The cooling zone 104 is connected to an exhaust gas inlet pipe 102, and the exhaust gas inlet pipe 102 is connected to the exhaust gas cooler 6. The cooling zone 104, the acid liquid zone 105, the alkaline liquid zone 106, and the odor adsorption zone 107 are connected to each other through a bend pipe 111, and an exhaust pipe 112 is arranged on the right side of the exhaust gas treatment box 101.

[0063] Specifically, the exhaust gas enters the exhaust gas treatment box 101 through 102, and the exhaust gas enters the cooling zone 104 to cool the exhaust gas, and then enters the acid solution zone 105 and the alkali solution zone 106 in sequence through the bent pipe 111 for neutralization reaction, and then passes through the odor adsorption zone 107 for exhaust gas odor adsorption.

[0064] In the present embodiment, coolant, acid, alkali and activated carbon particles 109 are arranged in sequence inside the cooling zone 104, the acid zone 105, the alkali zone 106 and the odor adsorption zone 107. A metal mesh 108 is arranged in the odor adsorption zone 107, and the activated carbon particles 109 are placed on the top of the metal mesh 108. The exhaust gas treatment box 101 is located in the odor adsorption zone 107 and is provided with a box cover 114. Three discharge pipes 113 are arranged on the outside of the exhaust gas treatment box 101, and the three discharge pipes 113 are respectively connected to the cooling zone 104, the acid zone 105 and the alkali zone 106.

[0065] Specifically, the metal mesh 108 is used to support the activated carbon particles. The activated carbon particles can be replaced by opening the box cover 114, and the coolant, acid solution, alkali solution, etc. can be discharged through the three discharge pipes 113.

[0066] Embodiment 3

[0067] Reference Figure 4 The rest of the third embodiment is the same as the first and second embodiments, except that:

[0068] In this embodiment, in S2, two sets of outer ring tubes are arranged outside the polymerization tube reactor 5.

[0069] In this embodiment, in S2, the catalyst batching kettle 1 is connected to the polymerization sleeve reactor 5 through a catalyst metering pump 2 and a group of outer ring pipes, and the raw material batching kettle 3 is connected to the polymerization sleeve reactor 5 through a raw material delivery pump 4 and another group of outer ring pipes.

[0070] In this embodiment, in order to improve the reaction conversion rate, another set of outer loops is provided in the lower part of the polymerization sleeve reactor 5, and the catalyst and oxygen are respectively introduced into the bottom of the outer loops, and the circulating flow formed in the loops is also returned to the polymerization sleeve reactor 5 in a tangential direction. Since the oxidative coupling reaction is an exothermic reaction, a sleeve is provided outside the outer loop, and a cooling medium is introduced into the sleeve to maintain the reaction temperature at about 25°C to inhibit the occurrence of side reactions.

[0071] Embodiment 4

[0072] The remaining parts of the fourth embodiment are the same as those of the first embodiment, the second embodiment and the third embodiment, except that:

[0073] Agitators are provided in the catalyst batching kettle 1 and the raw material batching kettle 3. The working time of the agitators is 30 min, the speed of the agitators is 300 r / min, and the stirring temperature is 25°C.

[0074] Embodiment 5

[0075] The remaining parts of the fourth embodiment are the same as those of the first embodiment, the second embodiment and the third embodiment, except that:

[0076] Agitators are provided in the catalyst batching kettle 1 and the raw material batching kettle 3. The working time of the agitators is 25 min, the speed of the agitators is 250 r / min, and the stirring temperature is 23°C.

[0077] Experimental example

[0078] Product qualification rate Exhaust gas treatment effect Embodiment 1 91％ 70％ Embodiment 2 92％ 90％ Embodiment 3 94％ 91％ Embodiment 4 93％ 91％ Embodiment 5 93.5％ 89％

[0079] In summary, by comparing embodiments 1, 2, 3, 4 and 5, embodiment 3 is the best embodiment.

[0080] The above description is only a preferred specific implementation manner of this embodiment, but the protection scope of this embodiment is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes according to the technical scheme and inventive concept of this embodiment within the technical scope disclosed in this embodiment, and they should be covered by the protection scope of this embodiment.

Claims

1. A polyphenylene ether polymerization process, characterized in that: The following steps are involved: S1: Prepare reaction equipment and raw materials; the reaction equipment includes: a catalyst batching kettle (1), a catalyst metering pump (2), a raw material batching kettle (3), a raw material delivery pump (4), a polymerization sleeve reactor (5), an exhaust gas cooler (6), a gas-liquid separation tank (7), an extraction tower feed pump (8), a rotary disc extraction tower (9), and an exhaust gas processor (10); the reaction raw materials include: 2-6-dimethylphenol, toluene, and a catalyst; S2: The device is connected and powered on; S3: start reaction work; S4: Product testing; S5: Equipment cleaning and maintenance.

2. A polyphenylene ether polymerization process according to claim 1, characterized in that: In the above S2, an outer ring tube is arranged on the outer side of the polymerization jacket reactor (5).

3. A polyphenylene ether polymerization process according to claim 1, characterized in that: In the S2, the catalyst batching kettle (1) is connected to the polymerization jacket reactor (5) via a catalyst metering pump (2) and an outer ring pipe, and the raw material batching kettle (3) is connected to the polymerization jacket reactor (5) via a raw material delivery pump (4) and an outer ring pipe.

4. A polyphenylene ether polymerization process according to claim 1, characterized in that: In the S2, the polymerization tube reactor (5) is connected to the tail gas cooler (6) and the gas-liquid separation tank (7), the gas-liquid separation tank (7) is connected to the rotary disc extraction tower (9) through the extraction tower feed pump (8), and the tail gas cooler (6) is connected to the tail gas processor (10).

5. A polyphenylene ether polymerization process according to claim 1, characterized in that: In said S3, the reaction work comprises the following steps: First, 2-6-dimethylphenol and toluene are mixed in a raw material batching kettle (3), and the mixed raw materials are sent to the bottom of the outer ring tube of the polymerization tube reactor (5) through a raw material delivery pump (4) and enter the outer ring tube in the direction of the circulation; Second, the catalyst is added to the catalyst batching kettle (1) for mixing, the prepared catalyst is injected into the mixed raw materials through the catalyst metering pump (2), and oxygen is injected into the rising section of the outer ring tube. The medium in the outer ring tube forms a fluid under the pressure of the injected medium and returns to the polymerization sleeve reactor (5); Third, oxidation, coupling and polymerization reactions are carried out in the outer loop and the reactor. The reaction products enter the polymerization tube reactor (5) from the outer loop in a tangential direction, and are separated by rotation. The reaction products with high density are deposited at the bottom of the reactor, and the materials with low density re-enter the outer loop of the reactor in the middle of the reactor to form a circulating flow. Fourth, the outer ring tube is wrapped with a tube sleeve, and a cooling medium is passed into the tube sleeve to maintain the reaction temperature at about 25°C and inhibit the occurrence of side reactions; Fifth, the tail gas from the polymerization tube reactor (5) enters the tail gas cooler (6) for cooling, and the uncooled tail gas is sent to the tail gas processor (10) for treatment; Sixth, the reaction product flows from the bottom of the polymerization sleeve reactor to the gas-liquid separation tank (7), stands in the gas-liquid separation tank (7), and after the dissolved oxygen is separated, the reaction product is sent to the upper part of the rotary disc extraction tower (9) through the extraction tower feed pump (8). Before entering the rotary disc extraction tower (9), the inhibitor solution is injected, and the extractant is injected into the lower part of the rotary disc extraction tower (9). The extractant dissolved with toluene is discharged from the top of the rotary disc extraction tower (9), and the final product PPE is discharged from the bottom of the rotary disc extraction tower (9).

6. A polyphenylene ether polymerization process according to claim 1, characterized in that: The catalyst batching kettle (1) and the raw material batching kettle (3) are both provided with a stirrer, the working time of the stirrer is 20-30 minutes, the speed of the stirrer is 200-300 r / min, and the stirring temperature is 20-25°C.

7. A polyphenylene ether polymerization process according to claim 1, characterized in that: The exhaust gas processor (10) comprises an exhaust gas treatment box (101), wherein a plurality of partitions (103) are arranged in the exhaust gas treatment box (101), wherein the plurality of partitions (103) divide the treatment box (101) into a cooling zone (104), an acid liquid zone (105), an alkaline liquid zone (106), and an odor adsorption zone (107); an exhaust gas inlet pipe (102) is connected to the cooling zone (104), and the exhaust gas inlet pipe (102) is connected to an exhaust gas cooler (6); positions of the cooling zone (104), the acid liquid zone (105), the alkaline liquid zone (106), and the odor adsorption zone (107) close to each other are connected via a bend pipe (111), and an exhaust pipe (112) is arranged on the right side of the exhaust gas treatment box (101).

8. A polyphenylene ether polymerization process according to claim 7, characterized in that: The cooling zone (104), the acid zone (105), the alkali zone (106), and the odor adsorption zone (107) are provided with cooling liquid, acid liquid, alkali liquid, and activated carbon particles (109) in sequence; a metal mesh (108) is provided in the odor adsorption zone (107); the activated carbon particles (109) are placed on the top of the metal mesh (108); a tail gas treatment box (101) is provided with a box cover (114) at a position located in the odor adsorption zone (107); three discharge pipes (113) are provided on the outside of the tail gas treatment box (101); and the three discharge pipes (113) are respectively connected to the cooling zone (104), the acid zone (105), and the alkali zone (106).

9. A polyphenylene ether polymerization process according to claim 1, characterized in that: In S4, the obtained product is tested, and the reaction time or the amount of raw materials and catalyst added is adjusted according to the test results.

10. A polyphenylene ether polymerization process according to claim 1, characterized in that: In the S5, the catalyst batching kettle (1), the catalyst metering pump (2), the raw material batching kettle (3), the raw material delivery pump (4), the polymerization sleeve reactor (5), the tail gas cooler (6), the gas-liquid separation tank (7), the extraction tower feed pump (8), the rotary disc extraction tower (9), and the tail gas processor (10) are cleaned and maintained.

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