CN108371932B - Reaction system and method for preparing small molecular weight polyphenylene ether - Google Patents
Reaction system and method for preparing small molecular weight polyphenylene ether Download PDFInfo
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- CN108371932B CN108371932B CN201711482181.6A CN201711482181A CN108371932B CN 108371932 B CN108371932 B CN 108371932B CN 201711482181 A CN201711482181 A CN 201711482181A CN 108371932 B CN108371932 B CN 108371932B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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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
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/34—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from hydroxy compounds or their metallic derivatives
- C08G65/38—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from hydroxy compounds or their metallic derivatives derived from phenols
- C08G65/44—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from hydroxy compounds or their metallic derivatives derived from phenols by oxidation of phenols
Abstract
The application discloses reaction system of preparation low molecular weight polyphenylene ether, the device includes interconnect's first reactor and second reactor, first discharge gate on the first reactor with second feed inlet on the second reactor is connected, second discharge gate on the second reactor with first feed inlet on the first reactor is connected, first reactor with the second reactor forms circulation reaction system, second discharge gate on the second reactor still is connected with the separator, the first reactor outside is equipped with cooling device. The application also discloses a method for preparing the polyphenylene ether with the small molecular weight, which takes 2, 6-dimethylphenol as a raw material and prepares the polyphenylene ether with the small molecular weight by using the reaction system for preparing the polyphenylene ether with the small molecular weight.
Description
Technical Field
The application relates to a reaction system and a method for preparing a small molecular weight polyphenylene ether, belonging to the field of chemical material preparation.
Background
Polyphenylene oxide (PPO or PPE), the chemical name of which is poly-2, 6-dimethyl-1, 4-phenylene oxide, is a high-strength engineering plastic. The insulating property is good, can use in 120 degrees steam. Has outstanding electric insulation and water resistance, better wear resistance and electric performance and good dimensional stability. The PPO and the MPPO are mainly used in the aspects of electronic appliances, automobiles, household appliances, office equipment, industrial machinery and the like, and are used for manufacturing automobile instrument panels, radiator grids, loudspeaker grids, consoles, fuse boxes, relay boxes, connectors and wheel covers by utilizing the heat resistance, impact resistance, dimensional stability, scratch resistance, stripping resistance, coatability and electrical performance of the MPPO; the electronic and electrical industry is widely used for manufacturing parts such as connectors, coil bobbins, switching relays, tuning devices, large-scale electronic displays, variable capacitors, storage battery accessories, microphones and the like. The household appliances are used for parts such as televisions, video cameras, video tapes, recorders, air conditioners, heaters, electric cookers and the like.
Polyphenylene ethers have been industrially produced by oxidation, polymerization and blending.
The oxidation method comprises two parts of polymerization and post-treatment, namely adding a quantitative copper ammonia complex catalyst into a polymerization reaction kettle, bubbling oxygen, then gradually adding 2, 6-dimethylphenol and an ethanol solution, and carrying out oxidative coupling polymerization to obtain a polymer. The post-treatment is to centrifugally separate the polymer, wash the polymer by ethanol solution containing 30 percent of sulfuric acid, soak the polymer by dilute alkali solution, wash the polymer by water, dry the polymer and granulate the polymer to obtain the granular resin of the polyphenyl ether.
The polymerization method adopts 2, 6-diphenyl phenol as a monomer, and the obtained polyphenylene oxide has better thermal stability and is used for manufacturing high-temperature resistant films and insulating products.
The blending method is used for improving the molding processability and reducing the cost, the polyphenyl ether can be modified by the blending method, the modified polyphenyl ether has low cost and market price competitive with ABS resin, and the modified polyphenyl ether can be widely used for replacing bronze or brass to manufacture various mechanical parts, pipelines and the like.
Disclosure of Invention
According to an aspect of the application, a reaction system for preparing a small molecular weight polyphenylene ether is provided, the device comprises a first reactor and a second reactor which are connected with each other, a first discharge port on the first reactor is connected with a second feed port on the second reactor, a second discharge port on the second reactor is connected with a first feed port on the first reactor, the first reactor and the second reactor form a circulating reaction system, a second discharge port on the second reactor is also connected with a separator, and a cooling device is arranged outside the first reactor.
Preferably, a circulation pump is arranged between the first reactor and the second reactor, and the circulation pump can drive the reaction mixture to circulate between the first reactor and the second reactor.
Preferably, the system further comprises a mixer disposed between the first feed port and the second feed port.
Preferably, a valve is arranged between the second discharge hole and the first feed hole, and the valve can guide the material discharged from the second discharge hole into the first reactor or the separator.
According to still another aspect of the present application, there is provided a method for producing a small molecular weight polyphenylene ether starting from 2, 6-dimethylphenol, using the reaction system for producing a small molecular weight polyphenylene ether, comprising the steps of:
1) adding a 2, 6-dimethylphenol solution and a catalyst solution into a second reactor, and establishing circulation between the first reactor and the second reactor after a certain liquid level is reached;
2) after circulation is stable, continuously introducing mixed gas containing oxygen and carrying out oxidative coupling reaction under the action of a catalyst; the reaction mixture discharged from the first reactor enters a second-stage reactor for continuous reaction, and the reaction tail gas is discharged after being purified;
3) when the oxygen is not consumed any more, the reaction is considered to be finished, the reaction mixed liquor is sent into a separator, the separated oil phase is separated and purified, and the water phase is dehydrated and recycled.
Preferably, the catalyst solution is an aqueous solution of an organic amine copper salt complex;
preferably, the copper salt is a divalent copper salt, more preferably, the copper salt is selected from at least one of copper chloride and copper sulfate;
preferably, the organic amine is at least one selected from tetraethyl ethylenediamine and tetramethyl ethylenediamine.
Preferably, in the catalyst, the mass ratio of the copper salt to the organic amine is 1: (5-20), wherein the mass percentage concentration of the organic amine copper salt complex in the catalyst solution is 20-45%.
Preferably, the amount of the catalyst is such that the mass ratio of the copper salt in the catalyst to the 2, 6-dimethylphenol is 1: (20-100).
Preferably, the mass percent of the 2, 6-dimethylphenol in the 2, 6-dimethylphenol solution is 5-30%, preferably 10-25%, and preferably, the solvent of the 2, 6-dimethylphenol solution is selected from at least one of toluene, ethylbenzene and xylene (ortho, meta and para).
Preferably, the oxygen content of the oxygen-containing mixed gas is 5-95%, preferably 10-90%, and preferably, the mixed gas enters the reaction system through a mixer.
Preferably, the reaction temperature of the reaction is 5-100 ℃, the reaction pressure is 0.1-10MPa, preferably, the reaction temperature of the reaction is 20-60 ℃, and the reaction pressure is 0.2-0.8 MPa.
The beneficial effects that this application can produce include:
1) the reaction system for preparing the small molecular weight polyphenylene ether can realize semi-continuous production of the small molecular weight polyphenylene ether, can quickly remove reaction heat of materials, and is favorable for carrying out oxidative coupling reaction;
2) the method for preparing the small molecular weight polyphenylene ether has the advantages of high raw material conversion rate, high target product yield and good selectivity of the small molecular weight polyphenylene ether;
3) in the method for preparing a small molecular weight polyphenylene ether provided by the application, the catalyst can be recycled.
Drawings
FIG. 1 is a schematic view of a reaction system for producing a small molecular weight polyphenylene ether in a preferred embodiment of the present application.
List of parts and reference numerals:
1-first reactor 2-second reactor 3-separator
4-circulating pump 5-mixer 6-valve
11-first inlet 12-first outlet 21-second inlet
22-second discharge hole
Detailed Description
The reaction system of the present application is described in detail below with reference to the accompanying drawings, it should be noted that the drawings and the description are intended to more clearly illustrate the reaction system of the present invention, and not to limit the present invention.
The invention provides a reaction system for preparing a small molecular weight polyphenylene ether, which comprises a first reactor 1 and a second reactor 2 which are connected with each other, wherein a first discharge hole 12 on the first reactor 1 is connected with a second feed hole 21 on the second reactor, a second discharge hole 22 on the second reactor is connected with a first feed hole 11 on the first reactor, the first reactor 1 and the second reactor 2 form a circulating reaction system, a second discharge hole 22 on the second reactor 2 is also connected with a separator 3, and a cooling device is arranged outside the first reactor.
In the invention, circulation is formed between the first reactor and the second reactor, when in application, liquid-phase raw materials and catalyst can be put into the second reactor, and the raw materials and the catalyst are driven to flow in the system to form circulation, and after the reaction reaches a steady state, the reaction is determined to be finished, and at the moment, the reaction mixture in the whole system is discharged to the separator.
In a preferred embodiment of the present invention, the first reactor is a gas-liquid three-phase reactor comprising a barrel; the cylinder is internally provided with a gas-liquid dispersion inner member; the method is suitable for the polymerization reaction for producing the polyphenyl ether under the conditions that the temperature is 5-100 ℃ and the pressure is 0.1-10.0 MPa;
in a preferred embodiment of the present invention, the second reactor is a gas-liquid three-phase reactor, which comprises a barrel; a distributor (formed by connecting a main distribution pipe, branch pipes and distribution caps) is arranged in the cylinder body; the method is suitable for the polymerization reaction for producing the polyphenyl ether under the conditions that the temperature is 5-100 ℃ and the pressure is 0.1-10.0 MPa.
In a preferred embodiment of the present invention, the first reactor comprises a shell side and a tube side, wherein the operation medium of the shell side is a cooling liquid, the cooling liquid can be one of water, brine or ethylene glycol aqueous solution, and the operation medium of the tube side comprises a raw material solution, a catalyst aqueous solution, a nitrogen-oxygen mixed gas and reaction product polyphenylene oxide.
The shell pass is used for cooling the first reactor, and the shell pass cooling liquid is used for realizing rapid heat removal, so that the selectivity of the low molecular weight polyphenylene ether is improved
In a preferred embodiment of the invention, the shell side is provided with a coolant inlet, a coolant outlet and 2-50 baffles 20, e.g., 2, 5, 10, 20, 25, 30, 35, 40, 45, 50 and any point in the range consisting of any two of the above points.
The baffle plate has the function of increasing the flow velocity of the cooling liquid and enhancing the heat transfer efficiency.
In a preferred embodiment of the present invention, the cooling liquid inlet and the cooling liquid outlet are provided on an outer wall of the first reactor cylinder; the inlet of the cooling liquid is arranged at the lower part of the cylinder, the cooling liquid enters the shell pass from the inlet and flows in the shell pass to achieve the effect of cooling the reaction system, and finally flows out from the cooling liquid outlet arranged at the upper part of the cylinder.
In a preferred embodiment of the present invention, the baffles are horizontally disposed on the inner wall of the first reactor barrel, and are disposed in parallel with each other, and the distance between the baffles is 10 to 1000mm, for example, 10mm,100mm,200mm,500mm,1000mm, and any point in the range of any two of the above points. The baffles may be equally spaced or unequally spaced, preferably equally spaced.
In a preferred embodiment of the present invention, the baffle plate is provided with small holes, the diameter of the small holes is 1-100mm, such as 1mm, 10mm, 20mm, 50mm, 100mm and other points in the range of any two of the above points, the arrangement mode is regular triangle, square or any combination of the two, and the aperture ratio is 0.1% -20%.
In a preferred embodiment of the present invention, in the tube side, the tube side feed opening is connected to the first feed opening, and the first feed opening introduces the material into the tube side feed opening;
the tube pass discharge hole is connected with the first discharge hole, and the tube pass discharge hole leads the material out to the first discharge hole.
In a preferred embodiment of the present invention, the tube side comprises a tube bundle comprising 1 to 1000 reaction tubes, such as 1, 10, 100, 500, 1000, and others in the range of any two of the above, the tube bundle having a diameter of 5 to 500mm and a length of 500 and 10000mm, and the reaction tubes in the tube bundle are arranged in at least one selected from the group consisting of regular triangle, square and single row.
In a preferred embodiment of the present invention, the reactor tube is provided with dispersing assemblies, and the number of dispersing assemblies in each reactor tube is 1-1000, such as 1, 10, 100, 500, 1000, and other points in the range of any two of the above points; said divisionThe specific surface area of the bulk component is 100-1000m2/m3The porosity is 0.01-0.1; the length is 10-1000 mm.
The combined application of the tube bundle and the dispersing assembly can realize the uniform dispersion of reactants to the maximum extent, improve the defects of the traditional reaction kettle and improve the process efficiency and the selectivity of the product, namely the small-molecule polymer.
In a preferred embodiment of the invention, the second reactor comprises a second reactor cylinder, a head, a liquid material inlet and a distributor;
the second reactor cylinder is a cylinder, the end socket is an ellipsoid or spherical end socket, and the end socket seals the upper opening and the lower opening of the second reactor cylinder;
the distributor is arranged in the second reactor barrel and is connected with the second feeding hole;
the liquid material feed inlet is arranged on the outer wall of the barrel and can guide liquid materials to the distributor.
In a preferred embodiment of the invention, the distributor comprises a distributor main pipe, distributor branch pipes and a distribution cap.
In a preferred embodiment of the invention, the distributor main tube has a diameter of 20 to 300mm and a length of 50 to 5000 mm.
In a preferred embodiment of the invention, the number of distributor legs is 2-200, the diameter is 5-100mm, the length is 50-2500mm, and each distributor leg is connected to the distributor main pipe.
In a preferred embodiment of the invention, the distribution cap is arranged at the distributor branch pipe and away from its connection with the distributor main pipe.
The working mechanism of the distributor is to realize the gas-liquid high-efficiency mass transfer by utilizing the micropore interface effect of the high specific surface of the distribution cap.
In a preferred embodiment of the present invention, the distribution cap is a hollow cylinder or cone made of at least one of sintered metal wire mesh, sintered metal powder, and welded metal wire mesh, and the average pore diameter of the distribution cap is between 0.01 and 1.0mm, and the aperture ratio is between 0.01 and 2.0%; the number of the distribution caps is 10-1000.
In a preferred embodiment of the present invention, the operation medium of the second reactor comprises a stock solution, an aqueous catalyst solution, a mixed gas of nitrogen and oxygen, and a reaction product polyphenylene ether.
In a preferred embodiment of the invention, the bottom of the second reactor is 0-50% higher than the bottom of the first reactor.
The second reactor 2 may be at the same height as the first reactor 1 or higher than the first reactor 1, based on the bottom of the reactor barrel. Since the connecting lines therebetween avoid oxygen accumulation in the gas phase, which would cause danger due to the increased concentration.
In a preferred embodiment of the present invention, a circulation pump 4 is provided between the first reactor 1 and the second reactor 2, and the circulation pump 4 is capable of driving the reaction mixture to circulate between the first reactor and the second reactor.
In a preferred embodiment of the present invention, the circulation pump is selected from any one of a centrifugal pump, a plunger pump, a progressive cavity pump, and a diaphragm pump.
The circulation pump is used to drive the circulation of the reaction mass in the first reactor 1 and the second reactor 2.
In a preferred embodiment of the present invention, the system further comprises a mixer 5, the mixer 5 being disposed between the first inlet 11 and the second outlet 22, the mixer thoroughly premixing the reaction raw materials of different phases.
In a preferred embodiment of the present invention, a valve 6 is disposed between the second discharge port 22 and the first feed port 11, and the valve 6 can guide the material discharged from the second discharge port to the first reactor or the separator. In use, when it is detected that the oxygen is no longer consumed, the valve will organize the passage of the second reactor to the first reactor, open the passage of the second reactor to the separator, and introduce the reaction mixture into the separator.
The production process of the present invention will be described in detail with reference to examples, but the present invention is not limited to these examples.
Example 1
The reaction system provided by the invention is adopted to prepare the polyphenyl ether under different reaction conditions according to different raw material concentrations and catalyst proportions, the composition and the dosage of the raw materials and the catalyst are shown in table 1, and the reaction conditions are shown in table 2.
TABLE 1 composition and proportioning of the raw materials and catalysts
TABLE 2 reaction conditions
| Experiment number | Temperature (. degree.C.) | Pressure (MPa) |
| 1 | 40 | 0.5 |
| 2 | 40 | 0.5 |
| 3 | 20 | 0.8 |
| 4 | 60 | 0.2 |
| 5 | 15 | 10 |
| 6 | 100 | 0.1 |
The reaction results are shown in table 3:
TABLE 3 results of the reaction
As can be seen from the above reaction results, a polyphenylene ether having a small molecular weight can be obtained in a high yield and selectivity by the process of the present invention.
Although the present application has been described with reference to a few embodiments, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the application as defined by the appended claims.
Claims (18)
1. A method for preparing polyphenylene ether with small molecular weight is characterized in that a device adopted by the method comprises a first reactor and a second reactor which are connected with each other, a first discharge hole on the first reactor is connected with a second feed hole on the second reactor, a second discharge hole on the second reactor is connected with the first feed hole on the first reactor, the first reactor and the second reactor form a circulating reaction system, a second discharge hole on the second reactor is also connected with a separator, and a cooling device is arranged outside the first reactor; the first reactor comprises a shell side and a tube side, wherein the operation medium of the shell side is cooling liquid, and the operation medium of the tube side comprises a raw material solution, a catalyst aqueous solution, a nitrogen-oxygen mixed gas and a reaction product polyphenylene oxide;
the first reactor is a gas-liquid three-phase reactor; the first reactor comprises a barrel; the cylinder is internally provided with a gas-liquid dispersion inner member;
the second reactor is a gas-liquid three-phase reactor; the second reactor comprises a barrel; a distributor is arranged in the cylinder body; the method comprises the following steps:
1) adding a 2, 6-dimethylphenol solution and a catalyst aqueous solution into a second reactor, and establishing circulation between the first reactor and the second reactor after a certain liquid level is reached;
2) after circulation is stable, continuously introducing mixed gas containing oxygen and carrying out oxidative coupling reaction under the action of a catalyst; the reaction mixture discharged from the first reactor enters a second-stage reactor for continuous reaction, and the reaction tail gas is discharged after being purified;
3) when the oxygen is not consumed any more, the reaction is considered to be finished, the reaction mixed liquor is sent into a separator, the separated oil phase is separated and purified, and the water phase is dehydrated and recycled; the raw material solution is 2, 6-dimethylphenol solution; the solvent of the 2, 6-dimethylphenol solution is at least one selected from toluene, ethylbenzene and xylene.
2. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein a circulation pump capable of driving the reaction mixture to circulate between the first reactor and the second reactor is provided between the first reactor and the second reactor.
3. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein said system further comprises a mixer disposed between the first supply port and the second supply port.
4. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein a valve is provided between said second port and said first port, and said valve allows a material discharged from said second port to be introduced into said first reactor or said separator.
5. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein said aqueous catalyst solution is an aqueous solution of an organic amine copper salt complex.
6. The process for producing a small molecular weight polyphenylene ether according to claim 5,
the copper salt is a divalent copper salt.
7. The process for producing a small molecular weight polyphenylene ether according to claim 6, wherein said copper salt is at least one selected from the group consisting of copper chloride and copper sulfate.
8. The method for producing a small molecular weight polyphenylene ether according to claim 5, wherein said organic amine is at least one selected from the group consisting of tetraethylethylenediamine, tetramethylethylenediamine and tetrapropylethylenediamine.
9. The method for producing a small molecular weight polyphenylene ether according to claim 5, wherein the mass ratio of the copper salt to the organic amine in the catalyst is 1: (5-20), wherein the mass percentage concentration of the organic amine copper salt complex in the catalyst aqueous solution is 20-45%.
10. The process for producing a small molecular weight polyphenylene ether according to claim 5,
the using amount of the catalyst meets the requirement, and the mass ratio of the copper salt in the catalyst to the 2, 6-dimethylphenol is 1: (20-100).
11. The method for producing a small molecular weight polyphenylene ether according to claim 1, wherein the mass percentage of 2, 6-dimethylphenol in the 2, 6-dimethylphenol solution is 5-30%.
12. The method for producing a small molecular weight polyphenylene ether according to claim 11, wherein the mass percentage of 2, 6-dimethylphenol in the 2, 6-dimethylphenol solution is 10-25%.
13. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein the non-oxygen gas in the oxygen-containing gas mixture is nitrogen.
14. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein the oxygen content of the oxygen-containing mixed gas is 5 to 95%.
15. The process for producing a small molecular weight polyphenylene ether according to claim 14, wherein the oxygen content of the oxygen-containing mixed gas is 10 to 90%.
16. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein said mixed gas is introduced into the reaction system through a mixer.
17. The process for producing a small molecular weight polyphenylene ether according to claim 1, wherein the reaction temperature of the reaction is 5 to 100 ℃ and the reaction pressure is 0.1 to 10 MPa.
18. The process for producing a small molecular weight polyphenylene ether according to claim 17,
the reaction temperature is 20-60 deg.C, and the reaction pressure is 0.2-0.8 MPa.
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| CN201711482181.6A CN108371932B (en) | 2017-12-29 | 2017-12-29 | Reaction system and method for preparing small molecular weight polyphenylene ether |
| PCT/CN2018/071836 WO2019127645A1 (en) | 2017-12-29 | 2018-01-09 | Reaction system and method for preparing polyphenyl ether having small molecular weight |
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| CN113493565B (en) * | 2020-04-02 | 2024-01-26 | 上海孛柯博科技有限公司 | Polyphenylene oxide, preparation method thereof and device for producing polyphenylene oxide |
| CN115228406A (en) * | 2022-08-03 | 2022-10-25 | 山东亿科化学有限责任公司 | Be applied to down shell and tube circulation type reation kettle among polyphenyl ether polymerization technology |
| CN116199875B (en) * | 2023-01-19 | 2023-11-17 | 北京中油创宇科技有限公司 | Method for preparing small-molecular-weight double-end hydroxyl polyphenyl ether by using micro-channel reactor |
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| US4696996A (en) * | 1984-11-17 | 1987-09-29 | Basf Aktiengesellschaft | Preparation of polyphenylene ethers, and an apparatus for this purpose |
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| CN2626605Y (en) * | 2003-07-15 | 2004-07-21 | 上海焦化有限公司 | Jet type internal circulation reacting device |
| CN101993350B (en) * | 2009-08-31 | 2013-06-05 | 中国石油化工股份有限公司 | Production method of glycol |
| FI125632B (en) * | 2010-05-25 | 2015-12-31 | Upm Kymmene Corp | Method and apparatus for producing hydrocarbons |
| CN103709398A (en) * | 2013-12-25 | 2014-04-09 | 济南开发区星火科学技术研究院 | Preparation method of polyphenyl ether |
| JP6374343B2 (en) * | 2014-04-15 | 2018-08-15 | 旭化成株式会社 | Process for producing polyphenylene ether |
| CN203990641U (en) * | 2014-08-29 | 2014-12-10 | 山东阳谷华泰化工股份有限公司 | The consersion unit of synthetic rubber accelerator NS |
| CN106188525A (en) * | 2016-07-18 | 2016-12-07 | 江苏三吉利化工股份有限公司 | A kind of synthetic method of polyphenylene oxide |
| CN107382665B (en) * | 2017-07-13 | 2023-06-30 | 南京国昌化工科技有限公司 | Methanol synthesis process and device |
| CN107353401B (en) * | 2017-08-24 | 2020-06-30 | 宋立旺 | Dihydroxy polyphenyl ether and preparation method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US4696996A (en) * | 1984-11-17 | 1987-09-29 | Basf Aktiengesellschaft | Preparation of polyphenylene ethers, and an apparatus for this purpose |
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| Title |
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| 聚苯醚的合成及对其分子量的控制;张玉芳等;《绝缘材料》;20070820;第40卷(第04期);第11页左栏第1段、图3-5 * |
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