CN114539514A - Phthalic anhydride and epoxypropane mixed feeding process, equipment and application - Google Patents
Phthalic anhydride and epoxypropane mixed feeding process, equipment and application Download PDFInfo
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- CN114539514A CN114539514A CN202111213851.0A CN202111213851A CN114539514A CN 114539514 A CN114539514 A CN 114539514A CN 202111213851 A CN202111213851 A CN 202111213851A CN 114539514 A CN114539514 A CN 114539514A
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- phthalic anhydride
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- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 title claims abstract description 93
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 title claims abstract description 93
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 43
- 238000002360 preparation method Methods 0.000 claims abstract description 35
- 238000002156 mixing Methods 0.000 claims abstract description 25
- 238000003756 stirring Methods 0.000 claims abstract description 24
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 18
- 239000000463 material Substances 0.000 claims abstract description 16
- 238000005273 aeration Methods 0.000 claims abstract description 8
- 238000001035 drying Methods 0.000 claims abstract description 5
- 238000001914 filtration Methods 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 57
- 239000000203 mixture Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 5
- 229920000704 biodegradable plastic Polymers 0.000 claims description 4
- 230000002194 synthesizing effect Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 2
- 229920000642 polymer Polymers 0.000 abstract description 13
- 229920003023 plastic Polymers 0.000 abstract description 7
- 239000004033 plastic Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000013461 design Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000011161 development Methods 0.000 abstract description 2
- 238000012545 processing Methods 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 28
- 229910002092 carbon dioxide Inorganic materials 0.000 description 15
- 239000001569 carbon dioxide Substances 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 239000007787 solid Substances 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- 238000002844 melting Methods 0.000 description 4
- 230000008018 melting Effects 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 239000011343 solid material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical group CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 239000002612 dispersion medium Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000010410 layer Substances 0.000 description 2
- SCRKTTJILRGIEY-UHFFFAOYSA-N pentanedioic acid;zinc Chemical compound [Zn].OC(=O)CCCC(O)=O SCRKTTJILRGIEY-UHFFFAOYSA-N 0.000 description 2
- 239000004417 polycarbonate Substances 0.000 description 2
- 229920000515 polycarbonate Polymers 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 229920001897 terpolymer Polymers 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- -1 for short Chemical compound 0.000 description 1
- 150000007529 inorganic bases Chemical class 0.000 description 1
- 239000002608 ionic liquid Substances 0.000 description 1
- 239000002609 medium Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
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Classifications
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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
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/64—Polyesters containing both carboxylic ester groups and carbonate groups
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyesters Or Polycarbonates (AREA)
- Epoxy Compounds (AREA)
Abstract
The invention relates to the field of IPC classified C08L69/00, in particular to a mixed feeding process, equipment and application of phthalic anhydride and propylene oxide. The feeding process steps in the application at least comprise the following steps: (1) the dosage of phthalic anhydride and propylene oxide; (2) mixing and feeding; (3) mixing and stirring; (4) adding auxiliary materials; (5) carrying out aeration polymerization; (6) and (5) filtering and drying. The main structure of the equipment comprises a metering tank, a preparation kettle and a reaction kettle. The process has good energy consumption control capability, can realize sectional feeding, effectively controls the length of a reaction molecular chain of a polymer and the block design, is suitable for popularization in the field of plastic manufacturing and processing, and has wide development prospect.
Description
Technical Field
The invention relates to the field of IPC classified C08L69/00, in particular to a mixed feeding process, equipment and application of phthalic anhydride and propylene oxide.
Background
With the use of plastic products in large quantities, the problem of white pollution of plastics is widely concerned by people. Biodegradable plastics are plastics which can be degraded under natural environmental conditions to be harmless to the environment after use, are considered as one of effective ways to solve the problem of plastic pollution, and are gradually receiving the support of national encouragement and attention of people.
PPC-P is a novel biodegradable plastic obtained by chemically modifying PPC with phthalic anhydride (phthalic anhydride, for short, phthalic anhydride or PA), and the rigidity of a high-molecular chain is improved by introducing the phthalic anhydride into the PPC main chain, so that the mechanical and thermal properties of the PPC are obviously improved, and the additional value of the PPC plastic can be greatly improved.
Chinese patent CN202010337273.0 discloses a new method for preparing a high-purity low-purity high-purity calcium2A process for synthesizing carbon dioxide-base polyester-polycarbonate terpolymer (PPC-P) includes such steps as proportionally adding phthalic anhydride, epoxy propane and catalyst to high-pressure reactor, charging 1.0-3.0MPa CO2And reacting for 12 hours at the temperature of 60-100 ℃, quenching reaction after the reaction is finished, and dissolving, precipitating and drying the product to obtain the product. The defects that the feeding mode of phthalic anhydride and propylene oxide mentioned in the patent is sequentially and independently feeding, if the phthalic anhydride is added in a solid state form, longer time is needed for dissolving, a large amount of heat is absorbed, the reaction time is prolonged, and the energy consumption is increased; if the phthalic anhydride is added in a liquid state, the melting point of the phthalic anhydride is 133 ℃, so that the local temperature of the reaction kettle is extremely high when the phthalic anhydride is added, the byproducts are increased, the yield is reduced, and the local pressure of the reaction kettle is higher.
Therefore, there is a need for a mixed feeding process and an apparatus thereof capable of effectively suppressing the generation of side reactions, improving the yield, and enabling the conversion rate and product selectivity of phthalic anhydride. In addition, the invention aims to improve the raw material feeding process of the biodegradable carbon dioxide polyester-polycarbonate terpolymer disclosed in patent CN202010337273.0, further improve the conversion rate of raw materials and the yield of products, and reduce the production cost.
The existing conventional process is that solid phthalic anhydride and propylene oxide are added separately in batches. The technical problem of the method is obvious. Firstly, solid phthalic anhydride is added, a large amount of manual operation is needed, and the efficiency is low; the factors of residue, dust loss and the like in the packaging bag easily cause that the feeding cannot be accurately measured; in the feeding process, more solid dust is generated, certain harm is caused to the occupational health of operators, and the workshop sanitation is difficult to guarantee; in the feeding process, the original materials in the kettle are mostly inflammable and explosive toxic substances, and the materials with lower boiling points overflow, so that the health of operators is harmed, and safety accidents are easy to happen.
In the actual operation process, according to the material characteristics, the melting point of phthalic anhydride is high, a large amount of heat is needed for melting after the phthalic anhydride is added into a reaction kettle, the energy consumption is high, frequent temperature reduction and temperature rise are realized, and the energy efficiency is poor; the solid materials have moisture absorption phenomenon, and the reaction is sensitive to moisture and has great influence on the experimental effect; in the process of adding the solid materials, the solid materials are often not uniformly distributed, have higher requirements on stirring and influence the subsequent reaction stability.
Disclosure of Invention
In order to solve the above problems, the present invention provides, in a first aspect, a mixed feeding process of phthalic anhydride and propylene oxide, comprising at least the following steps: (1) the dosage of phthalic anhydride and propylene oxide; (2) mixing and feeding; (3) mixing and stirring; (4) adding auxiliary materials; (5) carrying out aeration polymerization; (6) and (5) filtering and drying.
As a preferred variant, the phthalic anhydride and propylene oxide are metered in: liquid propylene oxide and liquid phthalic anhydride feed.
In a preferred embodiment, the molar ratio of the liquid propylene oxide to the liquid phthalic anhydride is 0.5 to 10: 1.
in a preferable embodiment, the molar ratio of the liquid propylene oxide to the liquid phthalic anhydride is 5 to 8: 1.
in the application, the toughness and the molecular weight uniformity of PPC-P are effectively improved by limiting the feeding and mixing molar ratio of liquid propylene oxide and liquid phthalic anhydride. The applicant speculates that: when the molar ratio of liquid epoxypropane to liquid phthalic anhydride is 5-8: 1, the liquid mixing feeding of the liquid epoxypropane and the liquid phthalic anhydride is cooperated, the molecular chain contact degree between different raw materials can be effectively realized, so that a uniform and stable block structure of hard segment, soft segment and hard segment is formed during mixing feeding, the molecular chain composition of a product is effectively controlled, and a molecular chain structure with high toughness is formed.
As a preferred scheme, the mixed feeding materials are as follows: mixing liquid epoxypropane and liquid phthalic anhydride, putting into a preparation container, and heating and stirring; the feeding sequence is that liquid propylene oxide is added firstly, and then liquid phthalic anhydride is added.
As a preferable scheme, during the mixed feeding, the feeding temperature of the liquid propylene oxide is 0-40 ℃; the feeding temperature of the liquid phthalic anhydride is 120-160 ℃.
As a more preferable scheme, the feeding temperature of the liquid propylene oxide is 15-30 ℃ during the mixed feeding; the feeding temperature of the liquid phthalic anhydride is 130-150 ℃.
As a preferred scheme, the mixing and stirring are as follows: and (3) fixing the stirring speed and stirring for a fixed time at a set temperature for the liquid propylene oxide and the liquid phthalic anhydride after feeding so as to achieve high mixing of the two raw materials.
As a preferable scheme, the stirring temperature of the preparation container is 30-120 ℃; the stirring speed of the preparation container is 30-200 r/min; the preparation and mixing time is 20-60 min.
As a more preferable scheme, the stirring temperature of the preparation container is 50-90 ℃; the stirring speed of the preparation container is 60-120 r/min; the preparation and mixing time is 40-50 min.
In the application, the conversion rate of phthalic anhydride is effectively improved through mixed feeding of liquid propylene oxide and liquid phthalic anhydride and limited setting of feeding temperature, so that the yield and purity of the whole product are improved. The applicant speculates that: compared with the feeding mode that propylene oxide and phthalic anhydride are fed separately and phthalic anhydride is directly fed into a solid in the prior art, the feeding mode that propylene oxide and phthalic anhydride are fed separately has the characteristics of more uniform material mixing and flexible feeding mode, and the preferentially added propylene oxide can be effectively used as a benign dispersion medium of phthalic anhydride, so that the molecular doping of the propylene oxide and the phthalic anhydride is more uniform; the method for feeding the mixed liquid raw materials effectively avoids the technical problems that the phthalic anhydride needs a certain time to be uniformly mixed in the reaction kettle and the reaction time is prolonged due to the adoption of a feeding mode of solid phthalic anhydride and propylene oxide, and the technical problems that the side reaction is increased due to the fact that the temperature is higher than 130 ℃ after the phthalic anhydride is fed into the reaction kettle, the selectivity of the product PPC-P is reduced, the local pressure of the reaction kettle is overhigh and the potential safety hazard is formed when the liquid phthalic anhydride and the propylene oxide are independently fed are also avoided.
As a preferable scheme, the auxiliary material is at least one of an inorganic base catalyst, a metal salt catalyst, an organic catalyst and an ionic liquid catalyst.
As a preferable scheme, the auxiliary material is zinc glutarate.
As a preferred embodiment, the vented polymerization is: after the mixture of the liquid epoxypropane and the liquid phthalic anhydride is put into a reaction vessel, carbon dioxide gas with fixed pressure is filled into the reaction vessel, the reaction is carried out for a period of time at high temperature, and carbon dioxide is released after the reaction is finished.
As a preferable scheme, the weight ratio of the liquid propylene oxide to the carbon dioxide is 3.8-4.2: 0.6 to 0.8.
As a more preferred embodiment, the weight ratio of liquid propylene oxide to carbon dioxide is 3.8: 0.692.
in the application, the reaction rate of polymerization is effectively improved by controlling the mass compounding ratio of the propylene oxide and the introduced carbon dioxide gas, and the reaction stability is further improved. The applicant speculates that: when the weight ratio of liquid propylene oxide to carbon dioxide is 3.8: 0.692, liquid propylene oxide can serve as a dispersion medium for mixing and feeding in the system, and simultaneously, the contact degree of the mixture and carbon dioxide is fully improved within a proper range, so that the mixture is not limited to the surface layer part of the mixture in the polymerization process, and the mixture can be effectively driven to the whole part of a column-shaped mixing system along with a certain content of propylene oxide, thereby maintaining good reaction stability on the basis of improving the reaction rate and obviously improving the product yield.
As a preferable scheme, the mass ratio of the carbon dioxide to the auxiliary materials is 9-11: 1.
as a more preferable scheme, the mass ratio of the carbon dioxide to the auxiliary materials is 9.6-9.8: 1.
as a preferable scheme, the fixed pressure is 2-3 MPa.
As a more preferable mode, the fixed pressure is 2.1 MPa.
Preferably, the time of the aeration polymerization reaction is 8-12 h.
As a more preferred embodiment, the reaction time of the aerated polymerization is 10 hours.
Preferably, the polymerization temperature in the aeration polymerization process is 50-90 ℃.
In a more preferable embodiment, the polymerization temperature during the aeration polymerization is 60 to 80 ℃.
As a preferable scheme, the feeding equipment mainly comprises a metering tank, a preparation kettle 5 and a reaction kettle 6.
As a preferred approach, the metering tanks include a phthalic anhydride metering tank 4 and a propylene oxide metering tank 3; the outer layers of the preparation kettle 5 and the reaction kettle 6 are provided with jackets or coil pipes 7, and heating media or cooling media are introduced into the jackets or coil pipes 7 to control the temperature in the kettles; the preparation kettle 5 is provided with a stirring paddle 5-1, so that the materials can be uniformly mixed at the temperature.
Preferably, the phthalic anhydride metering tank 4 and the propylene oxide metering tank 3 are fixedly connected with an upper pipeline of the preparation kettle 5, and the pipeline is used for conveying liquid phthalic anhydride and propylene oxide.
In a preferred embodiment, a phthalic anhydride inlet 2 and a propylene oxide inlet 1 are fixedly connected to the front ends of the phthalic anhydride measuring tank 4 and the propylene oxide measuring tank 3, respectively, for introducing raw materials.
Preferably, the preparation kettle is fixedly connected with the reaction kettle through a pipeline, and the pipeline is used for conveying the mixed liquid of the phthalic anhydride and the propylene oxide.
The invention provides an application of the phthalic anhydride and propylene oxide mixed feeding process, which comprises the application of the process in a preparation process for synthesizing biodegradable plastics.
Has the advantages that:
1. the mixed feeding process provided by the application can effectively realize staged feeding, so that the composition control of a molecular chain of a product can be effectively realized, the block design of a chain segment is realized, and finally, multiple performances are endowed to a polymer.
2. The mixed feeding process can effectively realize the comprehensive utilization of the energy consumption of the hot phthalic anhydride, fully utilizes the characteristic of high melting point of the phthalic anhydride, adds the polymerization kettle at high temperature, and can effectively provide reaction temperature for the polymerization process, thereby effectively reducing the heat energy supply of the reaction process.
3. The mixed feeding process provided in the application has the advantages that the phthalic anhydride is pre-dissolved, the gas-liquid reaction can be effectively completed, the reaction is easier to initiate, the controllability is stronger, the stirring is more uniform, the whole-course phthalic anhydride polymerization reaction can be realized, and the more uniform molecular weight distribution of the product is realized.
Drawings
Fig. 1 is a schematic structural diagram of the mixing and feeding device of the present application.
In the figure: 1 propylene oxide feed inlet, 2 phthalic anhydride feed inlet, 3 propylene oxide metering tank, 4 phthalic anhydride metering tank, 5 preparation kettle, 5-1 stirring paddle, 6 reaction kettle, 7 jacket or coil pipe.
Detailed Description
Example 1
Example 1 in a first aspect, there is provided a mixed phthalic anhydride and propylene oxide feed process comprising the steps of: (1) the dosage of phthalic anhydride and propylene oxide; (2) mixing and feeding; (3) mixing and stirring; (4) adding auxiliary materials; (5) carrying out aeration polymerization; (6) and (5) filtering and drying.
In a second aspect, this embodiment provides a mixed feeding apparatus as shown in fig. 1, which mainly comprises a metering tank, a preparation kettle and a reaction kettle.
Wherein the metering tank comprises a phthalic anhydride metering tank and a propylene oxide metering tank; the outer layers of the preparation kettle and the reaction kettle are provided with jackets, and a heating medium and a cooling medium are introduced into the jackets to control the temperature in the kettle; the preparation kettle is provided with a stirring paddle, so that the materials can be uniformly mixed at the temperature.
The phthalic anhydride metering tank and the propylene oxide metering tank are fixedly connected with an upper pipeline of the preparation kettle, and the pipeline is used for conveying liquid phthalic anhydride and propylene oxide.
The preparation kettle is fixedly connected with the reaction kettle through a pipeline, and the pipeline is used for conveying the mixed liquid of the phthalic anhydride and the epoxypropane.
The actual operation process is as follows: preparation work: 1m of preparation kettle and reaction kettle3Performing nitrogen replacement for three times in the high-pressure reaction kettle; (1) respectively weighing 380Kg of liquid propylene oxide and 172Kg of liquid phthalic anhydride by using a metering tank; (2) the raw materials are sequentially put into a preparation kettle, the feeding temperature of liquid propylene oxide is controlled to be 25 ℃, and the feeding temperature of liquid phthalic anhydride is controlled to be 140 ℃; (3) controlling the temperature in the preparation kettle to be 70 ℃, stirring the mixture at a rotating speed of 90r/min, and uniformly mixing the epoxypropane and the phthalic anhydride after mixing and stirring the mixture for 30min to obtain a mixed solution; (4) introducing the mixed solution into a reaction kettle, and adding 7.2kg of zinc glutarate catalyst into the mixed solution; (5) filling 2.1MPa carbon dioxide 69.2KG, reacting at 80 ℃ for 10h, dissolving the product with absolute ethyl alcohol after the reaction is finished until the product is completely dissolved, finishing the reaction, and precipitating to obtain a polymer; (6) the polymer was dried in a vacuum oven at 80 ℃ for 60 hours, and the mass of the polymer was measured to be 602.3Kg, and the polymer yield was calculated to be 96.96%.
In this example, propylene oxide was purchased from superior grade propylene oxide of san Yue chemical Co., Ltd, Shandong.
In this example, phthalic anhydride was purchased as a premium phthalic anhydride from Shandong Hongtong chemical Co., Ltd.
Example 2
The embodiment of the present invention is different from embodiment 1 in that: 392Kg of liquid propylene oxide, 161Kg of solid phthalic anhydride, 6.9Kg of catalyst and 72.6Kg of carbon dioxide were added; the mass of the final polymer was measured to be 494.6Kg, and the polymer yield was calculated to be 79.06%.
Example 3
The embodiment of the present invention is different from embodiment 1 in that: the adding amount of liquid propylene oxide is 408Kg, the adding amount of solid phthalic anhydride is 166Kg, and the propylene oxide and the phthalic anhydride solid are directly placed into a reaction kettle without stirring and mixing steps in a preparation kettle, 7.5Kg of catalyst is added, and the introducing amount of carbon dioxide is 75.6 Kg; the mass of the final polymer was measured to be 445.7Kg and the polymer yield was calculated to be 68.61%.
Example 4
The embodiment of the present invention is different from embodiment 1 in that: the adding amount of the liquid propylene oxide is 400Kg, the adding amount of the liquid phthalic anhydride is 165Kg, and the introducing amount of the carbon dioxide is 68.6 Kg; the mass of the final polymer was measured to be 614.8Kg and the polymer yield was calculated to be 97.03%.
Embodiments 1 to 4 show that the mixed feeding process, equipment and application of phthalic anhydride and propylene oxide provided by the invention have good energy consumption control capability, and can realize segmented feeding, so that the length and the block design of a reaction molecular chain of a polymer are effectively controlled, and the process is suitable for popularization in the field of plastic manufacturing and processing, and has a wide development prospect. Wherein, the embodiment 1 obtains the best product purity and yield under the conditions of optimal preparation raw material proportion, preparation process and the like.
Claims (10)
1. A mixed feeding process of phthalic anhydride and propylene oxide is characterized in that: the steps at least comprise the following steps: (1) the dosage of phthalic anhydride and propylene oxide; (2) mixing and feeding; (3) mixing and stirring; (4) adding auxiliary materials; (5) carrying out aeration polymerization; (6) and (5) filtering and drying.
2. The mixed phthalic anhydride and propylene oxide dosing process according to claim 1, characterized in that: the phthalic anhydride and propylene oxide are dosed in the following amounts: liquid propylene oxide and liquid phthalic anhydride feed.
3. The mixed phthalic anhydride and propylene oxide dosing process according to claim 2, characterized in that: the molar ratio of the liquid propylene oxide to the liquid phthalic anhydride is 0.5-10: 1.
4. the mixed feeding process of phthalic anhydride and propylene oxide according to any of claims 1 to 3, characterized in that: the mixed feeding comprises the following steps: mixing liquid epoxypropane and liquid phthalic anhydride, putting the mixture into a preparation container, and heating and stirring the mixture; the feeding sequence is that liquid propylene oxide is added firstly, and then liquid phthalic anhydride is added.
5. The phthalic anhydride and propylene oxide mixed feed process of claim 4, characterized in that: during the mixed feeding, the feeding temperature of the liquid propylene oxide is 0-40 ℃; the feeding temperature of the liquid phthalic anhydride is 120-160 ℃.
6. The phthalic anhydride and propylene oxide mixed feed process of claim 4, characterized in that: the stirring temperature of the preparation container is 30-120 ℃; the stirring speed of the preparation container is 30-200 r/min; the preparation and mixing time is 20-60 min.
7. The mixed feeding process of phthalic anhydride and propylene oxide according to any of claims 1 to 6, characterized in that: the temperature of the polymerization reaction in the aeration polymerization process is 50-90 ℃.
8. A feeding device for a phthalic anhydride and propylene oxide mixed feeding process according to any one of claims 1 to 7, characterized in that: the structure of the feeding equipment mainly comprises a metering tank, a preparation kettle and a reaction kettle.
9. The charging equipment for a mixed charging process of phthalic anhydride and propylene oxide according to claim 8, characterized in that: the metering tanks include a phthalic anhydride metering tank and a propylene oxide metering tank; the outer layers of the preparation kettle and the reaction kettle are provided with jackets or coil pipes, and heating media or cooling media are introduced into the jackets or coil pipes to control the temperature in the kettle; the preparation kettle is provided with a stirring paddle, so that the materials can be uniformly mixed at temperature.
10. Use of a mixed phthalic anhydride and propylene oxide feed process according to any of claims 1 to 7, characterized in that: comprising the application of the process in the preparation process of synthesizing biodegradable plastics.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111213851.0A CN114539514A (en) | 2021-10-19 | 2021-10-19 | Phthalic anhydride and epoxypropane mixed feeding process, equipment and application |
| PCT/CN2022/126045 WO2023066269A1 (en) | 2021-10-19 | 2022-10-19 | Method for mixed feeding of phthalic anhydride and propylene oxide, equipment, and application |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111213851.0A CN114539514A (en) | 2021-10-19 | 2021-10-19 | Phthalic anhydride and epoxypropane mixed feeding process, equipment and application |
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| CN114539514A true CN114539514A (en) | 2022-05-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111213851.0A Pending CN114539514A (en) | 2021-10-19 | 2021-10-19 | Phthalic anhydride and epoxypropane mixed feeding process, equipment and application |
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| CN (1) | CN114539514A (en) |
| WO (1) | WO2023066269A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023066269A1 (en) * | 2021-10-19 | 2023-04-27 | 山东联欣环保科技有限公司 | Method for mixed feeding of phthalic anhydride and propylene oxide, equipment, and application |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110092900A (en) * | 2019-04-30 | 2019-08-06 | 华中科技大学 | A kind of preparation method of carbon dioxide group block copolymer |
| CN111378101A (en) * | 2020-04-26 | 2020-07-07 | 中山大学 | Preparation method of biodegradable carbon dioxide-based polyester-polycarbonate terpolymer |
| CN111378106A (en) * | 2020-03-30 | 2020-07-07 | 杭州普力材料科技有限公司 | Method for continuous production of polycarbonate-polyether polyol by preheating liquid phase method in pipeline manner |
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| GB1042525A (en) * | 1963-06-17 | 1966-09-14 | Allied Chem | Production of polyesters |
| JP5505920B2 (en) * | 2007-05-09 | 2014-05-28 | 学校法人東京理科大学 | Process for producing block copolymer |
| EP2441788A1 (en) * | 2010-10-14 | 2012-04-18 | Bayer MaterialScience AG | Method for manufacturing polyether polyols |
| CN102775594B (en) * | 2012-07-27 | 2014-10-22 | 湛江师范学院 | Cross-linking terpolymer of tetracarboxylic dianhydride compound, propylene epoxide and carbon dioxide and method for preparing same |
| CN207699497U (en) * | 2017-12-27 | 2018-08-07 | 江阴济化新材料有限公司 | A kind of esterification system producing PBT |
| CN111333825A (en) * | 2020-04-26 | 2020-06-26 | 中山大学 | Preparation method of carbon dioxide-based polyester-polycarbonate quaternary block copolymer |
| CN214076555U (en) * | 2020-10-23 | 2021-08-31 | 广东伟明涂料有限公司 | High-precision automatic feeding reaction device |
| CN114539514A (en) * | 2021-10-19 | 2022-05-27 | 山东联欣环保科技有限公司 | Phthalic anhydride and epoxypropane mixed feeding process, equipment and application |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110092900A (en) * | 2019-04-30 | 2019-08-06 | 华中科技大学 | A kind of preparation method of carbon dioxide group block copolymer |
| CN111378106A (en) * | 2020-03-30 | 2020-07-07 | 杭州普力材料科技有限公司 | Method for continuous production of polycarbonate-polyether polyol by preheating liquid phase method in pipeline manner |
| CN111378101A (en) * | 2020-04-26 | 2020-07-07 | 中山大学 | Preparation method of biodegradable carbon dioxide-based polyester-polycarbonate terpolymer |
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| WO2023066269A1 (en) * | 2021-10-19 | 2023-04-27 | 山东联欣环保科技有限公司 | Method for mixed feeding of phthalic anhydride and propylene oxide, equipment, and application |
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