CN206616174U - A kind of system for being modified continuous polycondensation - Google Patents

Abstract

The utility model relates to a system for modifying continuous polyester, which comprises a first esterification reactor, a first diesterization reactor, a second diesterization reactor, a third diesterization reactor, a pre- Polycondensation tank, the upper part of the diesterification first reaction tank is connected to the catalyst, the third monomer and the mixed steam main pipe through the feed and discharge pipelines respectively, and the upper part of the diesterization second reaction tank is respectively connected to the feed and discharge pipelines The pipelines are connected to the catalyst, the fourth monomer and the mixed steam main pipe, and the upper part of the third diesterization reaction kettle is respectively connected to the catalyst, antioxidant and mixed steam main pipe through the feed and discharge pipelines. The utility model is a three-pot diesterization process flow, each pot is added with different additives, and the reaction temperature and pressure are controlled according to the gradient, which is suitable for modified continuous polyester: atmospheric pressure boiling dyeable cationic dye can dye copolyester (ECDP) industrial production.

Description

A system for modifying continuous polyester

technical field

The utility model belongs to the application field of modified polyester, in particular to a system for modifying continuous polyester.

Background technique

Because the polyester macromolecules are neatly arranged and dense, and have a high degree of orientation, crystallinity and glass transition temperature, its hygroscopicity is poor. In addition, its molecular chain lacks active groups that can bond with dyes. In the presence of carriers, it is difficult for various dyes or substances with special properties to diffuse into PET molecules, which brings difficulties to the preparation process of dyeing or polyester with special properties, so it can only be carried out with disperse dyes under high temperature and high pressure or with a carrier dyeing. Therefore, in order to obtain high-performance modified polyester, domestic and foreign countries have been devoted to the research on the "modification" of polyester fiber, and various modified polyesters have appeared successively. Among them, the method of chemical modification is a relatively stable method. , long-lasting and effective methods, which include methods such as copolymerization, blending, and surface chemical reactions, and the copolymerization method is one of the important means in chemical modification. At present, the modified fibers prepared by the copolymerization method include disperse dyes and normal pressure Dyeable polyester, anionic dyeable polyester (ADP) and cationic dyeable polyester, polyester fiber surface modification, etc., and the more typical one is cationic dyeable polyester fiber, which is based on terephthalic acid (PTA) and ethylene glycol (EG) are the main raw materials, and a certain amount of third monomer is added in the synthesis stage, for example: sulfonates, dimethyl isophthalate-5-sodium sulfonate (SIPM), Bishydroxyethyl isophthalate-5-sodium sulfonate (SlPE), and the fourth monomer, for example: ester polybasic acid, oxalic acid, adipic acid, prepared by copolymerization, it can be divided into There are two kinds of high temperature and high pressure cationic dyeable copolyester (CDP) and atmospheric pressure boiling cationic dyeable copolyester (ECDP).

In the Chinese patent document CN10101735430A, a method for continuously preparing modified polyester is provided, including the following steps: PET and EG are added into the esterification tank from the feed port to carry out esterification reaction to obtain ethylene terephthalate The ester oligomer, after which the oligomer melt is input into the polycondensation tank through the pipeline to carry out polymerization reaction with the three-monomer or multi-monomer and additives, and the modified polyester melt obtained by the reaction is subsequently pelletized or directly spun, The two ends of the pipeline are respectively connected with the esterification tank and the polycondensation tank, and when the oligomer melt flows through the pipeline, the ethylene glycol solution of the tri-monomer or multi-monomer and the additive is added into the pipeline, and the oligomer and the oligomer The product melt is mixed evenly in the pipeline, and the reaction in the later stage of esterification is carried out at the same time, and then enters the polycondensation tank for polymerization. This method can only produce high-temperature and high-pressure cationic dye-dyeable copolyester (CDP), but cannot produce normal-pressure boiling dyeable cationic dye-dyeable copolyester (ECDP), and the addition position of the catalyst and the third monomer is on the pipeline , cannot be added step by step and fully mixed evenly, and the temperature cannot be controlled step by step.

Contents of the invention

The utility model aims to solve the above-mentioned defects, and provides a three-pot diesterization process flow, in which different additives are added to each pot, and the reaction temperature and pressure are controlled according to the gradient, which is suitable for modified continuous polyester: normal pressure boiling Industrial production of dyeable cationic dyeable copolyesters (ECDP).

In order to overcome the defects existing in the background technology, the technical solution adopted by the utility model to solve the technical problem is: a system for modifying continuous polyester, comprising a monoesterification kettle, a diester The first reactor for diesterification, the second reactor for diesterification, the third reactor for diesterification and the precondensation reactor, the first reactor for diesterification, the second reactor for diesterification, the third reactor for diesterification There are feed inlets and discharge pipes on the kettles, and the first diesterization reaction kettle, the second diesterification reaction kettle, and the third diesterification reaction kettle are all jacketed.

In a preferred embodiment of the present invention, the upper part of the diesterification first reactor is respectively connected to the catalyst and the third monomer through the feed port, and the upper part of the diesterization second reactor is connected to the catalyst through the feed port respectively. and the fourth monomer, the upper part of the third diesterization reactor is connected to the catalyst and the antioxidant through the feed inlet pipeline respectively, the first diesterization reactor, the second diesterization reactor, the diesterization reactor The top of the third reactor is also connected to the mixed steam main pipe through the discharge pipeline.

In a preferred embodiment of the present invention, the tops of the first diesterization reactor, the second diesterization reactor, and the third diesterization reactor are equipped with agitators that go deep into the interior.

The beneficial effects of the utility model are: the utility model is a three-pot diesterization process flow, each pot adds different additives, and the reaction temperature and pressure are controlled according to the gradient, which is suitable for modified continuous polyester: normal pressure boiling dyeing Industrial production of cationic dye-dyeable copolyesters (ECDP).

Description of drawings

Below in conjunction with accompanying drawing and embodiment the utility model is further described.

Fig. 1 is a structural representation of the utility model.

detailed description

The preferred embodiments of the utility model will be described in detail below in conjunction with the accompanying drawings, so that the advantages and characteristics of the utility model can be more easily understood by those skilled in the art, so that the protection scope of the utility model can be defined more clearly .

A kind of system that is used for modifying continuous polyester as shown in Fig. The third reactor 4 for esterification and the precondensation reactor 5, the first reactor 2 for diesterization, the second reactor 3 for diesterization, and the third reactor 4 for diesterification are equipped with feed inlets and discharge pipes , and the first diesterization reaction kettle 2, the second diesterization reaction kettle 3, and the third diesterification reaction kettle 4 are all jacketed structures. The upper part of the diesterization first reactor 2 is respectively connected to the catalyst and the third monomer through the feed port, and the third monomer is a sulfonate, for example: dimethyl isophthalate-5-sodium sulfonate (SIPM) , Bishydroxyethyl isophthalate-5-sodium sulfonate (SlPE); the upper part of the diesterification second reactor is connected to the catalyst and the fourth monomer through the feed port respectively, and the fourth monomer is an ester type polybasic acid, For example: oxalic acid, adipic acid; the upper part of the diesterization third reaction kettle is connected to the catalyst and antioxidant through the feed inlet pipeline respectively. The catalysts in the above are all antimony, such as: antimony trioxide or ethylene glycol Antimony; Antioxidants are mainly complexes of hindered phenols and phosphites, for example: bis (3,5-di-tert-butyl-4-hydroxybenzyl monoethyl phosphate) calcium salt, diesterification first reaction kettle, The tops of the second diesterization reaction kettle and the third diesterification reaction kettle are also connected to the mixed steam main pipe through the discharge pipeline.

The tops of the first diesterification reaction kettle 2, the second diesterification reaction kettle 3, and the third diesterification reaction kettle 4 are all provided with a stirrer 6 that goes deep into the interior, so that they can be mixed fully and uniformly to ensure step-by-step Reaction efficiency.

The ethylene terephthalate oligomer from the first esterification tank 1 enters from the bottom of the first diesterization reactor 2, and then enters with the catalyst and the third monomer that enters from the top of the first diesterization reactor 2 , enter the reaction under the sufficient mixing of the first diesterification reactor 2 stirrer, control the pressure at 30-20kpa (A), control the temperature at 208-212 ° C, the gas phase produced by the diesterification first reactor 2 passes through The top of it enters the mixed steam main pipe, and the material after the reaction of the first diesterization reactor 2 enters from the bottom of the second diesterization reactor 3, and then enters with the catalyst and the fourth monomer entered from the top of the second diesterization reactor 3, Enter the reaction under the full mixing action of the second diesterification reaction kettle 3 stirrer, control the pressure at 20-10kpa (A), control the temperature at 220-224 ° C, the gas phase generated by the diesterification second reaction kettle 3 passes through it The top enters the mixed steam main pipe, and the material after the reaction of the second diesterification reactor 3 enters from the bottom of the third diesterization reactor 4, and then enters with the catalyst and antioxidant at the top of the diesterification third reactor 4, in the second The third esterification reaction tank 4 enters the reaction under the full mixing action of the agitator, the pressure is controlled at 10-5kpa (A), the temperature is controlled at 253-257°C, and the gas phase generated in the second reaction tank 4 of the diesterification enters through its top. The mixed steam main pipe, the third diesterification reactor 4, after the reaction, the material enters the pre-condensation reactor 5 for further reaction, and then continues to polymerize through the final polycondensation reactor (not in the scope of this patent), and finally produces modified polyester: normal pressure boiling dyeing Type cationic dyeable copolyester (ECDP).

The above is only an embodiment of the utility model, and does not limit the patent scope of the utility model. Any equivalent structure or equivalent process conversion made by using the utility model specification and accompanying drawings, or directly or indirectly used in other Related technical fields are all included in the patent protection scope of the present utility model in the same way.

Claims (3)

1. A system for modifying continuous polyester, characterized in that: it comprises a first esterification kettle, a first diesterification reaction kettle, a second diesterification reaction kettle, a diesterification reaction kettle, and a diesterification reaction kettle connected successively by a pipeline at the bottom end. The third reaction kettle and the precondensation kettle, the first reaction kettle of diesterization, the second reaction kettle of diesterization, and the third reaction kettle of diesterification are all equipped with a feed inlet and a discharge pipe, and the diesterization The first reactor, the second diesterization reactor and the third diesterization reactor are all jacketed. 2. The system for modifying continuous polyester according to claim 1, characterized in that: the upper part of the diesterization first reactor is respectively connected to the catalyst and the third monomer through the feed port, and the diesterization The upper part of the second reactor is connected to the catalyst and the fourth monomer through the feed port, the upper part of the third diesterization reactor is connected to the catalyst and the antioxidant through the feed port pipeline, and the first diesterization reactor , the tops of the second diesterification reaction kettle and the third diesterification reaction kettle are also connected to the mixed steam main pipe through the discharge pipeline. 3. The system for modifying continuous polyester according to claim 1, characterized in that: at the top of the first diesterization reactor, the second diesterization reactor, and the third diesterization reactor All are equipped with a stirrer that goes deep into the interior.