METHOD FOR PRODUCING POLYETHER KETONE KETONE AND POLYETHER KETONE KETONE PRODUCED THEREBY

Abstract

A method for producing polyether ketone ketone at a high yield is disclosed. According to the method, a catalyst injection rate is controlled during production to suppress scale formation, whereby the yield can be improved. A polyether ketone ketone produced by the method is disclosed. The method makes it possible to maintain an intrinsic viscosity (IV) of the polymer without a significant change and adjust a particle size of polyether ketone ketone by preventing an aggregation between resin particles, thereby suppressing scale formation.

Claims

1. A method for producing polyether ketone ketone, which obtains high molecular weight polyether ketone ketone at high yield, the method comprising: (a) preparing a reaction solution by adding at least one selected from diphenyl oxide (DPO) and 1,4-bis(4-phenoxybenzoyl)benzene (EKKE) to terephthaloyl chloride (TPC), isophthaloyl chloride (IPC), and a liquid reaction medium in a reactor and simultaneously dissolving the same; (b) cooling the reaction solution and injecting a catalyst thereto; and (c) after the injecting of the catalyst, directly blowing an inert gas into the reaction solution and stirring the inert gas.

2. The method of claim 1, wherein the catalyst is at least one selected from aluminum chloride (AlCl.sub.3), potassium carbonate (K.sub.2CO.sub.3), and iron(III) chloride (FeCl.sub.3).

3. The method of claim 1, wherein the catalyst is injected at a rate of 1 to 10 g/min.

4. The method of claim 1, wherein a cooling temperature in the step (b) is -10 to -5° C.

5. The method of claim 1, wherein a nozzle for directly blowing the inert gas into the reaction solution is formed in an upper or lower portion of the reactor, so that the inert gas is injected in multiple directions.

6. The method of claim 1, wherein the inert gas is at least one selected from nitrogen, helium, neon, argon, and krypton.

7. The method of claim 1, wherein the step (c) comprises raising the temperature of the reactor to 80 to 100° C. while stirring.

8. The method of claim 1, comprising washing after the step (c) and rinsing with deionized water (DI water).

9. The method of claim 8, further comprising performing vacuum drying at 170 to 190° C. after the rinsing.

10. The method of claim 1, wherein the reaction solution comprises at least one capping agent selected from benzoyl chloride, benzenesulfonyl chloride, 4-chlorobiphenyl, 4-phenoxybenzophenone, 4-(4-phenoxyphenoxy)benzophenone, and biphenyl 4-benzenesulfonylphenyl phenyl ether.

11. The method of claim 1, wherein the liquid reaction medium is at least one solvent selected from o-dichlorobenzene (oDCB) and dichloromethane.

12. A polyether ketone ketone produced by the method according to claim 1.

13. The polyether ketone ketone of claim 12, wherein the polyether ketone ketone has a yield of 90% or more.

14. The polyether ketone ketone of claim 12, wherein the polyether ketone ketone has a particle size of 250 to 2,000 .Math.m.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0041] FIG. 1 is a photograph showing a particle shape (particle size of 250 to 500 .Math.m) of Example produced according to the present invention.

[0042] FIG. 2 is a photograph showing a particle shape (particle size of 500 to 1,000 .Math.m) of Example produced according to the present invention.

[0043] FIG. 3 is a photograph showing a particle shape (particle size of 20 to 100 .Math.m) of Comparative Example.

[0044] FIGS. 4 and 5 are diagrams showing an apparatus capable of simultaneously flowing nitrogen gas into a reaction solution and stirring in a method for producing polyether ketone ketone according to the present invention.

MODE OF DISCLOSURE

[0045] Reference is made to the accompanying drawing which shows, by way of illustration, specific embodiments in which the present invention may be practiced. The embodiments will be described in detail in such a manner that the present invention can be carried out by those of ordinary skill in the art. It should be understood that various embodiments of the present invention are different from each other, but need not be mutually exclusive. For example, certain shapes, structures, and features described herein may be implemented in other embodiments without departing from the spirit and scope of the present invention in connection with one embodiment. In addition, it will be understood that the locations or arrangement of individual components in the disclosed embodiments can be changed without departing from the spirit and scope of the present invention. Therefore, the following detailed description is not to be taken in a limiting sense, and the scope of the present invention is to be limited only by the appended claims and the entire scope of equivalents thereof, if properly explained. Like reference numerals in the drawing refer to the same or similar functions throughout the various aspects.

[0046] Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawing, so that those of ordinary skill in the art can easily carry out the present invention.

[0047] Scale formation during polymerization of poly ether ketone ketone (PEKK) causes an operational problem. Therefore, in order to solve the resulting decrease in productivity, the present invention proposes a technique capable of increasing a particle size by controlling a catalyst injection rate and improving the yield by suppressing scale formation.

[0048] In the past, there was a problem in that a product had to be obtained through an additional process of controlling a particle size using a dispersing agent or breaking aggregated particles through a pulverization process after polymerization. However, the present invention provides a producing method according to a catalyst injection rate, which the catalyst injection rate is controlled to prevent aggregation of resin particles and prevent scale formation.

[0049] The method for producing polyether ketone ketone, capable of obtaining high molecular weight polyether ketone ketone at high yield, according to the present invention includes: (a) preparing a reaction solution by adding at least one selected from diphenyl oxide (DPO) and 1,4-bis(4-phenoxybenzoyl)benzene (EKKE) to terephthaloyl chloride (TPC), isophthaloyl chloride (IPC), and a liquid reaction medium in a reactor and simultaneously dissolving the same; (b) cooling the reaction solution and injecting a catalyst thereto; and (c), after the injecting of the catalyst, directly blowing an inert gas into the reaction solution and stirring the inert gas.

[0050] Polyether ketone ketone is a polymer produced by chain polymerization of terephthaloyl represented by chemical structure 1 and isophthaloyl represented by chemical structure 2, and characteristics of polyether ketone ketone are determined by the ratio of terephthaloyl to isophthaloyl. Terephthaloyl moiety is linear and rigid, and isophthaloyl moiety gives structural diversity due to its curved structure. Isophthaloyl affects flexibility, fluidity, and crystallization properties of polymer chains.

##STR00002##

##STR00003##

[0051] The catalyst may be at least one selected from aluminum chloride (AICI.sub.3), potassium carbonate (K.sub.2CO.sub.3), and iron(III) chloride (FeCI.sub.3), but is not limited thereto, and may be any catalyst that is commonly used as a catalyst for Friedel-Crafts acylation polymerization.

[0052] Here, the catalyst may be injected at a rate of 1 to 10 g/min or more. Preferably, the catalyst is injected at a rate of 1 to 3 g/min. More preferably, the catalyst is injected at a rate of 1 to 1.5 g/min. When the catalyst is injected at a rate of 1 to 10 g/min, the particle size of the produced polyether ketone ketone may increase. In addition, the yield of polyether ketone ketone to be produced can be improved. In this case, the yield of polyether ketone ketone may be 90% or more.

[0053] In addition, the polyether ketone ketone may have a particle size of 250 to 2,000 .Math.m.

[0054] The increase in particle size reduces the possibility of dust scattering during a product injection process, thereby facilitating operations. When a small particle size is requested according to product requirements, it is possible to reduce the particle size through additional pulverization after drying. This has an advantage that can control the particle size while maintaining the yield.

[0055] In the producing method according to the present invention, the catalyst is injected after the reaction solution is cooled. At this time, the temperature may vary depending on the catalyst, but is preferably -10 to -5° C.

[0056] The step (c) is characterized in that an agitator (stirrer) having a plurality of agitating blades is rotated to disperse the injected inert gas. At least two agitators may be provided in the reactor to rotate in at least two directions to cause a vortex phenomenon. The rotational shaft of the agitator may be provided to rotate by a predetermined angle alternately in the forward direction and the reverse direction. In addition, the agitating blade is provided to form a predetermined angle with the rotational shaft, thereby increasing the dispersion force of the composition in the reactor.

[0057] FIGS. 4 and 5 are diagrams showing an apparatus capable of simultaneously flowing nitrogen gas into a reaction solution and stirring in a method for producing polyether ketone ketone according to the present invention. Referring to FIGS. 4 and 5, in the method for producing PEKK according to the present invention, a nozzle for directly blowing the inert gas into the reaction solution is formed in the upper or lower portion of the reactor, so that the inert gas can be injected in multiple directions. Due to this, hydrochloric acid can be quickly and efficiently removed by the inert gas.

[0058] At this time, the inert gas is at least one selected from nitrogen, helium, neon, argon, and krypton. The inert gas may be used alone or in combination during the polymerization reaction.

[0059] After the inert gas is injected, the temperature of the reactor is raised to 80 to 100° C. while stirring and PEKK is polymerized. The polymerization reaction according to the present invention may be carried out in various reactors. Preferably, the polymerization reaction may be carried out in a continuous stirred tank reactor (CSTR) or a loop reactor.

[0060] The method for producing PEKK according to the present invention further includes washing the polymerized PEKK and rinsing the polymerized PEKK with deionized water (DI water). The washing may be carried out with a solution of methanol (CH.sub.3OH), hydrochloric acid, and sodium hydroxide (NaOH). Preferably, the washing may be carried out by methanol 3 times, hydrochloric acid once, and sodium hydroxide once. Here, the washing with hydrochloric acid and sodium hydroxide may be omitted.

[0061] After the washing, deionized water may be provided in the rinsing step. In this case, the rinsing may be preferably carried out 3 times.

[0062] After the rinsing, the method may further include obtaining PEKK polymerized resin powder by vacuum drying at 170 to 190° C.

[0063] When the three monomers are added to the liquid reaction medium and dissolved, a capping agent may be added and dissolved together. The capping agent is added to the polymerization medium to cap the polymer in at least one end of the polymer chain. This terminates the continuous extension of the chain and controls the molecular weight of the polymerized polymer. As a preferred capping agent, benzoyl chloride, benzenesulfonyl chloride, 4-chlorobiphenyl, 4-phenoxybenzophenone, 4-(4-phenoxyphenoxy)benzophenone, biphenyl 4-benzenesulfonylphenyl phenyl ether, and the like may be used.

[0064] In addition, the liquid reaction medium may be at least one solvent selected from o-dichlorobenzene (oDCB) and dichloromethane, but is not limited thereto, and may be any solve that is commonly used as a solvent for Friedel-Crafts acylation polymerization.

[0065] The polyether ketone ketone produced by the producing method described above exhibits improved physical properties, compared to polyether ketone ketone produced through the prior art. In addition, according to the present invention, the catalyst is injected at a rate of 1 to 10 g/min to prevent aggregation between resin particles and suppress scale formation, thereby obtaining high molecular weight polyether ketone ketone at high yield. Preferably, the yield of polyether ketone ketone may be 90% or more.

[0066] In addition, the polyether ketone ketone may have a particle size of 250 to 2,000 .Math.m.

[0067] In the method for producing polyether ketone ketone and the polyether ketone ketone produced thereby according to the present invention, the catalyst is injected at a rate of 1 to 10 g/min to prevent aggregation between resin particles and suppress scale formation, thereby obtaining an effect of large particle size, and the value of inherent viscosity (IV) remains unchanged, thereby obtaining an effect that can high molecular weight polyether ketone ketone at high yield, preferably 90% or more.

[0068] Hereinafter, the structure and operation of the present invention will be described in more detail with reference to preferred examples of the present invention. However, these examples are shown by way of illustration and should not be construed as limiting the present invention in any sense.

[0069] Since contents not described herein can be sufficiently technically inferred by those of ordinary skill in the art, descriptions thereof will be omitted.

Examples

Example 1

[0070] 26.6 g of EKKE, which was one selected from diphenyl oxide (DPO) and 1,4-bis(4-phenoxybenzoyl)benzene (EKKE) as monomers, 4.26 g of terephthaloyl chloride (TPC), 6.75 g of isophthaloyl chloride (IPC), and 0.48 g of benzoyl chloride as a capping agent were added to 750 g of o-dichlorobenzene (oDCB) as a reaction solvent in a reactor and were simultaneously dissolved, and the temperature of the reactor was lowered to -10 to -5° C. While maintaining the temperature of the solution constant at -10 to -5° C., 48 g of AICI.sub.3 as a catalyst was injected a rate of 1.1 g/min. After the injection of the catalyst is completed, the temperature of the reactor was raised to 90° C. while stirring the solution at the same time as blowing of N2 into the solution and was maintained for 30 minutes to polymerize PEKK. The polymerized resin was washed with methanol 3 times, 1 M hydrochloric acid, and 0.5 M NaOH solution, was rinsed with DI water 3 times, and was vacuum-dried at 180° C. to obtain PEKK polymerized resin.

Example 2

[0071] A PEKK polymerized resin was obtained in the same manner as in Example 1, except that a catalyst was injected at a rate of 1.2 g/min.

Example 3

[0072] A PEKK polymerized resin was obtained in the same manner as in Example 1, except that a catalyst was injected at a rate of 1.3 g/min.

Comparative Example 1

[0073] A PEKK polymerized resin was obtained in the same manner as in Example 1, except that a catalyst was injected at a rate of 0.8 g/min.

Comparative Example 2

[0074] A PEKK polymerized resin was obtained in the same manner as in Example 1, except that a catalyst was injected at a rate of 0.7 g/min.

Comparative Example 3

[0075] A PEKK polymerized resin was obtained in the same manner as in Example 1, except that a catalyst was injected at a rate of 0.6 g/min.

Experimental Example Inherent Viscosity (IV) and Yield Analysis

[0076] The IV and the yield of Examples 1 to 3 produced according to the present invention and Comparative Examples 1 to 3 were measured. The results thereof are shown in Table 1 below.

TABLE-US-00001 Classification Catalyst injection rate (g/min) IV (dℓ/g) Yield (%) Example 1 1.1 0.9 93 Example 2 1.2 0.9 96 Example 3 1.3 0.8 92 Comparative Example 1 0.8 0.9 66 Comparative Example 2 0.7 0.9 59 Comparative Example 3 0.6 1.0 62

[0077] Referring to FIGS. 1 to 3, as shown in Table 1 above, it was confirmed that the PEKK of Examples 1 to 3 produced by injecting the catalyst at a rate of 1 to 10 g/min according to the present invention exhibited a high yield, compared to Comparative Examples 1 to 3. In particular, Example 2, which was produced by injecting the catalyst at a rate of 1.2 g/min, exhibited the highest yield. Therefore, it can be seen that a rate of 1.2 g/min is the most preferable rate.

[0078] As can be seen from the results of Comparative Examples 1 to 3, when the catalyst was injected at a rate of less than 1 g/min, the yield was remarkably low. Therefore, it can be seen that the ideal catalyst injection rate range of the present invention is 1 to 10 g/min. Due to this, it was confirmed that the yield was improved by suppressing scale formation when the catalyst was injected at a rate of 1 to 10 g/min according to the present invention.

[0079] In addition, in the method for producing polyether ketone ketone and the polyether ketone ketone produced thereby according to the present invention, when the catalyst was injected at a rate of 1 to 10 g/min, the value of inherent viscosity (IV) remains unchanged, thereby obtaining an effect that can high molecular weight polyether ketone ketone at high yield, preferably 90% or more.

[0080] In addition, comparing the particle shapes of FIGS. 1 and 2 with the particle shape of FIG. 3, Examples 1 to 3 produced according to the present invention showed that the particle size of PEKK was increased. Therefore, it can be seen that the ideal catalyst injection rate range of the present invention is 1 to 10 g/min. Due to this, it was confirmed that, when the catalyst was injected at a rate of 1 to 10 g/min according to the present invention, there is an effect that the particle size was increased.

[0081] Therefore, the method for producing polyether ketone ketone and the polyether ketone ketone produced thereby according to the present invention have an effect of increasing the yield of polyether ketone ketone by controlling the catalyst injection rate so as to suppress scale formation.

[0082] In addition, in the method for producing polyether ketone ketone and the polyether ketone ketone produced thereby according to the present invention, when the catalyst was injected at a rate of 1 to 10 g/min, the value of inherent viscosity (IV) remains unchanged to prevent aggregation between resin particles and suppress scale formation, thereby obtaining an effect that can high molecular weight polyether ketone ketone at high yield, preferably 90% or more.

[0083] In addition, in the method for producing polyether ketone ketone and the polyether ketone ketone produced thereby according to the present invention, the particle size is increased by controlling the catalyst injection rate so as to suppress scale formation, thereby obtaining an effect of reducing the possibility of dust scattering and facilitating operations.

[0084] The method for producing polyether ketone ketone according to the present invention has an effect of obtaining particles having various sizes at high yield by drying and additionally pulverizing PEKK of large particles obtained at high yield.

[0085] While the present invention has been described by particular matters such as specific components and limited embodiments and drawings, this is provided only for helping the comprehensive understanding of the present invention. The present invention is not limited to the above-described embodiments, and it will be understood by those of ordinary skill in the art that various modifications and variations can be made thereto without departing from the scope of the present invention.

[0086] Therefore, it will be understood that the spirit of the present invention should not be limited to the above-described embodiments and the claims and all equivalent modifications fall within the scope of the present invention.