JPH0987392A - Continuous polycondensation polymer manufacturing apparatus and manufacturing method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To decrease the number of parts of a continuous production apparatus for a polycondensation polymer by decreasing the number of reactors by uniting a transesterification vessel with a part of an early-stage polymn. vessel and uniting the rest of the early-stage polymn. vessel with a final-stage polymn. vessel. SOLUTION: This apparatus comprises the first production apparatus 1 and the second production apparatus 35. In the first apparatus 1, a transesterification vessel 2 for producing an oligomer from a raw material mixture by transesterification and an early-stage polymn. vessel 3 for producing an intermediate polymer by the polycondensation of the oligomer are arranged vertically in series to form a vertical tower comprising vertically connected two towers, i.e., a transesterification tower as the upper tower and an early-stage polymn. tower as the lower tower. The second apparatus 35 is installed horizontally for producing the final polymer by the polycondensation of the intermediate polymer. In the first apparatus 1, the raw material entry port 13 of the upper tower is installed at the bottom side of the upper tower; a connecting pipe 7 connecting the upper and the lower tower is installed so that its upper end is at the liq. surface in the upper tower and its lower end is in the liq. in a liq. reservoir; and a treated liq. takeout port is installed at the bottom part.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus and method for producing polymer resins, and more particularly to an apparatus and method suitable for polymerizing polycondensation polymers such as polyethylene terephthalate and polycarbonate.

[0002]

2. Description of the Related Art Conventional polyethylene terephthalate (PE
As the polymerization method of T), a manufacturing process including a transesterification tank, an initial polymerization tank, and a polymerization tank is used as described in Process Compilation (1970) P892 edited by Japan Chemical Engineering Association. In an actual process, it is general that the transesterification tank is divided into several units, and the initial polymerization tank is also divided into two and used.

[0003]

An object of the present invention is to integrate a part of the transesterification tank and the initial polymerization tank into a first production apparatus, and integrate the rest of the initial polymerization tank and the final polymerization step into a second one.
As a manufacturing device, by reducing the number of reaction tanks, the number of drive parts, piping points, seal parts, etc. of each stirring tank is reduced.

[0004]

[Means for Solving the Problems] The above problems and objectives are to install a transesterification tank in an upper tower and an initial polymerization tank in a lower tower to integrate them into a first manufacturing apparatus, an intermediate polymerization tank and a final polymerization tank. By configuring a continuous polycondensation polymer manufacturing device with a horizontal second manufacturing device that integrates the above, the number of components and materials of the manufacturing device can be reduced, the number of man-hours for assembling and piping the device can be reduced, and the heat insulation and installation cost can be reduced. This is achieved by reducing the amount.

[0005]

The raw material continuously supplied from the inlet nozzle of the first manufacturing apparatus undergoes transesterification in the upper tower to form an oligomer, which is then supplied to the lower tower to evaporate volatile matter in each stirring chamber in the lower tower. However, it flows to the lower side of the lower tower, the polycondensation reaction proceeds efficiently, and the degree of polymerization is increased. Further, it is supplied to the second manufacturing apparatus, and subjected to stirring and surface renewal action by the stirring member in the horizontal stirring chamber, sequentially moving to the downstream side, and the reaction proceeds efficiently to increase the degree of polymerization to the target.

[0006]

FIG. 1 shows an embodiment of the present invention. In the figure, the left side shows a vertical first manufacturing apparatus, the right side shows a horizontal second manufacturing apparatus, 1 is a vertically long cylindrical first manufacturing apparatus main body and a heat medium jacket (not shown) on the outer periphery. Covered,
The container body is divided into two inside, the transesterification tank 2 is formed on the upper tower side, and the initial polymerization tank 3 is formed on the lower tower side. Raw material 13
Enters through a supply nozzle 4 provided in the lower part of the transesterification tank 2 and is agitated and mixed by a low-viscosity agitating blade 6 to accelerate the esterification reaction. A nozzle 11 for removing a by-product 12 produced by a transesterification reaction is attached to the upper part of the transesterification tank 2, and is separated and recovered by a condenser on the downstream side. The transesterification tank 2 and the initial polymerization tank 3 are connected by a connecting pipe 7. The upper end side of the transesterification tank 2 is raised to the liquid surface above the transesterification tank 2, and the lower end side thereof is provided in the upper part of the initial polymerization tank 3. The tray 8a is installed in the liquid pool, and the tray 8a is provided in the middle of the connecting pipe 7.
A flow rate adjusting valve 9 for adjusting the liquid level height of
The liquid level on the tray 8a is controlled to have a predetermined height. The vapor phase portion of the initial polymerization tank 3 is provided with a volatile matter extraction nozzle 10 for removing the volatile matter 14 generated by the polymerization reaction from the liquid surface of each tray and evaporated. A vacuum pump (not shown), a condenser (not shown) for collecting by-products, and the like are provided on the downstream side of the volatile matter removal nozzle 10 in order to reduce the pressure in the tank to a reduced pressure atmosphere. As shown in the figure, in this embodiment, the initial polymerization tank 3 has no stirring blade member inside. Instead of this agitating blade, downflow trays are installed in multiple stages to obtain a large surface renewal action. Inside the initial polymerization tank 3, ring-shaped trays 8a and cylindrical trays 8b are alternately arranged. On the inner peripheral upper surface side of the ring-shaped tray 8a and the outer peripheral upper surface side of the cylindrical tray 8b. Is provided with one or a plurality of notches, the processing liquid flows to the tray on the downstream side, reaches the bottom of the initial polymerization tank 3, and the initial polymerization product 15 is taken out from the extraction nozzle 5, Proceed to the next second manufacturing equipment.
In the figure, reference numeral 30 denotes a horizontally long cylindrical second manufacturing apparatus main body having a substantially circular cross section, the outer periphery of which is covered with a heat medium jacket (not shown), and two rotary shafts 31 extending in the inner longitudinal direction.
Is attached. For the rotary shaft 31, for example, the first patent
A stirring blade 32 formed of a scraping plate and a disc as shown in 024745 is installed. Each stirring blade 32
Rotates by scraping off the inner wall surface of the main body container 30, the stirring shaft, and the surfaces of the blades. Further, a volatile matter outlet nozzle is provided at the top of the main body 30 and is connected to a condenser and a vacuum pump (not shown) by piping to take out the reaction by-product 40. Further, the final polymerized product 41 of the treatment liquid is taken out from the outlet provided on the side opposite to the inlet.

The case of producing polyethylene terephthalate with the above constitution will be described. As a raw material of polyethylene terephthalate, a mixture of terephthalic acid and ethylene glycol or a mixture of dimethyl terephthalate and ethylene glycol is generally used. These raw materials are supplied to the transesterification tank 2 from the inlet nozzle 4 of the first manufacturing apparatus 1. The recommended operating condition of the present invention is that the transesterification tank has a stirring blade rotation speed of 100 to 200 rp.
m, temperature 240 ° C. to 260 ° C., pressure is atmospheric pressure or under elevated pressure to carry out the transesterification reaction. By-products (water and ethylene glycol or methanol and ethylene glycol) produced by the transesterification reaction are collected by a by-product collection condenser (not shown) installed upstream of the by-product removal nozzle 11. On the other hand, bis beta hydroxyethyl terephthalate (polymerization degree 4 to 8) produced by transesterification is supplied from the upper end of the connecting pipe 7 provided on the surface of the treatment liquid to the upper tray on the lower tower side.
At this time, the operating pressure of the lower tower is from 1.3 kPa to 133 Pa
Therefore, the flow rate adjusting valve 9 provided in the middle of the connecting pipe 7
The flow rate is adjusted so that the liquid height of the tray 8a is always constant. The processing liquid is the uppermost ring-shaped tray 8.
a to cylindrical tray 8b and ring-shaped tray 8a
It flows down to sequentially. At this time, since the treatment liquid is in a reduced pressure atmosphere, a by-product generated by the polymerization reaction is vaporized and vigorous foaming occurs. As a result, the treatment liquid is mixed and at the same time strongly receives a surface renewal action to accelerate the polymerization reaction. Will be done. By installing such a tray structure in a plurality of stages, it is possible to secure a residence time necessary for the reaction and obtain a desired degree of polymerization (10 to 30).
Further, the initial polymerization product 15 is continuously supplied from the inlet nozzle of the second manufacturing apparatus 30, and is stirred by the stirring blades 32 attached to the two stirring shafts 31 to renew the surface of the treatment liquid, so that ethylene glycol generated by the polymerization reaction is generated. And other volatile substances are removed by evaporation, the polycondensation reaction proceeds, and the highly viscous final polymer (degree of polymerization 90 to 11
0) 41. The volatile matter 40 such as ethylene glycol separated during this period is discharged from the outlet nozzle. The operating conditions at this time are, for example, a temperature of 260 to 300 ° C. and a pressure of 0.01.
It is performed in the range of 10 to 10 kPa and the rotation speed of 3 to 30 rpm. The processing liquid in the stirring chamber becomes a thin film by the stirring blades,
Since it undergoes a good surface renewal, it is possible to efficiently obtain a product polymer of good quality without deterioration due to retention.

Similarly, the present invention can be applied to continuous bulk polymerization of polycondensation resins such as polyamide and polycarbonate.

Another preferred embodiment of the present invention is shown in FIG. Since the configurations and operations of the transesterification tank 2 of the first manufacturing apparatus and the second manufacturing apparatus 30 in the figure are the same, description thereof will be omitted. The initial polymerization tank 3 of the present invention is connected to the transesterification tank 2 of the upper tower by a connecting pipe 7, and a flow rate adjusting valve 9 is provided between them.
The liquid level on the liquid tray 24 provided at the upper part of the lower tower is controlled so as to have a predetermined height. The liquid tray has a ring shape with a space in the center and is configured to have the same atmosphere as the downstream side. On the downstream side thereof, stirring chambers 20 forming a ring-shaped liquid pool are installed in multiple stages.
A stirring member 22 that stirs the inside of 0 is provided for each stirring chamber, and is connected to a stirring shaft 23 installed at the center of the initial polymerization chamber. Further, each stirring chamber 20 is provided with a connecting pipe 21 that connects the upper side liquid surface of each upper tray and the bottom side surface portion of the stirring chamber, so that the processing liquid always flows out from the liquid surface of the stirring chamber, The flow is supplied from the bottom side of the.

The case of producing polyethylene terephthalate with the above constitution will be described. As a raw material of polyethylene terephthalate, a mixture of terephthalic acid and ethylene glycol or a mixture of dimethyl terephthalate and ethylene glycol is generally used. These raw materials are supplied from the inlet nozzle 4 to the transesterification tank 2.
The transesterification tank has a stirring blade rotation speed of 100 to 200 rp
m, temperature 240 ° C. to 260 ° C., pressure is atmospheric pressure or under elevated pressure to carry out the transesterification reaction. By-products (water and ethylene glycol or methanol and ethylene glycol) produced by the transesterification reaction are collected by a by-product collection condenser (not shown) installed upstream of the by-product removal nozzle 11. On the other hand, bisbetahydroxyethyl terephthalate produced by transesterification is supplied from the upper end of the connecting pipe 7 provided on the surface of the treatment liquid to the upper tray on the lower tower side. At this time, since the operating pressure of the lower tower is 13 kPa to 133 Pa, the connecting pipe 7
The flow rate is adjusted by the flow rate adjusting valve 9 provided in the middle of the process so that the liquid height of the tray 24 is always constant. The treatment liquid on the uppermost tray flows to the stirring chamber 20 immediately downstream through the connecting pipe 21. The treatment liquid supplied to the stirring chamber 20 is stirred by the stirring member 22 to accelerate the polymerization reaction. In addition, the stirring action by the stirring blade activates the surface renewal action, and the reaction proceeds further. The reaction by-product generated at this time is removed from the volatile matter extraction nozzle 10 for removing the volatile matter 14. The treatment liquid after a predetermined residence time has elapsed in the initial polymerization tank is collected in the lower portion of the tank, the initial polymerization product 15 is taken out from the withdrawing nozzle 5, and further proceeds to the next vertical final polymerization tank (second manufacturing apparatus) for polymerization. The degree is increased.

Another preferred embodiment of the present invention is shown in FIG. The initial polymerization tank 3 and the second manufacturing apparatus 3 of the first manufacturing apparatus in the figure
Since the configuration and operation of 0 are the same, description thereof will be omitted.
The raw material 13 enters from a supply nozzle 4 provided at the bottom of the transesterification tank 2. At this time, the raw material 13 is heated to the transesterification reaction temperature by the external heat exchange 17 and supplied. Also,
The circulation liquid 18 circulated by the circulation pump 6 is supplied to the supply nozzle 4 from the circulation nozzle 16 in the upper part of the upper tower by merging with the material 13. The treatment liquid in the upper tower is agitated and mixed by the circulation action of the circulation pump 6, and the esterification reaction is promoted. A nozzle 11 for removing a by-product 12 produced by a transesterification reaction is attached to the upper part of the transesterification tank 2, and is separated and recovered by a condenser on the downstream side. The transesterification tank 2 and the initial polymerization tank 3 are connected by a connecting pipe 7. The upper end side of the transesterification tank 2 is raised to the liquid surface above the transesterification tank 2, and the lower end side thereof is provided in the upper part of the initial polymerization tank 3. It is installed in the liquid pool of the tray 8a, and a flow rate adjusting valve 9 for adjusting the liquid level height of the tray 8a is provided in the middle of the connecting pipe 7,
The upper liquid surface is controlled so as to have a predetermined height. The vapor phase portion of the initial polymerization tank 3 is provided with a volatile matter extraction nozzle 10 for removing the volatile matter 14 generated by the polymerization reaction from the liquid surface of each tray and evaporated. A vacuum pump (not shown), a condenser (not shown) for collecting by-products, and the like are provided on the downstream side of the volatile matter removal nozzle 10 in order to reduce the pressure in the tank to a reduced pressure atmosphere. As shown in the figure, in this embodiment, the initial polymerization tank 3
It does not have a stirring blade member inside. Instead of this agitating blade, downflow trays are installed in multiple stages to obtain a large surface renewal action. Inside the initial polymerization tank 3, ring-shaped trays 8a and cylindrical trays 8b are alternately arranged. On the inner peripheral upper surface side of the ring-shaped tray 8a and the outer peripheral upper surface side of the cylindrical tray 8b. Is provided with one or a plurality of notches, the processing solution flows to the tray on the downstream side, reaches the bottom of the initial polymerization tank 3, and the initial polymerization product 15 is taken out from the extraction nozzle 5, To the polymerization tank 30 (second manufacturing apparatus), and the degree of polymerization is further increased.

Another embodiment of the present invention is shown in FIG. In this embodiment, the initial polymerization tank of the lower tower of the first manufacturing apparatus of the embodiment shown in FIG. 3 is composed of a multi-stage stirring chamber 20 and a stirring member 22.

The initial polymerization tank 3 of the present invention is connected to the transesterification tank 2 of the upper tower by a connecting pipe 7, and a flow rate adjusting valve 9 is provided therebetween.
Is provided so that the liquid level on the liquid tray 24 provided at the upper part of the lower tower is controlled to a predetermined height. The liquid tray has a ring shape with a space in the center and is configured to have the same atmosphere as the downstream side. On the downstream side thereof, stirring chambers 20 forming a ring-shaped liquid pool are installed in multiple stages, and a stirring member 22 for thoroughly stirring the inside of the stirring chamber 20 is provided for each stirring chamber, and the center of the initial polymerization chamber is provided. It is connected to a stirring shaft 23 installed in the section. In addition, each stirring chamber 20
Is provided with a connecting pipe 21 that connects the upper liquid surface of each upper tray to the bottom side surface of the stirring chamber, and the processing liquid always flows out from the liquid surface of the stirring chamber and is supplied from the bottom side of the stirring chamber. It becomes a flow.

The case of producing polyethylene terephthalate with the above constitution will be described. As a raw material of polyethylene terephthalate, a mixture of terephthalic acid and ethylene glycol or a mixture of dimethyl terephthalate and ethylene glycol is generally used. These raw materials 13 are heated via the external heat exchanger 17 and supplied from the inlet nozzle 4 to the transesterification tank 2. In the transesterification tank, the circulating liquid 16 is circulated by the pump 6 from the circulation nozzle 16 provided at the upper part to uniformly stir the inside of the tank. The temperature in the tank is 240 ° C. to 260 ° C., and the transesterification reaction is carried out under atmospheric pressure or under pressure. By-products (water and ethylene glycol or methanol and ethylene glycol) produced by the transesterification reaction are collected by a by-product collection condenser (not shown) installed upstream of the by-product removal nozzle 11. On the other hand, bisbetahydroxyethyl terephthalate produced by transesterification is supplied from the upper end of the connecting pipe 7 provided on the surface of the treatment liquid to the upper tray on the lower tower side. At this time, the operating pressure of the lower tower is 1
Since the pressure is 3000 Pa to 133 Pa, the flow rate is adjusted by the flow rate adjusting valve 9 provided in the middle of the connecting pipe 7 so that the liquid height of the tray 24 is always constant. The treatment liquid on the uppermost tray flows to the stirring chamber 20 immediately downstream through the connecting pipe 21. The treatment liquid supplied to the stirring chamber 20 is stirred by the stirring member 22 to accelerate the polymerization reaction. In addition, the stirring action by the stirring blade activates the surface renewal action, and the reaction proceeds further. The reaction by-product generated at this time is removed from the volatile matter extraction nozzle 10 for removing the volatile matter 14. The treatment liquid after a lapse of a predetermined residence time in the initial polymerization tank collects in the lower part of the tank and the initial polymerization product 15 is taken out from the withdrawing nozzle 5 and proceeds to the second manufacturing apparatus 30 to undergo a surface renewal action in the apparatus to obtain a polymerization degree. Is increased.

Another embodiment of the present invention is shown in FIG. Since the present invention has the same construction and operation as the first manufacturing apparatus of FIG. 1 of another embodiment, detailed description thereof will be omitted. In this embodiment, a uniaxial horizontal device is used as the second manufacturing device. In the figure, reference numeral 35 denotes a horizontally long cylindrical second manufacturing apparatus main body having a substantially circular cross section, the outer periphery of which is covered with a heat medium jacket (not shown), and one rotary shaft 33 is attached in the inner longitudinal direction. Has been. The rotating shaft 33 is provided with a stirring blade 34 formed of, for example, a wheel-shaped disc and a scraping plate. Each stirring blade 34 scrapes against the inner wall surface of the main body container 35, the stirring shaft, and the surface of the blade to rotate. Further, the main body 35
An outlet nozzle for volatile matter is provided at the top of the pipe, and is connected to a condenser and a vacuum pump (not shown) by piping to take out the reaction by-product 40. The initial polymerization product 15 supplied from the first manufacturing apparatus undergoes a surface renewal action in the main body container 35 to increase the degree of polymerization, and the final polymerization product 41 of the treatment liquid is taken out from the outlet provided on the side opposite to the inlet. .

Another embodiment of the present invention is shown in FIG. Since the present invention has the same construction and operation as the first manufacturing apparatus of FIG. 2 of another embodiment, detailed description thereof will be omitted. In this embodiment, a uniaxial horizontal device is used as the second manufacturing device. Furthermore, as another embodiment of the present invention, the first embodiment shown in FIG. 3 or FIG.
The same operation and effect can be obtained when a uniaxial horizontal device is used as the manufacturing device and the second manufacturing device, but detailed description thereof will be omitted.

[0017]

According to the present invention, a polycondensation resin of a polycondensation system can be produced by connecting a first manufacturing apparatus having an integrated structure of a transesterification tank and an initial polymerization tank to a second manufacturing apparatus which is a horizontal final polymerization tank. There is an advantage that the device price of the continuous manufacturing device can be reduced and the installation space of the device can be significantly reduced.

[Brief description of drawings]

FIG. 1 is a device configuration diagram showing an embodiment of the present invention.

FIG. 2 is a device configuration diagram showing another embodiment of the present invention.

FIG. 3 is a device configuration diagram showing another embodiment of the present invention.

FIG. 4 is a device configuration diagram showing another embodiment of the present invention.

FIG. 5 is a device configuration diagram showing another embodiment of the present invention.

FIG. 6 is a device configuration diagram showing another embodiment of the present invention.

[Explanation of symbols]

DESCRIPTION OF SYMBOLS 1 ... Main body of a manufacturing apparatus, 2 ... Transesterification tank, 3 ... Initial polymerization tank, 4 ... Supply nozzle, 5 ... Extraction nozzle, 6 ... Low viscosity stirring blade, 7 ... Connection pipe, 8a ... Ring tray, 8b
... Cylindrical tray, 9 ... Flow rate adjusting valve, 10 ... Volatile substance taking-out nozzle, 11 ... By-product removing nozzle, 12 ... By-product, 13 ... Raw material, 14 ... Volatile substance, 15 ... Prepolymer, 1
6 ... Circulation nozzle, 17 ... External heat exchange, 18 ... Circulating liquid, 20
... stirring chamber, 21 ... connecting pipe, 22 ... stirring blade, 23 ... stirring shaft, 24 ... tray, 30 ... second manufacturing apparatus body, 31 ... rotating shaft, 32 ... stirring blade, 33 ... stirring shaft, 34 ... stirring blade Three
5 ... 2nd manufacturing apparatus main body, 40 ... By-product, 41 ... Final polymer.

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Takatoshi Kinoshita 794 Higashi-Toyoi, Kudamatsu City, Yamaguchi Prefecture Stock company Hitachi Ltd. Kasado Plant

Claims (15)

[Claims] 1. A transesterification tank for producing an oligomer by a transesterification reaction from a mixture of raw materials in a production apparatus for continuously producing a polycondensation polymer, and a polycondensation reaction between the oligomer and an initial stage of producing an intermediate polymer. By vertically arranging a polymerization tank in series and connecting a transesterification tower of an upper tower and an initial polymerization tower of a lower tower so as to form an integrated structure, a vertical type first manufacturing apparatus and a polycondensation reaction An apparatus for continuously producing a polycondensation polymer, comprising a horizontal second production apparatus for producing a final polymer from an intermediate polymer. 2. The continuous manufacturing apparatus according to claim 1, wherein the raw material inlet of the upper tower of the first manufacturing apparatus is provided on the bottom side of the upper tower,
Raise the connecting pipe of the upper tower and the lower tower to the upper liquid surface of the upper tower,
The end of the connecting pipe of the lower tower is provided in the liquid in the liquid pool provided at the upper part of the lower tower, and the outlet of the processing liquid is provided at the bottom of the lower tower. Continuous manufacturing equipment. 3. The continuous production apparatus according to claim 2, wherein a flow rate adjusting valve is provided in a connecting pipe connecting the upper tower and the lower tower to control the flow rate to a predetermined value even when there is a pressure difference between the upper tower and the lower tower. An apparatus for continuously producing a polycondensation polymer, which is characterized in that 4. The continuous production apparatus according to claim 2, wherein the upper tower is provided with a low-viscosity stirring blade for uniformly stirring and mixing the inside of the tank, and the lower tower is provided with a tray having a plurality of liquid pools. Then
An apparatus for continuously producing a polycondensation polymer, which has a structure without a stirring blade. 5. The continuous manufacturing apparatus according to claim 4, wherein a plurality of trays installed in the lower tower have a circular shape having a cross-sectional shape of an L-shaped ring-shaped tray and a diameter larger than the diameter of the ring-shaped hollow portion. An apparatus for continuous production of polycondensation polymer, characterized in that a plurality of trays are alternately installed. 6. The continuous manufacturing apparatus according to claim 5, wherein a part or a plurality of cutout trays are provided on each of the inner diameter side of the L-shaped ring tray and the outer diameter side of the circular tray installed in the lower tower. An apparatus for continuously producing a polycondensation polymer, characterized in that the treatment liquid in the inside is made to flow down. 7. The continuous manufacturing apparatus according to claim 2, wherein the upper tower is provided with a low-viscosity stirring blade for uniformly stirring and mixing the inside of the tank, and the lower tower is divided into a plurality of stages in the longitudinal direction inside the main body. Then, each of the ring-shaped members having an L-shaped cross section forms a stirring chamber having a space in the center, and the stirring members for thoroughly stirring the respective stirring chambers are attached to a stirring shaft provided in the center of the lower tower. An apparatus for continuously producing a polycondensation polymer, which is characterized in that 8. The continuous production apparatus according to claim 7, wherein a connecting pipe for connecting the upper and lower stirring chambers provided in the lower tower is the liquid surface side on the upper stirring chamber side and the stirring chamber bottom is on the lower stirring chamber side. An apparatus for continuously producing a polycondensation polymer, which has a structure of connecting to a polycondensation polymer. 9. The continuous production apparatus according to claim 2 or 3, wherein the upper tower is provided with an external circulation type stirring mechanism for uniformly stirring and mixing the inside of the tank, and has a structure without stirring blades. The continuous production equipment of the characteristic polycondensation polymer. 10. The continuous manufacturing apparatus according to claim 1,
The second manufacturing apparatus has an inlet and an outlet for the liquid to be treated at the lower portions of both ends in the longitudinal direction of the substantially horizontal substantially cylindrical container body, and a stirring member is attached to a rotary shaft provided in the longitudinal direction inside the body. And a device that rotates close to the inside of the main body,
An apparatus for continuous production of polycondensation polymers, characterized in that a volatile matter outlet is provided at the top of the main body. 11. The continuous manufacturing apparatus according to claim 10, wherein the second manufacturing apparatus has a biaxial stirring blade structure, and scrapes between the respective stirring blades, the surface of the stirring shaft, and the inner wall surface of the stirring chamber. An apparatus for continuously producing a polycondensation polymer, wherein a substantially disk-shaped stirring member having a take-up plate is attached to a rotary shaft. 12. The continuous manufacturing apparatus according to claim 10, wherein the second manufacturing apparatus has a uniaxial stirring blade structure, and the stirring blade is equipped with a scraping plate for scraping all over the inner wall surface of the stirring chamber. An apparatus for continuously producing a polycondensation polymer, wherein a disc-shaped stirring member is attached to a rotary shaft. 13. The continuous manufacturing apparatus according to claim 10, wherein the horizontal second manufacturing apparatus is provided with a plurality of partition plates in the longitudinal direction of the main body, and the height of the partition plates is adjusted according to the viscosity of the processing liquid inside. The continuous production apparatus for polycondensation polymer, characterized in that the amount of treatment liquid held between the respective partition plates is adjusted to an optimum amount. 14. A continuous production apparatus according to any one of claims 1 to 13, wherein a raw material for a polycondensation polymer is supplied to the first production apparatus, and transesterification is carried out in the upper column under substantially atmospheric pressure. The reaction is carried out to form an oligomer, and the polycondensation reaction is carried out in a lower column in a reduced pressure atmosphere to obtain an initial polymerization reaction product or an intermediate polymerization reaction product having a low to medium polymerization degree, and further producing the reaction product in the second production. A continuous production method of a polycondensation polymer, which comprises supplying a reactor and performing a polycondensation reaction operation in a reduced pressure atmosphere to obtain a reaction product having a high degree of polymerization. 15. A continuous production apparatus according to any one of claims 1 to 13, wherein a mixture of terephthalic acid and ethylene glycol or a mixture of dimethyl terephthalate and ethylene glycol is supplied as a raw material to the first production apparatus, and the upper tower is provided. At a temperature of 200 ° C to 270 ° C at a pressure of atmospheric pressure or under pressure to perform a transesterification reaction to produce bisbetahydroxyethyl terephthalate, which is flowed down to a lower column at a temperature of 200 ° C to 300 ° C and a pressure of 10 kPa to 0 Within the range of 1 kPa, volatile substances such as ethylene glycol are evaporated and sequentially moved to the stirring chamber on the downstream side to increase the degree of polymerization, and then supplied to the second manufacturing apparatus, and the temperature is from 260 ° C to 300 ° C and the pressure is from 10 kPa. A polyethylene terephthalate series that increases the degree of polymerization by performing a polycondensation reaction in the range of 0.01 kPa Polycondensation method.