KR101760169B1 - Manufacturing of Anionic polymerization initiators by continuous process and Anionic polymerization initiators by continuous process using the same - Google Patents

Abstract

The present invention relates to a process for producing a continuous process type anionic polymerization initiator and an anionic polymerization initiator.

Description

TECHNICAL FIELD The present invention relates to an anionic polymerization initiator and an anionic polymerization initiator,

The present invention relates to a process for producing a continuous process type anionic polymerization initiator and an anionic polymerization initiator.

In order to reduce carbon dioxide (CO ₂ ) emissions and improve fuel economy, high-efficiency, environment-friendly, high-performance tires are required to develop tire materials that meet such needs. Particularly, styrene-butadiene rubber (hereinafter referred to as SSBR) obtained by solution polymerization unlike emulsion polymerization generally has a structure change easily, and chain terminal ends are bonded or modified to reduce chain terminal movement and increase bonding force with carbon black And used as a rubber material for tire tread. In addition, as the silica filler is developed, low rolling resistance and high road surface braking force can be obtained at the same time. However, there is a need for a technique to disperse hydrophilic silica in combination with hydrophobic SSBR.

Such a method includes a method of enclosing the silica particles themselves with a hydrophobic substance, a method of using a coupling agent between silica and SSBR, and the like. In recent years, techniques for introducing a moiety capable of reacting and bonding with silica or a moiety serving to assist the SSBR polymer chain itself have been developed by using a denaturation initiator, a modified monomer, a denaturant, and the like in SSBR anionic polymerization. In particular, the modifier initiator is used as an essential material for the production of such modified SSBR since it initiates anionic polymerization and introduces functional groups at one end of the chain.

Hexamethylene lithium (HMI-Li) initiator, which is produced by the reaction of hexamethyleneimine (HMI) and n-butyllithium (BuLi) among the anionic polymerization initiators used in the synthesis of SSBR, same.

[Reaction Scheme 1]

However, since the solubility of the HMI-Li is low, the HMI-Li falls into precipitation over time and can be used as an initiator but has a lower reactivity than BuLi. In order to solve such disadvantages, conventionally, a conjugated diene (R) such as isoprene (IP) or 1,3-butadiene (BD) is further reacted after [Scheme 1] . Due to the addition of such conjugated dienes, the solubility in an organic solvent increases and a stable reaction can be achieved, and the reactivity as an initiator becomes higher than that of the HMI-Li state, which is sufficient to initiate anionic polymerization.

[Reaction Scheme 2]

N in the above Reaction Scheme 2 is 1 to 100.

However, the modified initiator thus produced is also unstable over time and falls into precipitation, or a very small amount of oxygen is combined with water to be inactivated. Therefore, the existing processes for preparing the above-mentioned polymerization initiator batchwise and then introducing the polymerization initiator into the polymerization reaction necessarily necessitate the storage step of the modifying initiator, thereby bringing about the above disadvantages. This may adversely affect the post-process, which may deteriorate the physical properties of the final synthesized SSBR, making it difficult to maintain a constant quality.

US registered patent US 005625017A US registered patent US 006080835A

In the prior art, anionic polymerization initiators were prepared by a batch process and used in the preparation of solution-polymerized styrene-butadiene rubber (SSBR). Or an anionic polymerization initiator and a solution polymerization styrene-butadiene rubber were produced simultaneously in a batch reactor in a single pot.

In the case of the former, inevitably, a step of storing a denatured initiator is required, and during the time period of storing the anion of the synthesized initiator, the surfactant reacts with various scavengers such as moisture and air to lose its activity. This may adversely affect the post-process, which may deteriorate the physical properties of the final synthesized SSBR, making it difficult to maintain a constant quality. In the latter case, the problem of storage can be solved as a step of causing polymerization reaction in the same batch reactor simultaneously with the initiator synthesis reaction. However, it is difficult to confirm whether the modification initiator is properly synthesized, and the physical properties are also lower than when the synthesized initiator is added. In addition, in all the conventional batch processes, there is a problem that the raw materials are directly introduced to produce by-products while mixing and reacting, and unreacted products are generated, resulting in lower polymerization yield.

In order to solve the above problems, the present invention uses a reactor including a static mixer in the form of a tube to produce an anionic polymerization initiator continuously during transportation. Particularly, it is an object of the present invention to provide a production method in which byproducts and unreacted materials are minimized by sequentially performing the first reaction and the second reaction during transport of the reactants, and the polymerization initiator added during the transfer is immediately fed into the polymerization vessel.

Accordingly, in the present invention, by introducing the reaction materials into a continuous process to synthesize a denaturation initiator, it can be directly introduced into a polymerization reaction without a storage step.

Furthermore, by improving the conventional batch reaction to a continuous reaction, it is possible to produce a continuous and consistent quality of initiator.

In order to achieve the above object, the present invention provides a process for producing an anion polymerization initiator of continuous process type in which an amine compound, an organolithium compound and a conjugated diene compound are introduced into a continuous reactor including a static mixer and reacted.

According to a preferred embodiment of the present invention, in the continuous process type anion polymerization initiator production method, the continuous reactor includes a first static mixer and a second static mixer, wherein (a) the first and second static mixers are mixed with an amine compound and an organic lithium Injecting a compound to prepare a first reactant; And (b) injecting the first reactant and the conjugated diene compound into a second static mixer to produce a second reactant.

Another aspect of the present invention provides an anionic polymerization initiator prepared by the production method according to the present invention.

According to a preferred embodiment of the present invention, the anion polymerization initiator may be a lithium amide type in which one terminal is modified with an amine.

The present invention can provide a method for producing an anionic polymerization initiator in a continuous reactor including a static mixer. In addition, the present invention can synthesize a polymerization initiator in a continuous polymerization reaction, directly inject it into the SSBR raw material and the polymerization vessel at the same time, and produce SSBR. As a result, the problems such as the physical properties of the SSBR can be minimized, and stable and constant quality products can be produced.

In addition, the process for preparing an anionic polymerization initiator of the present invention has a short reaction time and a high yield as compared with a batch reactor, and therefore can exert excellent effects such as economical reduction of the manufacturing process time.

Also, due to the high yield, economical and stable quality for mass production can be secured, and the manufacturing process time can be significantly reduced.

Fig. 1 is a schematic diagram of the preparation of an anionic polymerization initiator of the examples.
2 is a schematic diagram of the preparation of an anionic polymerization initiator of Comparative Example.
3 is a schematic diagram of an SSBR fabrication according to an embodiment of the present invention.

Hereinafter, the present invention will be described in detail. The following detailed description is merely an example of the present invention, and therefore, the present invention is not limited thereto.

When an anionic polymerization initiator is prepared in the conventional batch reactor, there is a problem that the synthesis yield is low and the initiator inactivation reaction occurs due to storage.

Therefore, the inventors of the present invention have found that the above problems can be solved by the continuous process formula manufacturing method and completed the present invention.

That is, the present invention provides a process for producing an anion polymerization initiator of continuous process type in which an amine compound, an organic lithium compound and a conjugated diene compound are introduced into a continuous reactor including a static mixer and reacted. The continuous reactor may include a static mixer as a form of a reactor therein.

According to a preferred embodiment of the present invention, the static mixer may be connected in series with one or more mixers selected from the group consisting of a plate mixer, a Kenics mixer, and a Sulzer mixer .

More specifically, a method for producing an anionic polymerization initiator produced in the continuous reactor of the present invention will be described.

According to a preferred embodiment of the present invention, the continuous reactor includes a first static mixer and a second static mixer, wherein (a) an amine compound and an organic lithium compound are injected into a first static mixer to produce a first reactant ; And (b) injecting the first reactant and the conjugated diene compound into a second static mixer to produce a second reactant.

First, the step (a) will be described.

This step is a step in which an amine compound and an organolithium compound are firstly reacted, and for example, HMI-Li can be produced.

Referring to FIG. 1, in step (a), an organic lithium compound solution is injected into the first injection port 101 and an amine compound solution is injected into the second injection port 102 simultaneously. Then, a first-order reaction occurs while being mixed in the first static mixer 103.

The amine compound in this step may be linear and / or cyclic amines having at least one secondary amine in the molecule. Specifically, according to one preferred embodiment of the present invention, the amine compound is at least one compound selected from the group consisting of dimethylamine, diethylamine, dipropylamine, dibutylamine, diisobutylamine, dipentylamine, dicyclohexylamine, diarylamine, And may include at least one member selected from the group consisting of dibenzylamine, trimethyleneimine, pyrrolidine, piperidine, methylpiperidine, hexamethyleneimine and heptamethyleneimine, preferably hexamethyleneimine ( HMI). The organic lithium compound may include at least one selected from the group consisting of conventional alkyl lithium, aryl lithium and alkenyl lithium, preferably n-butyl lithium (NBL).

In the present invention, the amine compound and the organic lithium compound may include a solvent and may be introduced into the reactor as an amine compound solution and an organic lithium compound solution, respectively.

The above solvents are hydrocarbon compounds that do not react with anions, and specifically include linear hydrocarbon compounds such as pentane, hexane, heptane and octane; Derivatives thereof having double bonds; Cyclic hydrocarbon compounds such as cyclohexane and cycloheptane; Aromatic hydrocarbon compounds such as benzene, toluene and xylene; And linear and cyclic ethers such as dimethyl ether, diethyl ether, anisole and tetrahydrofuran; Or a combination thereof. Preferably cyclohexane, hexane, tetrahydrofuran and diethyl ether, and most preferably cyclohexane. The concentration of the amine compound solution may be 0.1 to 50 wt%, the concentration of the organic lithium compound solution may be 0.1 to 30 wt%, and the remaining amount may be the solvent .

According to a preferred embodiment of the present invention, the reaction temperature of step (a) may be -30 to 100 ° C, and the reaction time may be 0.1 to 30 minutes. If the reaction temperature is less than -30 ° C, the feedstock may be frozen. If the reaction temperature exceeds 100 ° C, there may be a problem that the initiator is thermally decomposed. If the reaction time is less than 0.1 minute, there may be a problem that the reaction conversion rate is low, and if it exceeds 30 minutes, there is a problem that the production of side reaction products increases. Therefore, the total flow rate of the amine compound solution and the organic lithium compound solution may be 5 to 500 g / min. The molar ratio of the amine compound of the amine compound solution to the organolithium compound of the organic lithium compound solution may be 1: 1 to 2, preferably 1: 1 to 1.2. If the molar ratio of the organolithium compound is higher than the above range, there is a problem that the formation of byproducts increases. If the molar ratio of the amine compound is lower than the above range, unreacted amine compound increases.

In step (a) of this step, a hexamethyleneimine (HMI) solution as an amine compound solution and an n-butyllithium (NBL) solution as an organic lithium compound solution are injected into a first static mixer in a continuous reactor , Which is the first reaction step to produce HMI-Li. This is as shown in Reaction Scheme 1 below, and the solvent of the hexamethyleneimine (HMI) solution and n-butyllithium (NBL) solution is cyclohexane.

[Reaction Scheme 1]

When the molar ratio of hexamethyleneimine (HMI) and n-butyllithium (NBL) is firstly reacted within the above range, the desired intermediate material, HMI-Li, can be produced while lowering the production of unreacted materials and byproducts.

On the other hand, the above-mentioned HMI-Li has a low solubility in solvents and falls into precipitation after a lapse of time, and also has a problem that reactivity is lower than that of BuLi. Therefore, the following step (b) should be performed, but an anionic polymerization initiator containing a tertiary amine group to be prepared in the present invention can be prepared.

Next, the step (b) will be described.

This step is a step of reacting the first reactant produced in the step (a) with the conjugated diene compound (R), for example, to produce HMI-R-Li.

Referring to FIG. 1, the first static mixer 103 and the second static mixer 105 are connected to each other through a connection pipe 106 to connect the first reactant to the second static mixer 105 . Then, the conjugated diene compound solution is injected into the third injection port 104 formed at one end of the second static mixer 105. Then, the second reactant is mixed with the first reactant and the conjugated diene compound solution in the second static mixer 105, and the anion polymerization initiator flows out through the outlet 107. The first reactant may include a first reacted product and / or an unreacted HMI solution and an NBL solution.

The conjugated diene compound may be butadiene (BD) or isoprene (IP), preferably isoprene. In the present invention, The conjugated diene compound may be introduced into the reactor as a conjugated diene compound solution including a solvent. The solvent may be any conventionally usable solvent, preferably cyclohexane, hexane, tetrahydrofuran and diethyl ether, and most preferably cyclohexane. The concentration of the conjugated diene compound solution may be 1 to 100% by weight, and the remaining amount may be the solvent.

According to a preferred embodiment of the present invention, the reaction temperature in step (b) may be 20 to 120 ° C, and the reaction time may be 1 to 60 minutes. If the reaction temperature is lower than 20 ° C, there may be a problem that the reaction initiation speed is slow, and if it exceeds 120 ° C, there is a problem that the initiator is thermally decomposed. If the reaction time is shorter than 3 minutes, there may be a problem that the reaction time is insufficient. If the reaction time exceeds 60 minutes, there is a problem that unnecessary process cost is incurred in a state where the reaction is completed. Therefore, the total flow rate of the first reactant and the conjugated diene compound solution may be 5 to 500 g / min, and the total reaction time may be 3 to 60 minutes. The molar ratio of the amine compound of the amine compound solution to the conjugated diene compound of the conjugated diene compound solution may be 1: 1 to 100, preferably 1: 2 to 10. If the molar ratio of the conjugated diene compound is higher than the above range, the viscosity of the solution tends to increase. If the molar ratio of the amine compound is lower than the above range, there is a problem that the amine compound not attached with the diene compound increases.

In step (b) of this step, the first reactant reacted first in the first static mixer of the continuous reactor of the present invention and the isoprene solution are subjected to the second reaction in the second static mixer. This is as shown in Reaction Scheme 2 below, and the solvent of the isoprene solution is cyclohexane.

[Reaction Scheme 2]

As shown in Reaction Scheme 2, HMI-Li may be mixed with an isoprene solution to prepare an anionic polymerization initiator HMI-R-Li containing a tertiary amine group as a final product. N in the above Reaction Scheme 2 is an integer of 1 to 100.

According to a preferred embodiment of the present invention, the pressure inside the continuous reactor may be 1 to 5 bar.

On the other hand, in the case of the conventional method for producing an anionic polymerization initiator in a batch reactor, raw materials are directly introduced into the reaction system, and by-products are produced while mixing and reacting, and unreacted products are produced due to the reverse reaction.

However, in the present invention, fluids of an incoming raw material are continuously subjected to a first reaction and a second reaction in a first static mixer 103 and a second static mixer 105 of a continuous reactor, respectively, to produce an anionic polymerization initiator . That is, since the continuous process type production method of the present invention reacts stably and sequentially, by-products and unreacted products are not produced unlike the conventional processes. In addition, an anionic polymerization initiator can be produced with a high yield. Therefore, according to a preferred embodiment of the present invention, The amine compound conversion rate may be 95% or more.

In the present invention, in order to allow each injected material to flow in parallel to the first static mixer 103 and the second static mixer 105, and to prevent the flow in the reverse direction, Pressure control means for controlling the pressure of the fluid.

That is, according to a preferred embodiment of the present invention, the continuous process type reactor may further include a pressure control means for controlling an internal pressure. The amine compound, the organic lithium compound, and the conjugated diene compound injected into the production apparatus by the pressure control means can be mixed and reacted while flowing in the downstream direction at a pressure higher than the atmospheric pressure.

Another aspect of the present invention is directed to a first static mixer; A second static mixer; And a connection pipe connecting the first static mixer and the second static mixer. The present invention also provides an apparatus for manufacturing an anion polymerization initiator of continuous process type.

The static mixer may be connected in series with one or more mixers selected from the group consisting of a plate mixer, a Kenics mixer, and a Sulzer mixer.

The first static mixer may have a first injection port at one end and a second injection port in a direction perpendicular to the first injection port. In addition, a third inlet may be provided at one end of the second static mixer in a direction perpendicular to the connection pipe.

Referring to FIG. 1, an apparatus for producing an anion polymerization initiator of continuous process type according to an embodiment of the present invention includes a first static mixer 103; A second static mixer 105; And a connection pipe 106 connecting the first static mixer and the second static mixer. The second injection port 102 is formed at one end of the first static mixer 103 in a direction perpendicular to the first injection port 101 and the third injection port 104 is connected to the connection pipe 106, And is formed at one end of the second static mixer 105 in the vertical direction. And an outlet 107 is connected to the second static mixer.

According to a preferred embodiment of the present invention, the manufacturing apparatus may further include a pressure control means for controlling an internal pressure. The amine compound, the organic lithium compound and the diene compound injected into the production apparatus by the pressure control means can be mixed and reacted while flowing in the same direction.

Another aspect of the present invention provides an anionic polymerization initiator prepared by the method for producing an anionic polymerization initiator of the present invention. The anion polymerization initiator may be a lithium amide type in which one terminal is modified with an amine. That is, the anionic polymerization initiator provided in the present invention is an anionic polymerization initiator containing a tertiary amine group, and is preferably a lithium amide anion polymerization initiator having one terminal modified with an amine.

On the other hand, in the prior art, an anionic polymerization initiator was prepared by a batch process to prepare a solution-polymerized styrene-butadiene rubber (SSBR), or an anion polymerization initiator and a solution polymerization styrene-butadiene rubber were produced simultaneously in a batch reactor. In the case of the former, it is inevitably necessary to store the meta-initiator and thus the deactivation of the synthesized initiator takes place over time. This may adversely affect the post-process, which may deteriorate the physical properties of the final synthesized SSBR, making it difficult to maintain a constant quality. In the latter case, the problem of storage can be solved as a step of causing polymerization reaction in the same batch reactor simultaneously with the initiator synthesis reaction. However, it is difficult to confirm whether the modification initiator is properly synthesized, and the physical properties are also lower than when the synthesized initiator is added.

Therefore, the present invention produces an anionic polymerization initiator in a continuous manner during transportation using a reactor including a static mixer in the form of a tube. This provides a production method for preventing side reactions to obtain a high yield and simultaneously introducing an initiator into a polymerization tank. In addition, when an anionic polymerization initiator is prepared by the production method of the present invention and then directly fed into SSBR synthesis by on-demand synthesis, it is possible to solve the problem of the conventional initiator storage stability and to improve the anion initiator reactivity An amine group such as HMI can be introduced into the front-end of the SSBR.

Specifically, the method for preparing the anionic polymerization initiator of the present invention can be carried out continuously before the preparation of the SSBR.

That is, as shown in FIG. 2, (a) injecting an amine compound and an organolithium compound into a first static mixer 101 to produce a first reactant; (b) injecting the first reactant into a second static mixer 105 and mixing the second reactant with the conjugated diene compound to produce a second reactant; And (c) injecting the secondary reactant and the SSBR raw material into a batch reactor (301) to produce a solution-polymerized styrene-butadiene rubber (SSBR).

The raw material of the SSBR may be of any type as long as it can be used normally, and the other constitution and manufacturing method are well known in the art, and a detailed description thereof will be omitted.

In conclusion, the simultaneous preparation of the anion polymerization initiator and the SSBR by the on-demand synthesis method solves the problem of initiator storage stability and simultaneously increases the reactivity of the initiator so that the front- Can be modified with an amine compound. The present invention also provides a solution-polymerized styrene-butadiene rubber prepared by the process for preparing a solution-polymerized styrene-butadiene rubber (SSBR) according to the present invention, and the rubber can easily control the glass transition temperature to improve the braking performance. The present invention also provides a rubber composition for a tire comprising the rubber as a raw material rubber, wherein the composition has increased bonding force with a reinforcing agent such as silica or carbon black to reduce the movement of the end of the rubber chain, It is effective. According to one preferred embodiment of the present invention, the rubber composition for a tire can be used in a high performance racing tire.

Hereinafter, the present invention will be described in more detail with reference to examples. However, the embodiments of the present invention described below are illustrative only and the scope of the present invention is not limited to these embodiments. The scope of the present invention is indicated in the claims, and moreover, includes all changes within the meaning and range of equivalency of the claims. In the following Examples and Comparative Examples, "%" and "part" representing the content are based on weight unless otherwise specified.

Example  One

An anionic polymerization initiator was prepared using the continuous reactor according to the present invention shown in FIG. The first static mixer was a 1/4-inch diameter Kenics type static mixer having 500 helical elements inside. The second static mixer was a 1/4-inch diameter Kenics type static mixer with 2000 helical elements inside. Then, three stainless steel pressure vessels with a vacuum capacity of 3.75 L and a pressure of 6 bar were prepared. 800 g of cyclohexane and 150 g of hexamethyleneimine were added to the first pressure vessel to prepare an HMI solution. 200 g of cyclohexane and 615 g of n-butyllithium were added to another pressure vessel to prepare an NBL solution. 700 g of cyclohexane and 700 g of butadiene monomer were added to another pressure vessel to prepare a BD solution.

Then, a flow rate of 15 g / min of the HMI solution was injected into the first static mixer through the second inlet, and 10 g / min of the NBL solution was injected into the first static mixer. Then, the flow rate of the primary reactant of 25 g / min and the BD solution of 10 g / min were injected into the second static mixer through the third inlet. The first static mixer was maintained at 20 占 폚, and the second static mixer was maintained at 60 占 폚. The inside of the continuous reactor was adjusted to 3 bar each using a backpressure regulator.

The residence time of the first static mixer, that is, the reaction time was 5 minutes, and the residence time of the second static mixer was 10 minutes. Based on the molar ratio of HMI, the molar ratio of NBL was 1.01 and the molar ratio of BD was 4 times.

Comparative Example  One

As in Fig. 2, the same procedure as in Example 1 was performed except that a tube reactor was used instead of a static mixer.

Experimental Example  One

The HMI conversion ratio in Example 1 and Comparative Example 1 was analyzed by gas chromatography and calculated by the following formula (1).

[Equation 1]

As a result, the HMI conversion of the anionic polymerization initiator of Example 1 was about 95%, and the HMI conversion of the anionic polymerization initiator of Comparative Example 1 was about 37%.

101: first inlet, 102: second inlet, 103: first static mixer, 104: third inlet
105: second static mixer, 106: connecting pipe, 107: exhaust port, 201: first inlet port,
202: second inlet, 203: first tube reactor, 204: third inlet
205: second tube reactor, 206: connecting pipe, 207: outlet
301: SSBR batch reactor, 302: SSBR raw material inlet

Claims (18)

Introducing an amine compound, an organic lithium compound and a conjugated diene compound into a continuous reactor including a static mixer and reacting them to prepare an anion polymerization initiator; And
Preparing a styrene-butadiene polymer (SSBR) by charging the prepared anion polymerization initiator into a batch polymerization vessel for preparing a styrene-butadiene polymer (SSBR) without any additional aging time,
The step of producing the anionic polymerization initiator may include:
(a) injecting an amine compound and an organic lithium compound into a first static mixer to produce a first reactant; And
and (b) injecting the first reactant and the conjugated diene compound into a second static mixer to produce an anionic polymerization initiator. The method of producing a styrene-butadiene polymer (SSBR) The method according to claim 1,
Wherein the static mixer comprises at least one mixer selected from the group consisting of a plate mixer, a Kenics mixer, and a Sulzer mixer, and at least one of the mixers is connected in series to form a styrene-butadiene polymer (SSBR) . The method according to claim 1,
Wherein the continuous reactor comprises a step of controlling the internal pressure so that each injected material controls the fluid flow from the first static mixer to the second static mixer in one direction. The method according to claim 1,
Wherein the amine compound is a linear or cyclic amine having at least one secondary amine in the molecule. The method according to claim 1,
The amine compound may be selected from the group consisting of dimethylamine, diethylamine, dipropylamine, dibutylamine, diisobutylamine, dipentylamine, dicyclohexylamine, diarylamine, dibenzylamine, trimethyleneimine, pyrrolidine, (SSBR), which comprises at least one member selected from the group consisting of peridine, methylpiperidine, hexamethyleneimine, and heptamethyleneimine. The method according to claim 1,
Wherein the organolithium compound comprises at least one member selected from the group consisting of alkyl lithium, aryl lithium, and alkenyl lithium. The method according to claim 1,
Wherein the conjugated diene compound is butadiene or isoprene. ≪ RTI ID = 0.0 > 11. < / RTI > Claim 1
The pressure inside the continuous reactor is
1 to 5 bar. ≪ RTI ID = 0.0 > 11. < / RTI > Claim 3
The step (a)
Wherein the reaction temperature is from -30 to 100 占 폚, and the reaction time is from 0.1 to 30 minutes. The method of claim 3,
The step (b)
Wherein the reaction temperature is from 20 to 120 DEG C and the reaction time is from 1 to 60 minutes. The method according to claim 1,
Wherein the molar ratio of the amine compound to the organolithium compound is 1: 1 to 2. The method according to claim 1,
Wherein the molar ratio of the amine compound to the conjugated diene compound is 1: 1 to 100. An amine compound injection port for injecting an amine compound, and an organic lithium compound injection port for injecting an organic lithium compound,
A first static mixer in which the inlet of the amine compound and the inlet of the organic lithium compound are perpendicular to each other;
A second static mixer having an inlet for injecting a conjugated diene compound and an outlet for discharging the produced polymerization initiator into a batch reactor for polymerizing the styrene-butadiene polymer (SSBR); And
(SSBR) comprising a connecting pipe connecting the first static mixer and the second static mixer to the styrene-butadiene polymer (SSBR). 14. The method of claim 13,
Wherein the static mixer comprises at least one mixer selected from the group consisting of a plate mixer, a Kenics mixer, and a Sulzer mixer, wherein at least one of the mixers is connected in series to form a styrene-butadiene polymer (SSBR). Manufacturing apparatus. delete 14. The method of claim 13,
Wherein the second static mixer is provided at one end thereof with a conjugated diene compound injection port in a direction perpendicular to the connection pipe. 14. The method of claim 13,
An apparatus for producing a styrene-butadiene polymer (SSBR) further comprises a pressure control means for controlling an internal pressure, and the amine compound solution, the organic lithium compound solution and the conjugated diene compound solution Are mixed and reacted while flowing in the same direction. The apparatus for producing a styrene-butadiene polymer (SSBR) according to claim 1,
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