KR20220040944A - Processing method of polyolefin elastomer copolymer having ultra low density and high elastic property and polyolefin elastomer copolymer produced thereby - Google Patents

Abstract

The present invention provides a preparation method of a polyolefin elastomer copolymer that comprises a step (a) of inputting one type of olefin monomer selected from a liquid 1-butene monomer, a 1-hexene monomer, and a 1-octene monomer; ethylene gas; and a Ziegler-Natta type Ti-supported catalyst into a reactor; and a step (b) of performing a polymerization reaction at 50 to 7 ℃, and a polymer for an automotive interior and exterior material, shoes, or cable sheathing, which comprises the polyolefin elastomer copolymer prepared thereby.

Description

Method for producing polyolefin elastomer copolymer having ultra-low density and high elasticity, and polyolefin elastomer copolymer prepared thereby

The present invention relates to a method for preparing a polyolefin elastomer copolymer having ultra-low density and high elasticity, and to a polyolefin elastomer copolymer prepared thereby.

Polyolefin elastomer is a thermoplastic resin with rubber-like properties, and unlike polyurethane and vulcanized rubber, which are non-recyclable thermosetting resins, polyolefin elastomer is recyclable, so it is in the spotlight as a plastic resin to replace rubber and polyurethane elastomers. Polyolefin elastomer is known as a thermoplastic elastomer that can be used for various purposes such as automobile interior materials, shoes, cables, etc. by kneading with polyethylene or polypropylene resin.

Polyolefin elastomers are generally prepared by copolymerizing ethylene and 1-butene or copolymerizing ethylene and 1-octene using a metallocene catalyst. However, this method uses an expensive metallocene catalyst, which is economical, and the molecular weight distribution of the polyolefin elastomer produced is narrow due to the characteristics of the metallocene catalyst. It has the disadvantage of being low.

Therefore, various polyolefin elastomer polymerization methods have been developed to compensate for the above disadvantages. For example, polyolefin elastomers prepared by copolymerizing known 1-butene and propylene using a Ziegler-Natta catalyst have been developed.

However, the polyolefin elastomer as described above does not properly find a clue for solving the problems of low workability and high density and low elasticity, which have been problems in the prior art.

In addition, the situation does not provide physical properties that can replace the polyolefin elastomer made by copolymerization of ethylene and 1-butene or ethylene and 1-octene, which are conventionally used for interior and exterior materials for automobiles, shoes, and cable coverings.

On the other hand, currently commercially produced butene-1-based copolymers are generally produced by a solution polymerization method, and thus have a disadvantage in that production facilities such as high-cost devolatilization devices are required to remove the solvent. Therefore, improvement is also required.

Korean Patent Publication No. 10-2011-0138254

The present inventors have made intensive efforts to solve the above problems of the prior art, and found an efficient method for producing a polyolefin elastomer copolymer having sufficient elasticity and workability to be used in automobile interior and exterior materials, shoes, cable coverings, etc. was completed.

Therefore, an object of the present invention is to provide an efficient method for preparing a polyolefin elastomer copolymer having ultra-low density, high elasticity and excellent processability.

Another object of the present invention is to provide a method for producing a polyolefin elastomer copolymer capable of efficiently producing a copolymer using a conventional olefin homopolymer production apparatus.

Another object of the present invention is to provide a polyolefin elastomer copolymer manufactured by the above manufacturing method and having an ultra-low density, high elasticity, and excellent processability sufficient to be used in automobile interior and exterior materials, shoes, cable coverings, and the like.

In order to achieve the above object, the present invention

(a) one kind of olefin monomer selected from 1-butene monomer, 1-hexene monomer and 1-octene monomer in a liquid state in a reactor; ethylene gas; and adding a Ziegler-Natta type catalyst supported on Ti; and

(B) performing a polymerization reaction at 50 ~ 70 ℃; provides a method for producing a polyolefin elastomer copolymer comprising a.

In addition, the present invention,

It provides a polyolefin elastomer copolymer prepared by the above method.

According to the method for producing a polyolefin elastomer copolymer of the present invention, a polyolefin elastomer copolymer having ultra-low density, high elasticity and processability can be produced very efficiently.

In addition, according to the method for producing a polyolefin elastomer copolymer of the present invention, it is possible to efficiently produce a polyolefin elastomer copolymer using an existing apparatus for producing an olefin homopolymer.

In addition, the polyolefin elastomer copolymer of the present invention provides low density, high elasticity, and excellent processability sufficient for use in automobile interior and exterior materials, shoes, cable coverings, and the like, and thus can be very usefully used throughout the industry.

1 is a conceptual diagram illustrating a conventional manufacturing apparatus (a) for an olefin homopolymer and a manufacturing apparatus (b) for manufacturing a polyolefin elastomer copolymer of the present invention;
2 is a graph showing the density of the polyolefin elastomer prepared in Example of the present invention,
3 is a graph showing the molecular weight distribution (Mn/Mw) of the polyolefin elastomer prepared in Examples of the present invention.

Hereinafter, the present invention will be described in detail.

Unless otherwise specified, all numbers, values, and/or expressions expressing quantities of ingredients, reaction conditions, polymer compositions and formulations used herein, contain all numbers, values and/or expressions in which such numbers essentially occur in obtaining such values, among others. Since they are approximations reflecting various uncertainties in the measurement, it should be understood as being modified by the term "about" in all cases. Also, when numerical ranges are disclosed in this description, such ranges are continuous and inclusive of all values from the minimum to the maximum inclusive of the range, unless otherwise indicated. Furthermore, when such ranges refer to integers, all integers inclusive from the minimum to the maximum inclusive are included, unless otherwise indicated.

In this specification, when a range is described for a variable, the variable will be understood to include all values within the stated range including the stated endpoints of the range. For example, a range of “5 to 10” includes the values of 5, 6, 7, 8, 9, and 10, as well as any subranges such as 6 to 10, 7 to 10, 6 to 9, 7 to 9, etc. It will be understood to include any value between integers that are appropriate for the scope of the recited range, such as 5.5, 6.5, 7.5, 5.5 to 8.5 and 6.5 to 9, and the like. Also for example, ranges from "10% to 30%" include values of 10%, 11%, 12%, 13%, etc. and all integers up to and including 30%, as well as 10% to 15%, 12% to It will be understood to include any subranges such as 18%, 20% to 30%, etc., as well as any value between reasonable integers within the scope of the recited ranges, such as 10.5%, 15.5%, 25.5%, and the like.

the present invention

(a) one kind of olefin monomer selected from 1-butene monomer, 1-hexene monomer and 1-octene monomer in a liquid state in a reactor; ethylene gas; and adding a Ziegler-Natta type catalyst supported on Ti; and

(b) performing a polymerization reaction at 50 ~ 70 ℃; relates to a method for producing a polyolefin elastomer copolymer comprising a.

The method for preparing the copolymer of the present invention is characterized by performing bulk polymerization using a liquid olefin monomer and a gaseous ethylene monomer instead of a solution polymerization method. The currently commercialized solution polymerization method has a limitation in enhancing stereoregularity because the solvent-soluble component remains in the resin, and additional production facilities such as a devolatilization device are required to remove the solvent. However, in the present invention, since no polymerization solvent is additionally used, a high-purity olefin-ethylene copolymer having a high degree of polymerization can be prepared.

Conventional techniques used expensive metallocene catalysts to copolymerize ethylene and olefin monomers, whereas in the present invention, inexpensive Ziegler-Natta catalysts are used to copolymerize ethylene and olefin polyolefins with a wider molecular weight distribution compared to metallocene catalysts. It has the characteristics of being able to manufacture an elastomer and providing a polyolefin elastomer with excellent processability.

In addition, a polyolefin elastomer copolymer having ultra-low density and high elasticity can be produced very efficiently.

The polyolefin elastomer copolymer prepared by the above method can manufacture polyolefin elastomers having various olefin contents, melt flowability (MFR), and melting point (Melting Temperature) of the resin by controlling operating conditions, It has the advantage of being able to satisfy all the physical properties required by various application products such as cables.

In the manufacturing method of the present invention, in the step (a), any one of ethylene gas or Ziegler-Natta type supported catalyst is first added, and the temperature of the reactor is raised to 50 ~ 70 ℃, and then the other one is added can do.

This input method is preferable in that it is possible to control the ethylene content in the polyolefin elastomer to be prepared.

In the present invention, the Ti-supported catalyst of the Ziegler-Natta type is added so that Ti is 0.5 to 3 micromoles (μmol) based on 1 mole of the olefin monomer; Ethylene gas may be supplied to maintain a partial pressure of 0.1 to 2.0 MPa during the reaction time, and more preferably, may be supplied to maintain a partial pressure of 0.2 to 1.0 MPa.

Since the content of Ti means the amount of Ti supported on the support of the Ziegler-Natta type catalyst, the amount of the Ziegler-Natta type catalyst used is determined according to the amount of Ti.

The Zieger-Natta type catalyst is a catalyst used in the olefin polymerization process, and may be formed by simultaneously including a titanium (Ti) active ingredient and a halogen ligand, a carrier, or a ligand and a carrier. As the Zieger-Natta type catalyst, specifically, a catalyst in which a titanium (Ti) active metal is supported on a support including magnesium (Mg) may be typically used. More specifically, the titanium (Ti) active metal may be a catalyst supported on a magnesium halide carrier.

When the Ziegler-Natta type Ti supported catalyst is included below the above range, the catalyst activity is low and the polymerization reaction is difficult to proceed efficiently. The cost increases, and after the reaction, the physical properties of the product are deteriorated by the Ti catalyst remaining in the product.

The ethylene gas is preferably supplied at 0.1 to 2.0 MPa during the reaction time. When the ethylene gas is supplied at a pressure of less than 0.1 MPa, the ethylene content in the produced polyolefin elastomer is insufficient to show the physical properties of the polyolefin elastomer, and becomes 2.0 MPa or more, and only ethylene is polymerized to copolymerize ethylene and olefin monomers Chain polyolefin elastomers cannot be produced.

In the manufacturing method of the present invention, 50 to 700 moles of an aluminum-based promoter and 1 to 100 moles of a silane-based promoter may be further added per mole of Ti content in step (a).

More preferably, 400 to 600 moles of an aluminum-based promoter and 10 to 50 moles of a silane-based promoter may be further added per mole of Ti content.

The aluminum-based co-catalyst serves as a polymerization co-catalyst to cause coordination polymerization with titanium (Ti) of the main catalyst, and to remove catalyst poison by reacting with molecular oxygen, which is an impurity contained in the monomer. The aluminum-based cocatalyst may be an aluminum compound in which two or more species selected from a halogen atom and a C1 to C10 alkyl group are bonded. The aluminum-based promoter is specifically diethylaluminum chloride (DEAC), ethylaluminum dichloride (EADC), dinormalbutylaluminum chloride (DNBAC), diisobutylaluminum chloride (DIBAC), triethylaluminum (TEA), triethylaluminum (TEA), At least one selected from the group consisting of isobutylaluminum (TIBA), trinormalhexylaluminum (TNHA), trinormaloctylaluminum (TNOA), and trinormaldecylaluminum (TNDA) may be used, but the present invention is not limited thereto it is not

The aluminum-based promoter may be used in the range of 50 to 700 moles, more preferably in the range of 400 to 600 moles, based on 1 mole of Ti of the main catalyst. When the content of the aluminum-based cocatalyst is less than 50 mol, aluminum cannot play a role as a cocatalyst participating in coordination polymerization and a role for removing catalyst poison, so that the conversion rate of the raw material is lowered. On the other hand, when the content of the aluminum-based cocatalyst exceeds 700 mol, the effect of the addition according to the increase in the amount used is insignificant, so it is inefficient.

The silane-based cocatalyst serves to increase the stereoregularity of the copolymer. The silane-based cocatalyst may be one or more selected from mono-, di- or trialkoxysilane compounds to which heterogeneous species selected from a C1 to C10 alkyl group, a C1 to C10 alkoxy group, and a C6 to C12 aryl group are bonded. The silane-based promoter is specifically selected from diphenyldimethoxysilane, phenyltrimethoxysilane, isobutylmethoxysilane, diisobutyldimethoxysilane, cyclohexylmethyldimethoxysilane, diisopropyldimethoxysilane, and the like. One or more may be used, but the present invention is not limited thereto.

The silane-based cocatalyst may be used in the range of 1 to 100 moles, more preferably in the range of 10 to 30 moles, based on 1 mole of Ti of the main catalyst. When the content of the silane-based cocatalyst is less than 1 mol, the stereoregularity is lowered and the degree of crystallinity is lowered, thereby reducing mechanical properties. On the other hand, if it exceeds 100 moles, the effect of addition according to the increase in the amount of use is insignificant, so it is inefficient.

In addition, in constituting the catalyst system of the present invention, the conversion rate, stereoregularity, and molecular weight of the synthesized copolymer may be changed by the content ratio of the aluminum-based promoter and the silane-based promoter. Preferably, as a promoter, the molar ratio of the aluminum-based promoter and the silane-based promoter is preferably 10 to 30: 1, more preferably 20 to 30: 1. When the molar ratio is less than 10:1, the stereoregularity is increased, but the concentration of the aluminum-based cocatalyst is low, so that the coordination polymerization conversion rate is lowered, and it may be inefficient in removing the catalyst poison. On the other hand, if the molar ratio exceeds 30:1, the Ti active site is sufficiently activated and the catalyst activity is excellently maintained due to the removal of the catalyst poison, but it is difficult to obtain a copolymer having excellent stereoregularity of the polymer and low A polymer of molecular weight is produced and stickiness occurs.

In the production method of the present invention, in step (a), 1 to 200 mmol of hydrogen per 1 mole of the olefin monomer may be further added, more preferably 50 to 200 mmol of hydrogen per 1 mole of the olefin monomer, even more preferably 100 ~200 mmol may be further added.

The hydrogen is used as a molecular weight regulator. When the hydrogen content is less than 1 mmol, the copolymerization reaction between ethylene and the olefin monomer does not start, which may cause a problem that the polymerization rate is significantly lowered. As a result, a problem in which desired physical properties cannot be obtained may occur.

In the production method of the present invention, the polymerization reaction in step (b) is preferably performed for 0.5 to 3 hours. If the reaction time is shorter than 0.5 hours, the polymerization degree is low and a desired molecular weight may not be obtained. Not desirable.

In the manufacturing method of the present invention, an inert gas may be further supplied during the reaction time together with the supply of hydrogen.

Specifically, by introducing an inert gas together with hydrogen, the reaction pressure can be adjusted in the range of 5 to 50 bar. Maintaining a high reaction pressure exceeding 50 bar is not preferable because it is inefficient compared to facility investment.

By adding an inert gas together with hydrogen as described above and applying a pressure higher than the gas-liquid equilibrium pressure at the polymerization temperature, the activity of the polymerization reaction can be significantly increased. The inert gas does not affect the polymerization reaction Any gas may be used, and specifically, at least one selected from the group consisting of nitrogen, helium and argon may be used as the inert gas.

In the manufacturing method of the present invention, as shown in FIG. 1, the method connects an ethylene gas supply unit equipped with an opening/closing device to the reactor of the conventional olefin homopolymer manufacturing apparatus (FIG. 1 (a)) (FIG. 1) of (b)) can be performed.

Therefore, in the manufacturing method of the present invention, there is no need for a separate polymerization device, and the ethylene gas supply unit equipped with an opening/closing device is connected to the reactor of the conventional olefin homopolymer manufacturing device (FIG. 1 (a)) ((FIG. 1) b)) One apparatus can be used to carry out the preparation of the polybutylene elastomer copolymer.

In addition, when the switchgear of the ethylene gas supply unit provided with the switchgear is locked, the device can be efficiently used because a polymer such as an olefin homopolymer can be produced by an existing device.

Also, the present invention

It relates to an ethylene and olefin copolymer polyolefin elastomer copolymer prepared by the above method.

Since the polyolefin elastomer copolymer has low density, high elasticity and excellent processability, it can be very usefully used throughout the industry. In particular, it can be usefully used for automotive interior and exterior materials, shoes, or cable coverings.

Hereinafter, preferred examples are presented to help the understanding of the present invention, but the following examples are merely illustrative of the present invention, and it will be apparent to those skilled in the art that various changes and modifications are possible within the scope and spirit of the present invention, It goes without saying that such changes and modifications fall within the scope of the appended claims.

[Example]

Example 1: Preparation of polyolefin elastomer copolymer

The 1.5L volume stainless autoclave was sufficiently purged with nitrogen to remove oxygen and moisture that may affect the catalyst poison. As a reactant, 700 ml of liquid 1-butene was added to the reactor.

As a catalyst system, (A) a Ziegler-Natta type main catalyst using a catalyst in which a titanium (Ti) active metal is supported on a magnesium chloride (MgCl ₂ ) carrier, and (B) triethylaluminum (AlCl ₃ ) as an aluminum-based cocatalyst ) and (C) diisopropylmethoxysilane was used as a silane-based cocatalyst. Specifically, in the content of the catalyst, the main catalyst is quantified so that Ti supported on the magnesium chloride (MgCl ₂ ) carrier is 2 micromoles (μmol) based on 1 mole of the 1-butene monomer (14 mg is used) and hexane It was prepared by diluting to 1 wt%. Based on 1 mole of Ti content in the main catalyst, 60 mg of triethylaluminum and 2 mg of diisomethoxysilane were prepared so that 500 moles of an aluminum-based promoter and 20 moles of a silane-based promoter were obtained. Thus, the molar ratio of the aluminum-based promoter/silane-based promoter was quantified as 25 and prepared.

The prepared aluminum-based cocatalyst was dispersed in hexane at 5 wt%, and the silane-based cocatalyst was dispersed in hexane at 2 wt% and added to the autoclave reactor together with 1-butene monomer.

After adding 1-butene, an aluminum-based promoter, and a silane-based promoter, 20 mmol of hydrogen per mole of 1-butene was added. Then, ethylene gas was introduced until the pressure of the reactor reached 1.8 MPa.

The reactant was stirred for about 5 minutes at a speed of 150 rpm at room temperature using a mechanical stirrer, and the temperature inside the reactor was raised from room temperature to 60°C.

Then, the main catalyst prepared above was introduced into the reactor. The polymerization reaction was carried out at a polymerization temperature of 60° C. for 51 minutes while pressurized to a reactor internal pressure of 1.7 MPa. After the polymerization is completed, 10 ml of ethanol is added, the reaction is stopped by stirring for 5 minutes, unreacted ethylene and 1-butene are removed, and the polyolefin elastomer that has been polymerized is recovered from the autoclave and vacuum dried at 70° C. for 2 hours to 405 g of polybutylene elastomer copolymer was obtained.

Examples 2 and 3: Preparation of polyolefin elastomer copolymers

The 1.5L volume stainless autoclave was sufficiently purged with nitrogen to remove oxygen and moisture that may affect the catalyst poison. As a reactant, 700 ml of liquid 1-butene was added to the reactor.

As a catalyst system, (A) a Ziegler-Natta type main catalyst using a catalyst in which a titanium (Ti) active metal is supported on a magnesium chloride (MgCl ₂ ) carrier, and (B) triethylaluminum (AlCl ₃ ) as an aluminum-based cocatalyst ) and (C) diisopropylmethoxysilane was used as a silane-based cocatalyst. Specifically, as for the content of the catalyst, the main catalyst is quantified so that the Ti supported on the magnesium chloride (MgCl ₂ ) carrier is 2.0 micromoles (μmol) based on 1 mol of the 1-butene monomer (14 mg is used) and hexane It was prepared by diluting it to 1w%. Based on 1 mole of Ti content in the main catalyst, 60 mg of triethylaluminum and 2 mg of diisomethoxysilane were prepared so that 500 moles of an aluminum-based promoter and 20 moles of a silane-based promoter were obtained. Thus, the molar ratio of the aluminum-based promoter/silane-based promoter was quantified as 25 and prepared.

The prepared aluminum-based cocatalyst was dispersed in hexane at 5 wt%, and the silane-based cocatalyst was dispersed in hexane at 2 wt% and added to the autoclave reactor together with 1-butene monomer.

After adding 1-butene, an aluminum-based promoter, and a silane-based promoter, 150 mmol of hydrogen per mole of 1-butene was added, and then, the main catalyst prepared above was introduced into the reactor. The reactant was stirred for about 5 minutes at a speed of 150 rpm at room temperature using a mechanical stirrer, and the temperature inside the reactor was raised from room temperature to 60°C. After the internal temperature reached 60° C., ethylene gas was additionally supplied during the polymerization reaction so that the reactor internal pressure was maintained at 1.8 MPa. Polymerization was carried out at a polymerization temperature of 60° C. for 35 minutes. After the polymerization is completed, 10 ml of ethanol is added, the reaction is stopped by stirring for 5 minutes, unreacted ethylene and 1-butene are removed, and the polyolefin elastomer that has been polymerized is recovered from the autoclave and vacuum dried at 70° C. for 2 hours to 237 g of polyolefin elastomer copolymer was obtained.

The polyolefin elastomer copolymer of Example 3 was prepared in the same manner as in Example 2, except that the amount of hydrogen, the amount of nitrogen, and the reaction time were changed under the conditions shown in Table 1 below.

H ₂
[mmol] Cat.
[mg] Polymn.
time
[min] Yield
[g] Example 2 150 14 35 237 Example 3 150 14 57 300

Test Example: Evaluation of the physical properties of the copolymer

The polymers prepared in Examples 1 to 3 and Engrade7467, which is a commercially available polyolefin elastomer from DOW, were measured for physical properties by the following evaluation method, and the results are shown in Table 2 below.

<Method for evaluating physical properties of polymers>

(1) Activity (kg polymer/g catalyst.hour): Amount of polyolefin elastomer produced per unit catalyst and reaction time

Amount of polymer produced / (Amount of catalyst used X reaction time)

(2) MFR: melt flow index: ASTM D1238

(3) Density: ASTM D1505

(4) Number average molecular weight (Mn) and molecular weight distribution (Mw/Mn): measured by GPC

(5) C4 content (C4 content): measured by C ¹³ NMR

(6) Melting Temperature: Measured by DSC (Differential Scanning Calorimeter)

Activity
[kg/g h] MFR
[g/10min] Density
[g/cm ³ ]
GPC C4 content
(C ¹³ NMR)
[mol%] Melting Temperature
[℃]
(216N,
190℃) (2.16N,
190℃) Mn
[kg/mol] molecular weight distribution
(Mw/Mn) Example 1 34.0 - - 0.81 212.4 5.0 13.3 118.9 Example 2 29.0 - 8.1 0.83 44.9 4.3 83.0 36.0 Example 3 22.6 - 0.9 0.82 27.4 7.2 27.1 41.2 ENGRADE 7467 - 1.3 0.86 55.9 2.2 21.7 39.2

As can be seen in Table 2 above, the 1-butene content of the polyolefin elastomers prepared in Examples 1 to 3 of the present invention can be adjusted to various contents depending on the operating conditions. Also, as shown in FIG. 2, It is possible to manufacture a polyolefin elastomer with a low density compared to commercially available products, thereby providing a final product having excellent elasticity. In addition, as shown in FIG. 3 , it is possible to prepare a polyolefin elastomer having a molecular weight distribution (Mn/Mw) more than twice that of a commercial product prepared with a metallocene catalyst, thereby providing excellent processability.

Claims (10)

(a) one olefin monomer selected from 1-butene monomer, 1-hexene monomer and 1-octene monomer in a liquid state in a reactor; ethylene gas; and adding a Ziegler-Natta type catalyst supported on Ti; and
(b) performing a polymerization reaction at 50 ~ 70 ℃; Method for producing a polyolefin elastomer copolymer comprising a. According to claim 1,
Polyolefin elastomer aerial, characterized in that in step (a), either ethylene gas or Ziegler-Natta type supported catalyst is first added, the temperature of the reactor is raised to 50 ~ 70°C, and the other one is added A method for producing a composite. According to claim 1,
The Ziegler-Natta type supported catalyst is added so that Ti is 0.5 to 3.0 micromoles (μmol) based on 1 mole of the olefin monomer; A method for producing a polyolefin elastomer copolymer, characterized in that ethylene gas is supplied at 0.1 to 2.0 MPa during the reaction time. 4. The method of claim 3,
A method for producing a polyolefin elastomer copolymer, characterized in that 50 to 700 moles of an aluminum-based promoter and 1 to 100 moles of a silane-based promoter are further added per mole of the Ti content in step (a). 5. The method of claim 4,
A method for producing a polyolefin elastomer copolymer, characterized in that 1 to 200 mmol of hydrogen is further added per 1 mole of the olefin monomer in step (a). 5. The method of claim 4,
The method for producing a polyolefin elastomer copolymer, characterized in that the aluminum-based promoter and the silane-based promoter have a molar ratio of 10 to 30: 1. According to claim 1,
The polymerization reaction of step (b) is a method for producing a polyolefin elastomer copolymer, characterized in that it is carried out for 0.5 to 3 hours. According to claim 1,
The method is a method for producing a polyolefin elastomer copolymer, characterized in that it is carried out by connecting an ethylene gas supply unit equipped with an opening/closing device to the reactor of the olefin homopolymer production apparatus. A polyolefin elastomer copolymer prepared by the method of claim 1. 10. The method of claim 9,
The polyolefin elastomer copolymer is a polyolefin elastomer copolymer, characterized in that it is for automotive interior and exterior materials, shoes, or cable coverings.

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