Method for reducing activity of catalyst in polypropylene horizontal reactor

Abstract

The invention relates to a method for reducing the activity of a catalyst in a polypropylene horizontal reactor, and belongs to the technical field of polypropylene production. The method comprises the following steps: operating a polypropylene horizontal reaction system to carry out a polymerization reaction for preparing polypropylene, wherein the polymerization reaction is catalyzed by a catalyst composition; and when the polymerization reaction is carried out, an active inhibitor is introduced into the first reaction zone of the first horizontal reactor. When the polypropylene material is produced, the trace activity inhibitor is introduced into the first reaction zone of the first horizontal reactor, so that the activity of the catalyst in the first reaction zone of the first horizontal reactor can be effectively reduced; the generation of lump materials caused by too violent polymerization reaction (namely the initial stage of reaction for producing polypropylene) in the first reaction zone is prevented.

Description

Technical Field

[0001] The present invention relates to the technical field of polypropylene production, and particularly relates to a method for reducing the activity of a catalyst in a horizontal polypropylene reactor. Background Art

[0002] Most existing polypropylene materials adopt a gas-phase production process, and its supporting process system is provided with two gas-phase reactors, namely a first horizontal reactor and a second horizontal reactor. Four reaction zones are respectively arranged in each reactor. During the production of polypropylene, the main catalyst, cocatalyst, and modifier enter from the first reaction zone of the first horizontal reactor and are discharged from the fourth reaction zone of the second horizontal reactor to the downstream section. The whole process is close to plug flow. When producing special polypropylene products (such as polypropylene-3) by this process, the initial reaction activity of the catalyst in the first reaction zone of the first horizontal reactor is relatively high, which may lead to too high local hot spots in the polymerization reaction, causing the polymer to agglomerate and affecting the stability of production.

[0003] Currently, there are mainly three methods for controlling the activity of the polymerization reaction: (1) reducing the reaction load; (2) adjusting the reaction temperature and pressure; (3) changing the concentration and ratio of the catalyst. The above methods are all overall adjustments of the polymerization reaction activity in the whole reactor and cannot effectively reduce the activity of the catalyst, resulting in the generation of agglomerates in some areas of the reactor. Especially in the gap between the stirring shaft and the side wall in the first horizontal reactor, there may be some materials with blocked flow continuously reacting, and finally, due to the too high activity of the catalyst, agglomerates are quickly generated.

[0004] Therefore, it is very necessary to develop a method that can effectively reduce the activity of the catalyst in the horizontal polypropylene reactor. Summary of the Invention

[0005] The purpose of the present invention is to provide a method for reducing the activity of a catalyst in a horizontal polypropylene reactor by overcoming the deficiencies of the prior art.

[0006] To achieve the above purpose, the technical solution adopted by the present invention is as follows:

[0007] A method for reducing the activity of a catalyst in a horizontal polypropylene reactor, comprising the following steps:

[0008] Operate a horizontal polypropylene reaction system to carry out a polymerization reaction for preparing polypropylene, and the polymerization reaction is catalyzed by a catalyst composition;

[0009] When carrying out the polymerization reaction, introduce an activity inhibitor into the first reaction zone of the first horizontal reactor.

[0010] When the present invention produces polypropylene materials, by introducing a trace amount of active inhibitor into the first reaction zone of the first horizontal reactor, the activity of the catalyst in the first reaction zone of the first horizontal reactor can be effectively controlled, preventing the polymerization reaction occurring in the first reaction zone (i.e., the initial stage of the reaction for producing polypropylene) from being too intense and causing the rapid formation of lumps.

[0011] As a preferred embodiment of the present invention, the active inhibitor is compressed air.

[0012] The inventors have found through research that when using compressed air as the active inhibitor, it can be quickly and evenly distributed in the first horizontal polypropylene reactor, reaching every corner of the first reaction zone of the first horizontal reactor, which is beneficial to achieving precise and comprehensive control of the catalyst activity in the first reaction zone and effectively reducing the risk of caking during the production process.

[0013] As a preferred embodiment of the present invention, when carrying out the polymerization reaction, the active inhibitor is introduced into the first reaction zone of the first horizontal reactor at a flow rate not exceeding 500 NL / h.

[0014] Compared with the prior art, the present invention can effectively reduce the activity of the catalyst in the first reaction zone of the first horizontal reactor by controlling the flow rate of the introduced active inhibitor. The operation difficulty is small, and the amount of the introduced active inhibitor is small, without introducing impurities. The inventors have found through research that the flow rate of the active inhibitor should not exceed 500 NL / h to avoid too low activity of the catalyst in the initial stage of the reaction (corresponding to the first reaction zone of the first horizontal reactor) and affecting the production efficiency of polypropylene materials.

[0015] As a preferred embodiment of the present invention, when carrying out the polymerization reaction, the active inhibitor is introduced into the first reaction zone of the first horizontal reactor from at least one of the first recycle gas inlet and the non-drive end shaft seal.

[0016] Furthermore, when carrying out the polymerization reaction, the active inhibitor is introduced into the first reaction zone of the first horizontal reactor from the first recycle gas inlet at a flow rate of 20 - 180 NL / h.

[0017] Furthermore, when carrying out the polymerization reaction, the active inhibitor is introduced into the first reaction zone of the first horizontal reactor from the non-drive end shaft seal of the first reaction zone at a flow rate of 5 - 60 NL / h.

[0018] The inventors have found through research that in the first reaction zone of the first horizontal reactor, by introducing compressed air through the non-drive end shaft seal and the first recycle gas inlet of this first reaction zone, the activity of the catalyst in a local area (such as the gap between the stirring blades and the side wall of the stirring mechanism in the first reaction zone) is reduced or deactivated, avoiding caking phenomena in the local area.

[0019] The inventors' research found that when carrying out the polymerization reaction, introducing the activity inhibitor into the first reaction zone of the first horizontal reactor at a flow rate of 20 - 180 NL / h from the first recycle gas inlet, and introducing the activity inhibitor into the first reaction zone of the first horizontal reactor at a flow rate of 5 - 60 NL / h from the non-driven end shaft seal of the first reaction zone can effectively inhibit the activity of the catalyst and greatly reduce the production amount of lumps. When the flow rate of the activity inhibitor introduced from the first recycle gas inlet is 40 - 60 N / h, and when the flow rate of the activity inhibitor introduced from the non-driven end shaft seal is 20 - 30 N / h, it can significantly reduce the production amount of lumps while maintaining a relatively high catalyst activity.

[0020] As a preferred embodiment of the present invention, when carrying out the polymerization reaction, introducing the activity inhibitor into the first reaction zone of the second horizontal reactor at a flow rate of 100 - 200 NL / h.

[0021] As a preferred embodiment of the present invention, the catalyst composition includes a BCM-type catalyst, a modifier, and a cocatalyst. The molar ratio of the cocatalyst to the BCM-type catalyst is (3 - 6):1, and the molar ratio of the cocatalyst to the modifier is (1 - 2):1.

[0022] Furthermore, the BCM-type catalyst includes at least one of catalyst BCM-100, catalyst BCM-100H, catalyst BCM-200, catalyst BCM-300, catalyst BCM-400, and catalyst BCM-500; the modifier is diisobutyl dimethoxysilane; the cocatalyst is triethylaluminum.

[0023] As a preferred embodiment of the present invention, when carrying out the polymerization reaction, inputting the catalyst composition into the first reaction zone of the first horizontal polypropylene reaction zone, and the flow rate of the BCM-type catalyst in the catalyst composition is 15 - 40 Kg / h.

[0024] As a preferred embodiment of the present invention, in the first horizontal reactor, continuously introducing propylene and the catalyst composition, the flow rate of the introduced propylene is 200 - 250 m 3 / h, and carrying out the polymerization reaction under the conditions of a polymerization temperature of 65 - 80 °C and a polymerization pressure of 2 - 3 MPa. The intermediate polymer flows out from the bottom of the fourth reaction zone of the first horizontal reactor;

[0025] In the second horizontal reactor, continuously introducing propylene and the intermediate polymer, the flow rate of the introduced intermediate polymer is 9 - 13 t / h, and the flow rate of the introduced propylene is 140 - 180 m 3 / h, the polymerization reaction is carried out under the conditions of a polymerization temperature of 60 to 70 °C and a polymerization pressure of 2 to 3 MPa, and the polypropylene product flows out from the bottom of the fourth reaction zone of the second horizontal reactor.

[0026] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0027] When producing the polypropylene material, the present invention can effectively control the activity of the catalyst in the first reaction zone of the first horizontal reactor by introducing a trace amount of active inhibitor into the first reaction zone of the first horizontal reactor, and prevent the polymerization reaction occurring in the first reaction zone (i.e., the initial stage of the reaction for producing polypropylene) from being too violent and causing the generation of lumps. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 It is a schematic structural diagram of the polypropylene horizontal reaction system provided by the present invention. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0029] To better illustrate the purpose, technical solution and advantages of the present invention, the present invention will be further described below in conjunction with specific embodiments.

[0030] The materials, reagents, etc. used in the embodiments can be obtained from commercial channels without special instructions.

[0031] Example 1

[0032] This example provides a polypropylene horizontal reaction system, the structure of which is as Figure 1 shown.

[0033] The polypropylene horizontal reaction system includes two serially connected first horizontal reactors 1 and second horizontal reactors 2, and also includes a first propylene tank 3 and a second propylene tank 4. A first reaction zone, a second reaction zone, a third reaction zone and a fourth reaction zone are sequentially connected in both the first horizontal reactor 1 and the second horizontal reactor 2.

[0034] The first reaction zone of the first horizontal reactor 1 is provided with a first recycle gas inlet 11 and a first recycle gas outlet 12. The first recycle gas inlet 11 is connected to the outlet of the first propylene tank 3 through a pipeline, and the first recycle gas outlet 12 is connected to the inlet of the first propylene tank 3 through a pipeline. The first recycle gas inlet 11 is also connected to a compressed air supply pipeline; the first horizontal reactor 1 is equipped with a first stirring mechanism, and the non-driving end shaft 13 of the first stirring mechanism is sealed on the side wall of the first reaction zone. The non-driving end shaft seal 13 is a hollow structure and is communicated with the first reaction zone 11; the first reaction zone of the first horizontal reactor 1 is also provided with a catalyst inlet ( Figure 1 not shown);

[0035] Control valves and flow meters are provided on each pipeline ( Figure 1 not shown);

[0036] The first reaction zone of the second horizontal reactor 2 is provided with a second recycle gas inlet 21 and a second recycle gas outlet 22. The second recycle gas inlet 21 is connected to the outlet of the second propylene tank 4 through a pipeline, and the second recycle gas outlet 22 is connected to the inlet of the second propylene tank 4 through a pipeline. The second recycle gas inlet 21 is also connected with a compressed air supply pipeline; the second horizontal reactor 2 is equipped with a second stirring mechanism.

[0037] Example 2

[0038] This example provides a method for reducing the activity of the catalyst in a polypropylene horizontal reactor, which is implemented through the polypropylene horizontal reaction system provided in Example 1. The method includes the following steps:

[0039] In the first horizontal reactor 1, a complex of modifier diisobutyl dimethoxysilane and cocatalyst triethylaluminum, propylene, and catalyst BCM-100 are continuously introduced. When continuously introduced, the flow rate of propylene is 220 m 3 / h, the flow rate of catalyst BCM-100H is 25 Kg / h, the molar ratio of the cocatalyst to catalyst BCM-100 is 4.5:1, and the molar ratio of the cocatalyst to the modifier is 1.7:1; the polymerization reaction is carried out under the conditions of a polymerization temperature of 70 °C and a polymerization pressure of 2.45 MPa. The intermediate polymer flows out from the bottom of the fourth reaction zone of the first horizontal reactor 1; while the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 20 NL / h, and compressed air is continuously introduced into the first horizontal reactor 1 from the non-driven end shaft 13 at a flow rate of 10 NL / h;

[0040] In the second horizontal reactor 2, propylene and the intermediate polymer are continuously introduced. The flow rate of the intermediate polymer is 11 t / h, and the flow rate of the propylene is 160 m 3 / h. The polymerization reaction is carried out under the conditions of a polymerization temperature of 70 °C and a polymerization pressure of 2.45 MPa. The polypropylene product flows out from the bottom of the fourth reaction zone of the second horizontal reactor 2; while the polymerization reaction is carried out in the second horizontal reactor 2, compressed air is continuously introduced into the second horizontal reactor 2 from the second recycle gas inlet 21 at a flow rate of 150 NL / h.

[0041] Examples 3-8 and Comparative Example 1

[0042] Examples 3-8 and Comparative Example 1 respectively provide a method for reducing the activity of the catalyst in a polypropylene horizontal reactor. The differences between Examples 3-8 and Comparative Example 1 and Example 2 are as follows:

[0043] Example 3 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 40 NL / h;

[0044] Example 4 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 60 NL / h;

[0045] Example 5 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 90 NL / h;

[0046] Example 6 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 120 NL / h;

[0047] Example 7 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 150 NL / h;

[0048] Example 8 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 180 NL / h;

[0049] Comparative Example 1 When the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is not introduced from the first recycle gas inlet 11.

[0050] Examples 9 - 13 and Comparative Example 2

[0051] Examples 9 - 13 and Comparative Example 2 respectively provide a method for reducing the catalyst activity in a polypropylene horizontal reactor. The differences between Examples 9 - 13 and Comparative Example 2 and Example 3 are as follows:

[0052] Example 9 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the non - drive end shaft 13 at a flow rate of 5 NL / h;

[0053] Example 10 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the non - drive end shaft 13 at a flow rate of 20 NL / h;

[0054] Example 11 While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the non - drive end shaft 13 at a flow rate of 30 NL / h;

[0055] Example 12 While carrying out the polymerization reaction in the first horizontal reactor 1, compressed air was continuously introduced into the first horizontal reactor 1 from the non-driving end shaft 13 at a flow rate of 40 NL / h.

[0056] Example 13 While carrying out the polymerization reaction in the first horizontal reactor 1, compressed air was continuously introduced into the first horizontal reactor 1 from the non-driving end shaft 13 at a flow rate of 60 NL / h.

[0057] Comparative Example 2 When carrying out the polymerization reaction in the first horizontal reactor 1, compressed air was not introduced from the non-driving end shaft 13.

[0058] Example 14

[0059] This example provides a method for reducing the activity of the catalyst in a polypropylene horizontal reactor, which is implemented through the polypropylene horizontal reaction system provided in Example 1. The method includes the following steps:

[0060] In the first horizontal reactor 1, a complex of the modifier diisobutyl dimethoxysilane and the cocatalyst triethylaluminum, propylene, and the catalyst BCM-100 were continuously introduced. When continuously introducing, the flow rate of propylene was 200 m 3 / h, the flow rate of the catalyst BCM-100H was 15 Kg / h, the molar ratio of the cocatalyst to the catalyst BCM-100 was 3:1, and the molar ratio of the cocatalyst to the modifier was 1:1. The polymerization reaction was carried out under the conditions of a polymerization temperature of 65 °C and a polymerization pressure of 2 MPa. The intermediate polymer flowed out from the bottom of the fourth reaction zone of the first horizontal reactor 1. While carrying out the polymerization reaction in the first horizontal reactor 1, compressed air was continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 40 NL / h, and compressed air was continuously introduced into the first horizontal reactor 1 from the non-driving end shaft 13 at a flow rate of 20 NL / h.

[0061] In the second horizontal reactor 2, propylene and the intermediate polymer were continuously introduced. The flow rate of the intermediate polymer was 9 t / h, and the flow rate of the propylene was 140 m 3 / h. The polymerization reaction was carried out under the conditions of a polymerization temperature of 60 °C and a polymerization pressure of 2 MPa. The polypropylene product flowed out from the bottom of the fourth reaction zone of the second horizontal reactor 2. While carrying out the polymerization reaction in the second horizontal reactor 2, compressed air was continuously introduced into the second horizontal reactor 2 from the second recycle gas inlet 21 at a flow rate of 100 NL / h.

[0062] Example 15

[0063] This example provides a method for reducing the activity of the catalyst in a polypropylene horizontal reactor, which is implemented through the polypropylene horizontal reaction system provided in Example 1. The method includes the following steps:

[0064] In the first horizontal reactor 1, a compound of modifier diisobutyl dimethoxysilane and cocatalyst triethylaluminum, propylene, and catalyst BCM-100 are continuously introduced. When continuously introduced, the flow rate of propylene is 250 m 3 / h, the flow rate of catalyst BCM-100H is 40 Kg / h, the molar ratio of the cocatalyst to catalyst BCM-100 is 6:1, and the molar ratio of the cocatalyst to the modifier is 2:1. The polymerization reaction is carried out under the conditions of a polymerization temperature of 80 °C and a polymerization pressure of 3 MPa. The intermediate polymer flows out from the bottom of the fourth reaction zone of the first horizontal reactor 1. While the polymerization reaction is carried out in the first horizontal reactor 1, compressed air is continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 at a flow rate of 40 NL / h, and compressed air is continuously introduced into the first horizontal reactor 1 from the non-drive end shaft 13 at a flow rate of 20 NL / h;

[0065] In the second horizontal reactor 2, propylene and the intermediate polymer are continuously introduced. The flow rate of the intermediate polymer is 13 t / h, and the flow rate of the propylene is 180 m 3 / h. The polymerization reaction is carried out under the conditions of a polymerization temperature of 70 °C and a polymerization pressure of 3 MPa. The polypropylene product flows out from the bottom of the fourth reaction zone of the second horizontal reactor 2. While the polymerization reaction is carried out in the second horizontal reactor 2, compressed air is continuously introduced into the second horizontal reactor 2 from the second recycle gas inlet 21 at a flow rate of 200 NL / h.

[0066] Effect Example 1

[0067] During the implementation process of the above examples and comparative examples, the amount of polypropylene that can be produced by 1 kg of catalyst through the polymerization reaction is statistically calculated to evaluate the catalyst activity (unit: kg(pp) / kg(cat), where pp refers to polypropylene and cat refers to the catalyst), and the current production situation (i.e., the frequency of lumps appearing in the polypropylene product output from the system, and the normal polypropylene product is in a viscous flow state) is statistically calculated. The results are shown in Table 1 below.

[0068] Table 1

[0069]

[0070] As can be seen from Examples 2 to 8 and Comparative Example 1, no compressed air was introduced in Comparative Example 1, and the catalyst activity was too high, which promoted the rapid formation of lumps. The frequency of lumps in the product output by the system was too high, reaching 8 times / h. In the present invention, the flow rate of the compressed air continuously introduced into the first horizontal reactor 1 from the first recycle gas inlet 11 should be controlled within an appropriate range to reduce the amount of lumps generated while maintaining a relatively high catalytic activity. When the flow rate of the activity inhibitor introduced from the first recycle gas inlet is controlled within the range of 40 - 60 N / h in the present invention, a relatively high catalyst activity can be maintained, the catalyst activity is higher than 25000 kg(pp) / kg(cat), and the amount of lumps generated can be significantly reduced, so that the frequency of lumps in the product output by the system is reduced to 1 time / h.

[0071] As can be seen from Example 2, Examples 9 to 13 and Comparative Example 2, no compressed air was introduced into the first horizontal reactor 1 from the non-driving end shaft 13 in Comparative Example 2, resulting in a frequency of lumps as high as 8 times / h in the product output by the system. Moreover, through observation, lumps were found in the gap between the stirring blades and the side wall of the reactor. In the present invention, the flow rate of the compressed air continuously introduced into the first horizontal reactor 1 from the non-driving end shaft 13 should be controlled within an appropriate range to reduce the amount of lumps generated while maintaining a relatively high catalytic activity. When the flow rate of the activity inhibitor introduced from the non-driving end shaft seal is controlled within the range of 20 - 30 N / h in the present invention, a relatively high catalyst activity can be maintained, the catalyst activity is higher than 25000 kg(pp) / kg(cat), and the amount of lumps generated can be significantly reduced, so that the frequency of lumps in the product output by the system is reduced to 1 time / h.

[0072] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention rather than to limit the protection scope of the present invention. Although the present invention has been described in detail with reference to the preferred embodiments, those of ordinary skill in the art should understand that the technical solutions of the present invention can be modified or equivalently replaced without departing from the essence and scope of the technical solutions of the present invention.

Claims

1. A method for reducing the activity of a catalyst in a horizontal polypropylene reactor, characterized in that, it comprises the following steps: Operate a horizontal polypropylene reaction system to carry out a polymerization reaction for preparing polypropylene, and the polymerization reaction is catalyzed by a catalyst composition; When carrying out the polymerization reaction, introduce an activity inhibitor into the first reaction zone of the first horizontal reactor.

2. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 1, characterized in that, the activity inhibitor is compressed air.

3. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 1, characterized in that, When carrying out the polymerization reaction, introduce the activity inhibitor into the first reaction zone of the first horizontal reactor at a flow rate not greater than 500 NL / h.

4. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 1, characterized in that, When carrying out the polymerization reaction, introduce the activity inhibitor into the first reaction zone of the first horizontal reactor from at least one of the recycle gas inlet of the first reaction zone and the non-driven end shaft seal of the first reaction zone.

5. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 4, characterized in that, When carrying out the polymerization reaction, introduce the activity inhibitor into the first reaction zone of the first horizontal reactor from the recycle gas inlet of the first reaction zone at a flow rate of 20 - 180 NL / h.

6. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 4, characterized in that, When carrying out the polymerization reaction, introduce the activity inhibitor into the first reaction zone of the first horizontal reactor from the non-driven end shaft seal of the first reaction zone at a flow rate of 5 - 60 NL / h.

7. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 1, characterized in that, the catalyst composition includes a BCM type catalyst, a modifier and a cocatalyst, the molar ratio of the cocatalyst to the BCM type catalyst is (3 - 6):1, and the molar ratio of the cocatalyst to the modifier is (1 - 2):

1.

8. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 7, characterized in that, the BCM type catalyst includes at least one of catalyst BCM-100, catalyst BCM-100H, catalyst BCM-200, catalyst BCM-300, catalyst BCM-400 and catalyst BCM-500; the modifier is diisobutyl dimethoxysilane; the cocatalyst is triethylaluminum.

9. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 1, characterized in that, When carrying out the polymerization reaction, input the catalyst composition into the first reaction zone of the first horizontal polypropylene reaction zone, and the flow rate of the BCM type catalyst in the catalyst composition is 15 - 40 Kg / h.

10. The method for reducing the activity of a catalyst in a horizontal polypropylene reactor according to claim 1, characterized in that, When carrying out the polymerization reaction, an active inhibitor is introduced into the first reaction zone of the second horizontal reactor at a flow rate of 100 to 200 NL / h.

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