阅读说明：本技术 一种催化剂的配制方法及其应用 (Preparation method and application of catalyst ) 是由 孙延举 王晓东 包满 冯超 乔丙臣 曹雷 李红卫 于 2020-05-21 设计创作，主要内容包括：本发明涉及催化剂制备领域,公开了一种聚丙烯生产中使用的催化剂的配制方法。该方法包括以下步骤：1)在主催化剂贮存单元使主催化剂与凡士林油进行第一接触后,得到第一混合物,并将第一混合物送入至主催化剂配制单元；2)将凡士林脂从凡士林脂贮存单元通过凡士林脂输料单元输送至主催化剂配制单元；3)将第一混合物和凡士林脂在主催化剂配制单元内进行第二接触,得到第二混合物；4)将第二混合物送入至催化剂预接触单元后,与助催化剂进行第三接触,得到催化剂。使用该方法可以解决固态催化剂投料时附着在容器上的问题,不仅减少催化剂的浪费,而且不会产生带有残留催化剂的容器,环保经济,操作简便。(The invention relates to the field of catalyst preparation, and discloses a preparation method of a catalyst used in polypropylene production. The method comprises the following steps: 1) after the main catalyst storage unit makes the main catalyst and the vaseline oil perform first contact, obtaining a first mixture, and feeding the first mixture into a main catalyst preparation unit; 2) the vaseline fat is conveyed from the vaseline fat storage unit to the main catalyst preparation unit through the vaseline fat conveying unit; 3) carrying out second contact on the first mixture and vaseline in a main catalyst preparation unit to obtain a second mixture; 4) and feeding the second mixture into a catalyst pre-contact unit, and carrying out third contact on the second mixture and the cocatalyst to obtain the catalyst. The method can solve the problem that the solid catalyst is attached to a container during feeding, not only reduces the waste of the catalyst, but also does not produce a container with residual catalyst, and is environment-friendly, economic and simple and convenient to operate.)

1. A method of formulating a catalyst, the method comprising the steps of:

1) after the main catalyst storage unit (100) makes the main catalyst and the vaseline oil perform first contact, obtaining a first mixture, and feeding the first mixture into a main catalyst preparation unit (300);

2) the vaseline oil is conveyed from a vaseline oil storage unit (200) to a main catalyst preparation unit (300) through a vaseline oil conveying unit;

3) carrying out second contact on the first mixture and vaseline in a main catalyst preparation unit (300) to obtain a second mixture;

4) and feeding the second mixture into a catalyst pre-contact unit (400), and carrying out third contact on the second mixture and the cocatalyst to obtain the catalyst.

2. The method for preparing the catalyst according to claim 1, wherein in the step 1), the main catalyst is a spherical polypropylene catalyst for loop process;

preferably, the primary catalyst is a DQC401 catalyst and/or an HR catalyst; more preferably, the primary catalyst is a DQC401 catalyst;

preferably, the mass-to-volume ratio of the main catalyst to the vaseline oil is 1: 2.5-4kg/L, preferably 1: 2.8-3.2kg/L, more preferably 1: 3-3.2 kg/L.

3. The method of formulating a catalyst according to claim 1 or 2, wherein the method further comprises: a step of mixing a first mixture before feeding the first mixture to a main catalyst preparation unit (300);

preferably, the mixing is performed by rotating the main catalyst storage unit (100) on the main catalyst tank drum (120);

preferably, the rotation time is 8-48h, more preferably 16-48h, and further preferably 24-48 h;

preferably, the main catalyst storage unit (100) is a storage tank.

4. The method for formulating a catalyst according to any one of claims 1-3, wherein the first mixture in the main catalyst storage unit (100) is fed to the main catalyst formulation unit (300) using an inert gas (N);

preferably, the inert gas (N) is N₂CO and CO₂Preferably N, is preferably N₂；

Preferably, the pressure of the inert gas (N) is 0.2 to 0.6MPa, preferably 0.3 to 0.6MPa, more preferably 0.4 to 0.5 MPa.

5. The method for preparing a catalyst according to any one of claims 1 to 3, wherein in the step 2), the petrolatum storage unit (200) is a storage tank;

preferably, the petrolatum storage unit (200) has a stirrer (201) and a bubbler (202);

preferably, in the petrolatum storage unit (200), the petrolatum is stirred in the presence of an inert gas (N) before being transferred to the main catalyst formulation unit (300);

preferably, the inert gas (N) is N₂CO and CO₂Preferably N, is preferably N₂；

Preferably, the stirring temperature is 60-90 ℃, and the stirring time is 8-48 h; more preferably, the stirring temperature is 70-90 ℃, and the stirring time is 16-48 h; further preferably, the stirring temperature is 70-80 ℃, and the stirring time is 24-48 h.

6. The method for preparing a catalyst according to any one of claims 1 to 3, wherein in the step 2), the petrolatum delivery unit includes a pipe connecting the petrolatum storage unit (200) with the main catalyst preparation unit (300), and a petrolatum delivery pump (210) and a petrolatum filter (220) disposed on the pipe.

7. The method for preparing a catalyst according to any one of claims 1 to 3, wherein the mass-to-volume ratio of the main catalyst to the petrolatum is 1: 1.3-2kg/L, preferably 1: 1.4-1.8kg/L, more preferably 1: 1.5-1.7 kg/L.

8. The method for formulating a catalyst according to any one of claims 1 to 3, wherein, in step 3), the main catalyst formulation unit (300) is a formulation tank;

preferably, the main catalyst preparation unit (300) is provided with a stirrer (301), and after the first mixture and the vaseline ester are conveyed to the main catalyst preparation unit (300), the main catalyst preparation unit (300) is vacuumized and stirred;

preferably, the degree of vacuum is 1-50mmHg, preferably 15-25 mmHg;

preferably, the stirring temperature is 60-80 ℃, and the stirring time is 4-96 h.

9. The method of formulating a catalyst as set forth in any of claims 1-3, further comprising reducing the temperature of the second mixture to 8-12 ℃ prior to delivering the second mixture to the catalyst precontacting unit (400).

10. The process for the preparation of a catalyst according to any one of claims 1 to 3, wherein the cocatalyst is triethylaluminium;

preferably, the mass ratio of the main catalyst to the cocatalyst is 1: 0.2 to 1, preferably 1: 0.2-0.8; more preferably 1: 0.3-0.5.

11. Use of the method of formulating a catalyst according to any one of claims 1 to 10 in the formulation of a polypropylene catalyst.

Technical Field

The invention relates to the field of catalyst preparation, in particular to a preparation method of a catalyst used in polypropylene production.

Background

At present, in the process of producing polypropylene by a continuous method, whether the SPHERIPOL process or the ST process is adopted, the preparation method of the catalyst is to add the solid catalyst into the mixture of the vaseline oil and the vaseline fat, or to add the vaseline oil, the solid catalyst and the vaseline fat in sequence and then mix the mixture. In actual industrial production, the solid catalyst is generally added by pouring the solid catalyst directly from its packaging container to a catalyst preparation tank.

The solid catalyst particles are small and easy to absorb moisture and are powdery, so that the solid catalyst particles are partially attached to the wall of a packaging container during pouring and cannot be completely poured out, and a small amount of solid catalyst particles are still attached even under the beating and shaking of a shaker. Especially in wet summer, the adhesion phenomenon of the solid catalyst is more serious. Therefore, not only is the waste of production raw materials caused, but also the treatment of the catalyst container causes severe environmental protection pressure for the production enterprises because the catalyst belongs to dangerous chemicals. In addition, when the catalyst is prepared by using the method, even if the catalyst is stirred, the solid catalyst is still difficult to be completely and uniformly dispersed in the vaseline oil and the vaseline grease, part of the solid catalyst is not uniformly dispersed, so that the solid catalyst is agglomerated and agglomerated, and further blocks with different sizes are formed, and the blocks also block pipelines, so that the smooth production is influenced.

Disclosure of Invention

The invention aims to overcome the problems and provides a preparation method of a catalyst, which can solve the problem that a solid catalyst is attached to a container during feeding, reduce the waste of the catalyst, avoid the generation of a container with the residual catalyst, and is environment-friendly, economical and simple to operate.

In order to achieve the above object, the present invention provides a method for preparing a catalyst, comprising the steps of:

1) after the main catalyst storage unit 100 makes the main catalyst and the vaseline oil perform the first contact, a first mixture is obtained, and the first mixture is sent to the main catalyst preparation unit 300;

2) the vaseline fat is transported from the vaseline fat storage unit 200 to the main catalyst preparation unit 300 through the vaseline fat delivery unit;

3) carrying out second contact on the first mixture and vaseline in the main catalyst preparation unit 300 to obtain a second mixture;

4) after the second mixture is fed to the catalyst pre-contacting unit 400, it is subjected to a third contact with the cocatalyst to obtain a catalyst.

Preferably, in step 1), the main catalyst is a spherical polypropylene catalyst for loop process.

Preferably, the primary catalyst is a DQC401 catalyst and/or an HR catalyst; more preferably, the primary catalyst is a DQC401 catalyst.

Preferably, the mass-to-volume ratio of the main catalyst to the vaseline oil is 1: 2.5-4kg/L, preferably 1: 2.8-3.2kg/L, more preferably 1: 3-3.2 kg/L.

Preferably, the method further comprises: a step of mixing the first mixture before feeding the first mixture into the main catalyst preparation unit 300.

Preferably, the mixing is performed by rotating the main catalyst storage unit 100 on the main catalyst tank drum 120.

Preferably, the rotation time is 8-48h, more preferably 16-48h, and even more preferably 24-48 h.

Preferably, the main catalyst storage unit 100 is a storage tank.

Preferably, the first mixture in the main catalyst storage unit 100 is fed to the main catalyst preparation unit 300 using an inert gas N.

Preferably, the inert gas N is N₂CO and CO₂Preferably N, is preferably N₂。

Preferably, the pressure of the inert gas N is 0.2 to 0.6MPa, preferably 0.3 to 0.6MPa, more preferably 0.4 to 0.5 MPa.

Preferably, in step 2), the petrolatum storage unit 200 is a storage tank.

Preferably, the petrolatum storage unit 200 has a stirrer 201 and a bubbler 202.

Preferably, the petrolatum is stirred in the presence of the inert gas N before being transferred to the main catalyst formulation unit 300 in the petrolatum storage unit 200.

Preferably, the inert gas N is N₂CO and CO₂Preferably N, is preferably N₂。

Preferably, the stirring temperature is 60-90 ℃, and the stirring time is 8-48 h; more preferably, the stirring temperature is 70-90 ℃, and the stirring time is 16-48 h; further preferably, the stirring temperature is 70-80 ℃, and the stirring time is 24-48 h.

Preferably, in step 2), the petrolatum delivery unit includes a pipeline connecting the petrolatum storage unit 200 and the main catalyst preparation unit 300, and a petrolatum delivery pump 210 and a petrolatum filter 220 disposed on the pipeline.

Preferably, the mass-volume ratio of the main catalyst to the vaseline oil is 1: 1.3-2kg/L, preferably 1: 1.4-1.8kg/L, more preferably 1: 1.5-1.7 kg/L.

Preferably, in step 3), the main catalyst preparation unit 300 is a preparation tank.

Preferably, the main catalyst preparation unit 300 has a stirrer 301, and after the first mixture and the petrolatum are delivered to the main catalyst preparation unit 300, the main catalyst preparation unit 300 is vacuumized and stirred.

Preferably, the degree of vacuum is 1 to 50mmHg, preferably 15 to 25 mmHg.

Preferably, the stirring temperature is 60-80 ℃, and the stirring time is 4-96 h.

Preferably, the method further comprises reducing the temperature of the second mixture to 8-12 ℃ prior to delivering the second mixture to the catalyst precontacting unit 400.

Preferably, the cocatalyst is triethylaluminium.

Preferably, the mass ratio of the main catalyst to the cocatalyst is 1: 0.2 to 1, preferably 1: 0.2-0.8; more preferably 1: 0.3-0.5.

The second aspect of the invention provides the application of the preparation method of the catalyst in the preparation of a polypropylene catalyst.

According to the technical scheme, the main catalyst and the vaseline oil are mixed in the main catalyst storage unit in advance, and then the main catalyst and the vaseline oil are introduced into the main catalyst preparation unit to be mixed, so that the problem that part of the main catalyst is remained in a packaging container when the main catalyst is directly fed into the main catalyst preparation unit is solved. The invention not only can prevent polypropylene preparation factories from processing catalyst packaging containers, but also can improve the caking phenomenon generated in the catalyst preparation process and improve the production quality. In addition, the main catalyst storage device for mixing the main catalyst and the vaseline oil can be recycled after cleaning, so that the resource waste is further reduced.

Drawings

FIG. 1 is a simplified schematic of the catalyst formulation process of the present invention.

Description of the reference numerals

100: the main catalyst storage unit 120: main catalyst tank drum

111. 112, 113: electromagnetic valve 200: vaseline fat storage unit

201. 301, 401: the stirrer 202: bubbling device

210: petrolatum delivery pump 220: vaseline fat filter

300: main catalyst preparation unit 310: main catalyst filter

320: metering pump 400: catalyst precontacting unit

N: inert gas

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

FIG. 1 is a simplified schematic of the catalyst formulation process of the present invention. As shown in fig. 1, the preparation method of the catalyst provided by the present invention comprises the following steps:

1) after the main catalyst storage unit 100 makes the main catalyst and the vaseline oil perform the first contact, a first mixture is obtained, and the first mixture is sent to the main catalyst preparation unit 300;

2) the vaseline fat is transported from the vaseline fat storage unit 200 to the main catalyst preparation unit 300 through the vaseline fat delivery unit;

3) carrying out second contact on the first mixture and vaseline in the main catalyst preparation unit 300 to obtain a second mixture;

4) after the second mixture is fed to the catalyst pre-contacting unit 400, it is subjected to a third contact with the cocatalyst to obtain a catalyst.

The preparation method of the catalyst can be applied to the preparation of the catalyst used in the production of polypropylene, in the current production of polypropylene, a polypropylene production enterprise purchases a main catalyst from a catalyst manufacturer and then prepares the main catalyst with vaseline and vaseline oil on a production site, a part of the main catalyst remains on the wall of a packaging container in the catalyst feeding process, the complete feeding is difficult, the waste of production raw materials is caused, and the problem of difficult treatment of the container with the main catalyst remains is also caused.

In the invention, the main catalyst and the vaseline oil are stored in a main catalyst storage tank in advance, the whole catalyst is transported to a polypropylene preparation factory, and an empty tank for storing the main catalyst can be recycled, cleaned and reused after the catalyst is prepared. Therefore, the problems of catalyst residue and difficulty in processing containers with catalyst residues in the prior art can be solved, waste is reduced, and the cyclic utilization of resources is realized.

According to the present invention, in step 1), the main catalyst may be various spherical polypropylene catalysts used in the loop process, for example, may be a DQC401 catalyst and/or an HR catalyst, preferably a DQC401 catalyst.

According to the present invention, in step 1), the amounts of the main catalyst and the vaseline oil may vary within a wide range, and are not particularly limited as long as the main catalyst can be uniformly dispersed. The dosage of the vaseline oil can be determined according to the dosage of a main catalyst, and preferably, the mass-to-volume ratio of the main catalyst to the vaseline oil is 1: 2.5-4kg/L, preferably 1: 2.8-3.2kg/L, more preferably 1: 3-3.2 kg/L.

According to the present invention, in step 1), the main catalyst storage unit 100 may be various devices used for storage in the art, as long as the purpose of storage and transportation can be satisfied, and is not particularly limited. Preferably, the main catalyst storage unit 100 is a storage tank.

In the present invention, in order to prevent the main catalyst from being oxidized and deteriorated in contact with air and affecting the catalyst activity, the main catalyst storage unit 100 may introduce an inert gas so that the first contact is performed under the protection of the inert gas.

The introduced inert gas may be various gases that do not react with the main catalyst. The kind of the inert gas is not particularly limited, and may be, for example, N₂CO and CO₂Preferably N, is preferably N₂。

In the present invention, the pressure of the inert gas filled in the main catalyst storage unit may be 0.01 to 0.06MPa, preferably 0.03 to 0.05 MPa.

In the present invention, the main catalyst storage unit 100 may be rotated on the main catalyst tank drum 120 to mix the first mixture in the main catalyst storage unit 100.

In the present invention, after the first contact is completed, before the catalyst is sent to the main catalyst preparation unit 300 for main catalyst preparation, preferably, the main catalyst storage unit 100 is rotated on the main catalyst tank drum 120 for 8-48 h; more preferably, the main catalyst storage unit 100 is rotated on the main catalyst tank drum 120 for 16-48 h; further preferably, the main catalyst storage unit 100 is rotated on the main catalyst tank drum 120 for 24-48 h. Through the rotation within the time range, the first mixture in the main catalyst storage unit 100 can be uniformly mixed, which is not only beneficial to the dispersion of the main catalyst, but also can avoid the agglomeration of the main catalyst, prevent the pipeline from being blocked in the transferring process and be beneficial to the subsequent preparation.

According to the present invention, the first mixture in the main catalyst storage unit 100 may be fed into the main catalyst preparation unit 300 through a main catalyst delivery unit including a pipeline and solenoid valves 112 and 113 provided on the pipeline.

According to the present invention, the first mixture may be fed to the main catalyst preparation unit 300 using an inert gas N. The inert gas N is not particularly limited as long as it does not affect the activity of the catalyst. The inert gas N may be N₂CO and CO₂Preferably N, is preferably N₂。

In the present invention, the pressure of the inert gas N is not particularly limited as long as the first mixture can be fed to the main catalyst preparation unit 300. Preferably, the pressure of the inert gas N is 0.2 to 0.6MPa, preferably 0.3 to 0.6MPa, more preferably 0.4 to 0.5 MPa.

According to the present invention, in step 2), the petrolatum storage unit 200 may be various storage devices generally used in the art, and may be, for example, a storage tank.

Preferably, the petrolatum storage unit 200 has a stirrer 201 and a bubbler 202.

According to the present invention, before the petrolatum is sent to the main catalyst preparation unit 300, the inert gas N may be blown into the petrolatum storage unit 200 by the bubbler 202, and under the combined action of the blowing of the inert gas N and the stirring by the stirrer 201, the moisture in the petrolatum may be removed, so as to achieve the purpose of drying and dehydrating the petrolatum, and prevent the main catalyst from being adversely affected by the presence of moisture in the subsequent steps.

According to the present invention, the inert gas N blown by the bubbler is not particularly limited as long as it does not affect the catalyst activity, and may be, for example, N₂CO and CO₂Preferably N, is preferably N₂。

According to the present invention, the amount of air taken into the bubbler may be varied within a wide range without particular limitation, and may be, for example, 1 to 10Nm³H, preferably 5 to 10Nm³/h。

According to the invention, in order to fully dehydrate the vaseline fat, the stirring temperature is preferably 60-90 ℃, and the stirring time is preferably 8-48 h; more preferably, the stirring temperature is 70-90 ℃, and the stirring time is 16-48 h; further preferably, the stirring temperature is 70-80 ℃, and the stirring time is 24-48 h.

According to the present invention, in step 2), the petrolatum delivery unit includes a pipeline, and a petrolatum delivery pump 210 and a petrolatum filter 220 mounted on the pipeline. The vaseline transfer pump 210 is used for providing power, and the vaseline filter 220 is used for filtering vaseline to prevent the pipeline from being blocked by the caked vaseline.

In the present invention, one end of the vaseline resin delivery unit is connected to the vaseline resin storage unit 200, and the other end is connected to the main catalyst preparation unit 300, so that vaseline resin is delivered from the vaseline resin storage unit 200 to the main catalyst preparation unit 300.

According to the present invention, in step 3), the main catalyst preparation unit 300 may be any of various devices generally used in the art for preparing a catalyst, for example, a preparation tank. Preferably, the main catalyst preparation unit 300 has a stirrer 301, and the contents in the preparation unit can be stirred. Preferably, the main catalyst formulation unit 300 can regulate temperature.

In the present invention, the main catalyst preparation unit 300 may be preheated in advance, and then the first mixture and the vaseline may be fed into the main catalyst preparation unit 300 to be mixed. This can shorten the preparation time of the catalyst.

The amount of the petrolatum according to the present invention may vary widely and is not particularly limited. The amount of the petrolatum may be determined according to the amount of the main catalyst, and preferably, the mass volume ratio of the main catalyst to the petrolatum is 1: 1.3-2kg/L, preferably 1: 1.4-1.8kg/L, more preferably 1: 1.5-1.7 kg/L.

After the first mixture and the petrolatum are fed into the main catalyst preparation unit 300, the main catalyst preparation unit 300 is vacuumized and stirred in order to prevent air from adversely affecting the main catalyst. Preferably, the degree of vacuum of the vacuum is 1-50mmHg, and more preferably, the degree of vacuum of the vacuum is 15-25 mmHg.

According to the invention, in order to uniformly mix the first mixture and the vaseline fat, the stirring temperature is preferably 60-80 ℃, and the stirring time is preferably 4-96 hours; more preferably, the stirring temperature is 65-75 ℃, and the stirring time is 48-72 h.

According to the present invention, in order to ensure that the temperature of the catalyst slurry is consistent with that of the reaction raw material propylene and to prevent the polymer generated by the prepolymerization from being broken, the second mixture is subjected to a temperature reduction treatment before being transferred to the catalyst precontacting unit 400. Preferably, the temperature of the second mixture is reduced to 8-12 ℃; more preferably, the temperature of the second mixture is reduced to 9-11 ℃.

According to the present invention, in step 4), the second mixture is fed to the catalyst pre-contact unit 400 through a main catalyst delivery unit, which includes a pipe, and a filter 310 and a metering pump 320 disposed on the pipe. The filter 310 is used to filter the second mixture, further preventing the catalyst from plugging the tubes. The metering pump 320 is used to meter the amount of the second mixture fed to the catalyst precontacting unit 400, thereby calculating the amount of the subsequent cocatalyst.

In the present invention, for the main catalyst to form the active site, for example, Ti⁴⁺Reduction to Ti³⁺The present invention uses a cocatalyst which can be any of the various cocatalysts used in the art for the preparation of polypropylene, for example, triethylaluminum.

According to the present invention, the second mixture is subjected to a third contact with the cocatalyst in the catalyst precontacting unit 400. The catalyst precontacting unit 400 may be a contact tank, and preferably, the catalyst precontacting unit 400 has an agitator 401.

In the present invention, the amount of the co-catalyst may be determined according to the amount of the main catalyst, and preferably, the mass ratio of the main catalyst to the co-catalyst is 1: 0.2 to 1, preferably 1: 0.2-0.8; more preferably 1: 0.3-0.5.

According to the present invention, in order to ensure the stereospecificity of the polymer, in addition to the second mixture and the cocatalyst, an external electron DONOR may be further added in the third contacting of the precontacting unit, and the external electron DONOR may be various external electron DONORs commonly used in the art for preparing polypropylene, such as one or more of methylcyclohexyldimethoxysilane (C-DONOR), dicyclopentyldimethoxysilane (D-DONOR), tetraethoxysilane (T-DONOR) and diisopropyldimethoxysilane (P-DONOR), preferably, methylcyclohexyldimethoxysilane (C-DONOR).

In the present invention, the amount of the external electron donor may be determined according to the amount of the main catalyst, and preferably, the mass ratio of the main catalyst to the external electron donor is 1: 0.01 to 0.15, preferably 1: 0.01-0.1; more preferably 1: 0.01-0.03.

According to the present invention, the second mixture, the cocatalyst and the external electron donor are thoroughly mixed after precontacting in the catalyst precontacting unit 400, and the mixing may be performed by stirring through the stirrer 401. The stirring temperature is 8-12 ℃, the stirring time is 1-10min, preferably, the stirring temperature is 9-11 ℃, and the stirring time is 3-5 min.

The second aspect of the invention provides an application of the preparation method of the catalyst in the preparation of a polypropylene catalyst.

The present invention will be described in detail below with reference to examples, but the present invention is not limited to the following examples. In the following examples, all reagents used are commercially available unless otherwise specified.

Example 1

1) 80kg of main catalysts DQC401 and 248L of vaseline oil are put into a main catalyst storage tank with the volume of 460L to obtain a first mixture, nitrogen is filled into the main catalyst storage tank until the pressure is 0.05Mpa, and then the mixture is conveyed to a polypropylene preparation factory.

2) Before catalyst preparation, rotating the main catalyst storage tank on a catalyst tank rotary drum for 24 hours, and then sending the first mixture into a main catalyst preparation tank preheated to 70 ℃ by nitrogen with the pressure of 0.5 Mpa;

3) adding 124L of vaseline and fat into a vaseline and fat storage tank, opening a bubbler, blowing nitrogen gas into the bubbler while stirring, wherein the nitrogen gas flow blown by the bubbler is 5Nm³The stirring temperature is 70 ℃, and the stirring time is 24 h. Then the mixture is filtered by a vaseline filter through a vaseline conveying pump and then is sent into a main catalyst preparation tank which is preheated to 70 ℃;

wherein, step 2) and step 3) can be performed simultaneously.

4) Vacuumizing the main catalyst preparation tank and stirring the second mixture, wherein the vacuum degree is 20mmHg, the stirring temperature is 70 ℃, and the stirring time is 48 hours; after stirring, the temperature of the second mixture in the main catalyst preparation tank is reduced to 10 ℃.

5) And (3) feeding the second mixture obtained in the step 4) into a catalyst pre-contact tank through a main catalyst filter and a metering pump, mixing the second mixture with 24kg of triethyl aluminum and 0.8kg of methylcyclohexyl dimethoxysilane (C-DONOR) in the pre-contact tank, and stirring the mixture at 10 ℃ for 4 minutes to obtain the catalyst.

Example 2

The procedure was followed as in example 1, except that the amount of the main catalyst was 80kg, the amount of vaseline oil was 240L, the amount of vaseline oil was 120L, the amount of the co-catalyst was 40kg, and the amount of the external electron donor was 2.4 kg.

Example 3

The procedure was followed as in example 1, except that 80kg of the main catalyst, 256L of vaseline oil, 136L of vaseline oil, 32kg of the cocatalyst and 1.6kg of the external electron donor were used.

By adopting the technical scheme, the main catalyst and the vaseline oil are mixed in the main catalyst storage tank (main catalyst storage unit) in advance, and then the main catalyst preparation tank (main catalyst preparation unit) is introduced to be mixed with the vaseline oil again, so that the problem that part of the main catalyst is remained in a packaging container when the main catalyst is directly fed into the main catalyst preparation tank is solved. In addition, the main catalyst storage tank for mixing the main catalyst and the vaseline oil can be recycled after cleaning, so that the resource waste is further reduced.

The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.

It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. The invention is not described in detail in order to avoid unnecessary repetition.

In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.