CN112724283B - Method for preparing polypropylene random copolymer of propane and butane - Google Patents
Method for preparing polypropylene random copolymer of propane and butane Download PDFInfo
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Abstract
The invention relates to the technical field of olefin polymerization and materials, and discloses a method for preparing polypropylene random copolymer, which comprises the following steps: mixing the polypropylene base material with a degrading agent, an antioxidant and a halogen absorbent; wherein, the dosage of the degradation agent is 0.01 to 0.18 weight part relative to 100 weight parts of the polypropylene-random copolymer base material. Through the technical scheme, the method can effectively degrade the polypropylene random copolymer under the condition of lower content of the degradation agent.
Description
Technical Field
The invention relates to the technical field of olefin polymerization and materials, in particular to a method for preparing polypropylene random copolymer.
Background
The polypropylene fiber or the non-woven fabric has soft hand feeling and exquisite appearance, has the advantages of moisture resistance, air permeability, light weight, acid and alkali resistance and the like, and is widely applied to the fields of sanitary materials (such as masks), medical supplies, packaging, building materials and the like.
Such polypropylenes are generally required to have a narrow molecular weight distribution (generally required < 4), a suitable melt flow rate (MFR (> 30g/10 min), and good flowability. There are currently mainly two processes for preparing such polypropylenes. One method is to control the melt flow rate of the polymer by adjusting the amount of chain transfer agent-hydrogen added during the polymerization process. The polymer obtained by adopting the Z-N catalyst has lower MFR and wider molecular weight distribution; the polymer MFR obtained by adopting the metallocene catalyst can be very large and has narrow molecular weight distribution, but the metallocene catalyst has strong hydrogen sensitivity, the polymer MFR can not be well stably controlled in the production process, and the catalyst cost is higher. The other method is to add a degrading agent (generally peroxide) into the low-melting-index polypropylene powder, so that the molecular chain of the polypropylene is broken in the granulation process, and the high-melting-index and narrow-molecular-weight-distribution polypropylene is obtained through degradation. The method has the advantages of low production cost, wide polymer MFR adjustable range and narrow molecular weight distribution, and can be widely applied to the preparation of polypropylene fiber products.
The polypropylene degradation technology generally requires that the molecular weight distribution of a base material is narrow, so that a product with narrower molecular weight distribution can be prepared under the action of a degradation agent, and the processing performance of the product can be improved. In the traditional degradation method, the polypropylene fiber material adopts homo-polypropylene or propylene-ethylene random copolymerization polypropylene base material, and no report related to degradation of propylene-butylene random copolymerization polypropylene base material exists.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provide a method for preparing polypropylene random copolymer of propane and butane.
In order to achieve the above objects, the present invention provides a method for preparing a polypropylene random copolymer, comprising: mixing the polypropylene base material with a degrading agent, an antioxidant and a halogen absorbent; wherein, the dosage of the degradation agent is 0.01 to 0.18 weight part relative to 100 weight parts of the polypropylene-random copolymer base material.
Through the technical scheme, the method can effectively degrade the polypropylene random copolymer under the condition of lower content of the degradation agent, the whole process can be carried out without using other components (such as a carrier of the degradation agent), and the method is simple and easy to implement.
The polypropylene random copolymer of propane and butane obtained by the invention has the characteristics of high melt index, narrow molecular weight distribution, low content of xylene soluble substances, high tensile strength and the like, and simultaneously has good processing performance and spinnability, and can be widely applied to the fields of polypropylene fiber materials, non-woven fabrics and the like. Specifically, the melt index of the degraded polypropylene random copolymer of the invention is 20-50g/10min (more than 35g/10min in a preferred embodiment), the molecular weight distribution is less than 3, the tensile strength is more than 26MPa, the flexural modulus is less than 1.1Gpa, and the xylene soluble content is less than 3wt.%.
Detailed Description
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.
The invention provides a method for preparing polypropylene random copolymer, which is characterized by comprising the following steps: mixing the polypropylene base material with a degrading agent, an antioxidant and a halogen absorbent; wherein, the amount of the degradation agent is 0.01-0.18 weight part relative to 100 weight parts of the polypropylene random copolymer base material.
According to the present invention, the process may be performed with a lower amount of the degradation agent used, and thus, it is preferable that the degradation agent is used in an amount of 0.03 to 0.055 parts by weight, such as 0.03 parts by weight, 0.032 parts by weight, 0.036 parts by weight, 0.038 parts by weight, 0.04 parts by weight, 0.05 parts by weight, 0.052 parts by weight, 0.054 parts by weight, 0.055 parts by weight, or any value therebetween, with respect to 100 parts by weight of the polypropylene random copolymer base material.
According to the invention, the degrading agent can be various organic peroxides commonly used in the art, in particular of the general formula R 1 -O-H or R 2 —O—O—R 3 Wherein R is 1 、R 2 And R 3 Each independently is an organic group such as an alkyl group, an acyl group, or a carbonate group.
Preferably, the degradation agent is selected from one or more of benzoyl peroxide, t-butyl peroxybenzoate, di-t-butyl peroxide, t-butyl peroxy-2-hexylhexanoate, t-butyl hydroperoxide, 5-dimethyl-2, 5-di (t-butyl) hexane peroxide, 6, 9-triethyl-3, 6, 9-trimethyl-1, 4, 7-triperoxonane, di-t-amyl peroxide, 2, 5-dimethyl-2, 5-bis (t-butylperoxy) hexane, dicumyl peroxide, and 3,6, 9-triethyl-3, 6, 9-trimethyl-1, 4, 7-triperoxonane; more preferably at least one selected from the group consisting of 5-dimethyl-2,5 bis (t-butylperoxy) hexane, dicumyl peroxide and 3,6, 9-triethyl-3, 6, 9-trimethyl-1, 4, 7-triperoxonane.
According to the present invention, there is no particular requirement for the amount of the antioxidant, and preferably the antioxidant is used in an amount of 0.04 to 0.4 parts by weight, such as 0.04 parts by weight, 0.05 parts by weight, 0.08 parts by weight, 0.1 parts by weight, 0.2 parts by weight, 0.3 parts by weight, 0.4 parts by weight, or any value therebetween.
According to the present invention, the antioxidant may be an antioxidant conventionally used in the art, and preferably, the antioxidant is selected from at least one of antioxidant 1010 (CAS number: 6683-19-8), antioxidant 1790 (CAS number: 40601-76-1), antioxidant B501W (complex antioxidant), antioxidant 1076 (CAS number: 2082-79-3), antioxidant 1024 (CAS number: 32687-78-8), antioxidant CA (CAS number: 1843-03-4), and antioxidant 168 (CAS number: 31570-04-4). More preferably, the antioxidant of the present invention is composed of a primary antioxidant and a secondary antioxidant, wherein the primary antioxidant is at least one selected from the group consisting of antioxidant 1010, antioxidant 1790, antioxidant 1076, antioxidant 1024 and antioxidant CA; the auxiliary antioxidant is antioxidant 168. The weight ratio of the primary antioxidant to the secondary antioxidant can be 1. According to another preferred embodiment of the invention, the antioxidant is antioxidant B501W.
According to the present invention, the amount of the halogen absorbent used is not particularly limited, but is preferably 0.03 to 0.2 parts by weight, such as 0.03 parts by weight, 0.04 parts by weight, 0.05 parts by weight, 0.06 parts by weight, 0.1 parts by weight, 0.2 parts by weight, or any value therebetween.
According to the present invention, the halogen absorbent may be a halogen absorbent conventionally used in the art, preferably, the halogen absorbent is hydrotalcite, metal stearate, etc., more preferably selected from calcium stearate, zinc stearate, sodium stearate, and hydrotalcite (e.g., aluminum magnesium hydrotalcite, mgAl (OH) 3 CO 3 ·H 2 O).
The process of the present invention is particularly suitable for the degradation of polypropylenes having a narrow molecular weight distribution, and therefore, according to a preferred embodiment of the present invention, the molecular weight distribution of the polypropylene random copolymer base is < 4.5 (e.g., 2, 2.3, 2.4, 2.5, 3, 3.5, 4, 4.5 or any value therebetween). According to one embodiment of the present invention, the butene content of the propane-butene random copolymer polypropylene base may be 0.5 to 6mol%, preferably 2 to 5.5mol% (or 2.5 to 5 mol%). According to another embodiment of the present invention, the melt index of the polypropylene random copolymer base material at 230 ℃ under a load of 2.16kg may be 0.5-10g/10min, preferably 2-8g/10min (e.g., 2g/10min, 2.5g/10min, 3g/10min, 4g/10min, 4.5g/10min, 5g/10min, 6g/10min, 7g/10min, 8g/10min or any value therebetween).
According to the present invention, the propane-butane random copolymer polypropylene base may be obtained in a conventional manner, but according to a preferred embodiment of the present invention, the preparation of the propane-butane random copolymer polypropylene base comprises the steps of:
step A: the catalyst, the organic aluminum (cocatalyst) and the external electron donor are pre-contacted to obtain a catalyst system with an active center, and a prepolymerization reaction is carried out in the presence of a propylene monomer; or the catalyst, the organic aluminum and the external electron donor are directly subjected to prepolymerization reaction without precontacting;
and B: and (3) copolymerizing the catalyst particles after the prepolymerization reaction in the presence of a comonomer 1-butene to obtain the propylene-butene random copolymer polypropylene. Can be prepared by introducing H 2 Controlling the polymer melt index.
The polypropylene catalyst in step a is a Ziegler-Natta catalyst having high stereoselectivity, which means a catalyst that can be used to prepare a propylene homopolymer having an isotactic index of greater than 96%. Such catalysts are generally titanium-containing solid catalysts, and the main components thereof are magnesium, titanium, halogen and an internal electron donor, wherein the internal electron donor can be at least one selected from diesters, ethers, succinates, 1, 3-alcohol esters and sulfonamides known in the art, and phosphoric acid esters and diethers are preferred.
The organoaluminum in step A is not limited to any organoaluminum commonly used in the current polyolefin industry and commonly used, and is preferably at least one member selected from the group consisting of trialkylaluminums (e.g., trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-butylaluminum, trihexylaluminum, trioctylaluminum, etc.), diethylaluminum monochloride, diisobutylaluminum monochloride, ethylaluminum dichloride and ethylaluminum dichloride.
The external electron donor in step A is preferably an organosilicon compound having the general formula R n Si(OR') 4-n Wherein n is more than 0 and less than or equal to 3, R is selected from hydrogen atom, halogen, alkyl, cycloalkyl, aryl and halogenated alkyl, and R' is selected from alkyl, cycloalkyl, aryl and halogenated alkyl. Specifically, the method may include but is not limited to: cyclohexylmethyldimethoxysilane, diisopropyldimethoxysilane, tetramethoxysilane, tetraethoxysilane, trimethylmethoxysilane, trimethylethoxysilane, trimethylphenoxysilane, dimethyldimethoxysilane, dimethyldiethoxysilane, methyl-t-butyldimethoxysilane, methylisopropyldimethoxysilane, diphenoxydimethoxysilane, diphenyldiethoxysilane, phenyltrimethoxysilane, phenyltriethoxysilane, vinyltrimethoxysilane, (1, 1-trifluoro-2-propyl) -2-ethylpiperidinyldimethoxysilane, and (1, 1-trifluoro-2-propyl) -methyldimethoxysilane, and the like.
In step a, the amount of the catalyst, the organoaluminum and the external electron donor can be determined according to the need, and preferably, the weight ratio of the organoaluminum to the catalyst is 1. The weight ratio of the organoaluminium to the external electron donor may be from 0.1 to 150, preferably from 2 to 1.
The precontacting in step A can be continuous or batch operation and can be carried out by means of a reactor, and the precontacting reactor can be a kettle type reactor, a tubular type reactor and other reactors with mixing action. The pre-contact temperature can be controlled between-10 ℃ and 60 ℃, and the preferred temperature is 0 ℃ to 30 ℃. The pre-contact time is controlled within 0.1-180min, preferably 5-30min.
In the step A, the catalyst which is or is not pre-contacted is subjected to prepolymerization treatment, and the prepolymerization reactor can be in a kettle type, a loop type or other forms with mixing action. The prepolymerization can be carried out continuously under liquid phase bulk conditions or intermittently in an inert solvent. The temperature of the prepolymerization can be controlled between-10 ℃ and 60 ℃, preferably 0-40 ℃. The ratio of prepolymerization is controlled to 0.5-1000 times, preferably 1.0-500 times.
The copolymerization in step B may be carried out continuously or batchwise.
The copolymerization according to step B can be carried out in one or more reactors connected in series, preferably in a single reactor, in order to ensure a narrow molecular weight distribution. The polymerization reactor in step B may be a liquid phase reactor or a gas phase reactor.
The liquid phase reactor may be one of a loop reactor or a tank reactor. The temperature of the liquid phase polymerization reaction is 30-150 ℃, and preferably 60-95 ℃; the reaction pressure is 1-8MPa, preferably 1.2-5.5MPa; the reaction time is 10-180min, preferably 20-120min; the molar concentration of the butene fed into the reactor is 0-35%, preferably 4-22%; the molar concentration of hydrogen is from 0 to 4000ppm, preferably from 300 to 2000ppm.
The gas phase reactor may be in the form of a stirred tank reactor, a horizontal stirred reactor, a vertical stirred reactor, a fluidized bed reactor, or the like. The gas-phase polymerization temperature is 0-150 ℃, and preferably 40-100 ℃; the polymerization pressure is more than or equal to the normal pressure, and preferably 0.5-2.5MPa; the reaction time is 10 to 180 minutes, preferably 20 to 120 minutes; the molar concentration of the butene fed to the reactor is between 0 and 35%, preferably between 4 and 22%; the molar concentration of hydrogen is 0-8000ppm, preferably 300-4000ppm.
And D, transferring the polypropylene particles obtained by the reaction in the step B into a separation tank, and separating the polypropylene, propylene, comonomer, hydrogen and the like to obtain the base material of the polypropylene random copolymer. The separation may be by flash separation. The conditions for the flash separation include: the temperature is 40-100 ℃, preferably 50-85 ℃; the pressure is 0.1-2.5MPa, preferably 0.3-2MPa.
According to one embodiment of the present invention, the process of the present invention further comprises preparing a polypropylene random copolymer base stock according to the process described above.
According to the invention, the mixing can be carried out in a twin-screw extruder, and therefore, the mixing is preferably carried out in the following manner: and (3) putting the mixture containing the polypropylene random copolymer base material, the degrading agent, the antioxidant and the halogen absorbent into a double-screw extruder to enable the polypropylene random copolymer to generate free radical degradation reaction.
Wherein the twin screw extruder comprises a plurality of temperature control sections. Generally, the temperature of each section of the twin-screw extruder is controlled within the range of 180-220 ℃, more preferably, the temperature of the first section is 180-210 ℃, the temperature of the second section is 195-215 ℃, the temperature of the third section is 195-220 ℃, the temperature of the fourth section is 195-220 ℃, the temperature of the fifth section is 195-220 ℃ and the temperature of the sixth section is 195-215 ℃. The twin-screw extruder has a (main) rotational speed of 200 to 600rpm, preferably 250 to 400rpm.
The invention also relates to the propane-butadiene random copolymerization polypropylene prepared by the method.
The present invention will be described in detail below by way of examples. In the following examples, antioxidant B501W is a Pasteur IRGANOX B501W product; the double-screw extruder is a GLS-30B plastic granulator of Suzhou Congrale rubber and plastic machinery Limited company;
the relevant data in the examples were obtained according to the following test methods:
(1) butene and ethylene content in the polymer: measuring by adopting an infrared spectrum method;
(2) polymer room temperature xylene solubles content (XS): measured according to ASTM D5492;
(3) melt index (melt index, MFR): measured according to GB/T3682-2000, using a melt index apparatus model 7026 from CEAST, at 230 ℃ under a load of 2.16 kg;
(4) flexural modulus: measured according to GB/T9341-2008;
(5) tensile strength: measured according to GB/T1040.1-2006;
(6) molecular weight distribution (Mw/Mn): measured by PL-GPC 220 gel permeation chromatography of Polymer Laboratories, UK;
(7) yellow index: measured according to GB/T2409-1980;
(8) melting temperature: the measurement was carried out in accordance with GB/T19466.3-2004 using a differential scanning calorimeter model DSC-7 from Perkin-Elmer.
Example 1
A polymerization stage:
the base material of the propylene-butadiene copolymer polypropylene of the invention is carried out on a 25kg/h scale loop polypropylene pilot plant. The device mainly comprises a pre-complexing reactor, a pre-polymerization reactor, a loop reactor and a flash tank.
(1) Pre-complexing and pre-polymerizing
The flow rate of the main catalyst (HR catalyst, supplied by Beijing Odada division of China petrochemical catalyst Co., ltd.) was 0.8g/HR, the flow rate of the cocatalyst (triethylaluminum, TEA) was 6.3g/HR, the flow rate of the external electron donor (cyclohexylmethyldimethoxysilane, CHMMS) was 1.05g/HR, and the pre-complexing (contact) reaction was carried out at 6 ℃ for 8min.
And continuously adding the catalyst system after the pre-complexation into a continuous stirring tank type prepolymerization reactor, and carrying out prepolymerization reaction under the environment of a propylene liquid phase body, wherein the temperature is 15 ℃, the retention time is about 12min, and the prepolymerization multiple of the catalyst is about 160 times under the condition.
(2) Propylene polymerization
Continuously introducing the prepolymerized catalyst into a loop reactor to perform propylene polymerization reaction, wherein the temperature of the loop polymerization reaction is 70 ℃, the reaction pressure is 4MPa, 1-butene and hydrogen are added into propylene feed of the loop reactor, the molar concentrations of the 1-butene and the hydrogen detected by online chromatography are respectively about 11.5 percent and 750ppm, the retention time is 1h, and the reactor discharges to a flash tank; the operating temperature of the flash tank is 70 ℃, the operating pressure is 1.8MPa, the polymer powder A (the low-melting-index polypropylene random copolymer base material) is finally obtained after separation, and the molecular weight distribution, the butene content and the melting index of the polymer powder A are tested.
The polymerization parameters and the data of the results of the tests are shown in Table 1.
And (3) a granulation stage:
100 parts by weight of polymer powder A, 0.053 part by weight of a degradation agent (2, 5-dimethyl-2, 5 bis (t-butylperoxy) hexane), 0.2 part by weight of an antioxidant (1790, 168=1 (g/g)) and 0.05 part by weight of a halogen absorbent (calcium stearate) were blended, and after blending, the blend was extruded and pelletized by a twin-screw extruder to obtain polymer pellets B (propylbutane random copolymer polypropylene), and the molecular weight distribution and melt index of the polymer pellets B were measured. The rotation speed of the screw extruder is 350rpm, and the temperatures of the first section to the sixth section are respectively 200 ℃, 210 ℃, 215 ℃ and 210 ℃.
The polymer pellet test results are shown in table 2.
Example 2
A polymerization stage: same as example 1
And (3) a granulation stage: 100 parts by weight of polymer powder A, 0.051 part by weight of a degrading agent (dicumyl peroxide), 0.3 part by weight of an antioxidant (B501W) and 0.04 part by weight of a halogen absorbent (zinc stearate) are blended, and after blending, a double-screw extruder is used for extrusion and granulation to obtain polymer granules B (propyl-butyl random copolymer polypropylene), and parameters such as molecular weight distribution, melt index and the like are tested. The rotation speed of the screw extruder is 350rpm, and the temperatures of the first section to the sixth section are respectively 200 ℃, 215 ℃, 205 ℃ and 210 ℃.
Example 3
A polymerization stage: same as example 1
And (3) a granulation stage: 100 parts by weight of polymer powder A, 0.05 part by weight of a degradation agent (3, 6, 9-triethyl-3, 6, 9-trimethyl-1, 4, 7-triperoxonane), 0.25 part by weight of an antioxidant (1024 168= 2). The rotation speed of the screw extruder was 350rpm, and the temperatures of the first to sixth stages were 205 ℃, 210 ℃, 215 ℃, 210 ℃ respectively.
Example 4
A polymerization stage: same as example 1
And (3) a granulation stage: the same as example 1, except that antioxidant 1790 was changed to antioxidant 1010 at the granulation stage, and the addition amount and the ratio were unchanged.
Example 5
A polymerization stage: the same as in example 1, except that the amount of 1-butene added was adjusted during the polymerization and the molar concentration of 1-butene measured by on-line chromatography was 7%.
And (3) a granulation stage: the same as in example 1.
Example 6
A polymerization stage: the same as in example 1, except that the amount of 1-butene added was adjusted during the polymerization and the molar concentration of 1-butene measured by on-line chromatography was 14%.
And (3) a granulation stage: the same as in example 1.
Example 7
A polymerization stage: the same as in example 1, except that the amount of hydrogen added was adjusted in the course of polymerization, the molar concentration of hydrogen as measured by on-line chromatography was 1050ppm.
And (3) a granulation stage: the same as in example 1, except that the amount of the degradation agent added was adjusted to 0.038 parts by weight.
Example 8
The preparation of propylene-butadiene random copolymer polypropylene was conducted in accordance with the procedure of example 1, except that the antioxidant was a mixture of antioxidant 3114, antioxidant 330 and antioxidant 168 in a weight ratio of 1:1:1.
comparative example 1
A polymerization stage: the same as example 1, except that the polymerization process was carried out by replacing 1-butene with ethylene and carrying out propylene ethylene random polymerization, the molar concentrations of ethylene and hydrogen measured by on-line chromatography were about 2.54% and 750ppm, respectively.
And (3) a granulation stage: the same as in example 1, except that the degrading agent was added in an amount of 0.062 parts by weight. In experiments, it is found that if the addition amount of the degradation agent is less than 0.062 parts by weight, the melt index of the obtained propylene-ethylene random copolymer polypropylene is significantly less than 35.5g/10min.
Comparative example 2
Homopolypropylene was prepared according to the method of comparative example 1, except that homopolymerization of propylene was carried out without adding 1-butene during the polymerization, and the degradation agent was added in an amount of 0.062 part by weight at the time of granulation.
Comparative example 3
A comparative test was carried out on commercially available homo-polypropylene Y35 (Luoyang division, petrochemical Co., ltd., china).
Comparative example 4
A comparison test was carried out on commercially available polypropylene Y35XB (ChangLing division, petrochemical Co., ltd., china).
TABLE 1
TABLE 2
The molecular weight distribution of the degraded polypropylene is less than 2.8, which is obviously less than the molecular weight distribution of the commercially available Y35 and Y35XB materials, and the melting temperature is less than 150 ℃, which is lower than the melting temperature of homopolymerization products such as Y35 and the like by more than 10 ℃, thus effectively reducing the processing energy consumption.
As can be seen from the results of example 1 and comparative example 1, the tensile strength of the degraded polypropylene is more than 27MPa, which is significantly larger than that of the degraded polypropylene. The content of xylene solubles in the polypropylene random copolymer of propylene and ethylene is obviously lower than that of the polypropylene random copolymer of propylene and ethylene. Degrading to obtain the final product with the same melt index, wherein the dosage of the degrading agent used by the polypropylene random is 85.5 percent of that of the homo-polypropylene degrading agent, and the dosage of the degrading agent is obviously reduced.
Further spinning experimental results (not shown) show that the obtained polypropylene random copolymer fiber material has good spinnability, and under the same spinning process, the non-woven fabric produced by the polypropylene random copolymer fiber material has softer touch compared with a homopolymerization product, and is equivalent to the performance of an ethylene propylene random product.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including various technical features being combined in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (9)
1. A process for preparing a polypropylene random copolymer comprising: mixing the polypropylene base material with a degrading agent, an antioxidant and a halogen absorbent; wherein the degrading agent is used in an amount of 0.03 to 0.055 parts by weight, relative to 100 parts by weight of the propane-butene random copolymer polypropylene base material, and the degrading agent is selected from at least one of 2, 5-dimethyl-2, 5-bis (t-butylperoxy) hexane, dicumyl peroxide, and 3,6, 9-triethyl-3, 6, 9-trimethyl-1, 4, 7-triperoxonane.
2. The method of claim 1, wherein the antioxidant is used in an amount of 0.04 to 0.4 parts by weight, and the halogen absorbent is used in an amount of 0.03 to 0.2 parts by weight.
3. The method of claim 1 or 2, wherein the antioxidant is selected from at least one of antioxidant 1010, antioxidant 1790, antioxidant B501W, antioxidant 1076, antioxidant 1024, antioxidant CA, and antioxidant 168.
4. The process according to claim 1 or 2, wherein the halogen absorber is hydrotalcite, a metal stearate.
5. The method of claim 4, wherein the halogen absorbent is selected from at least one of calcium stearate, zinc stearate, sodium stearate, and hydrotalcite.
6. The process according to claim 1, wherein the propylene-butylene random copolymer polypropylene base stock has a molecular weight distribution of < 4.5, a butylene content of 0.5 to 6mol% and a melt index at 230 ℃ under a 2.16kg load of 0.5 to 10g/10min.
7. The method of claim 1, wherein the mixing is by: and (3) putting the mixture containing the polypropylene random copolymer base material, the degrading agent, the antioxidant and the halogen absorbent into a double-screw extruder to enable the polypropylene random copolymer to generate free radical degradation reaction.
8. The process as claimed in claim 1 or 7, wherein the temperature of the sections of the twin-screw extruder is in the range of 180-220 ℃ and the rotation speed is 200-600rpm.
9. The process as claimed in claim 8, wherein the rotational speed of the twin-screw extruder in each stage is 250-400rpm.
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| CN109233113A (en) * | 2018-08-24 | 2019-01-18 | 大连兴辉化工有限公司 | A kind of atactic copolymerized polypropene and preparation method thereof using edman degradation Edman preparation |
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