CN114478880A - Method for producing high-melt index melt-blown polypropylene by adopting intermittent liquid phase method and high-melt index melt-blown polypropylene - Google Patents

Method for producing high-melt index melt-blown polypropylene by adopting intermittent liquid phase method and high-melt index melt-blown polypropylene Download PDF

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CN114478880A
CN114478880A CN202011148398.5A CN202011148398A CN114478880A CN 114478880 A CN114478880 A CN 114478880A CN 202011148398 A CN202011148398 A CN 202011148398A CN 114478880 A CN114478880 A CN 114478880A
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dimethoxypropane
polymerization
polypropylene
melt
propane
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杨芝超
杜亚锋
李�杰
张雅茹
仝钦宇
徐萌
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/04—Monomers containing three or four carbon atoms
    • C08F110/06—Propene
    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
    • D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
    • D01F6/02—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds
    • D01F6/04—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds from polyolefins
    • D01F6/06—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolymers obtained by reactions only involving carbon-to-carbon unsaturated bonds from polyolefins from polypropylene
    • D—TEXTILES; PAPER
    • D04—BRAIDING; LACE-MAKING; KNITTING; TRIMMINGS; NON-WOVEN FABRICS
    • D04H—MAKING TEXTILE FABRICS, e.g. FROM FIBRES OR FILAMENTARY MATERIAL; FABRICS MADE BY SUCH PROCESSES OR APPARATUS, e.g. FELTS, NON-WOVEN FABRICS; COTTON-WOOL; WADDING ; NON-WOVEN FABRICS FROM STAPLE FIBRES, FILAMENTS OR YARNS, BONDED WITH AT LEAST ONE WEB-LIKE MATERIAL DURING THEIR CONSOLIDATION
    • D04H1/00—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres
    • D04H1/40—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres from fleeces or layers composed of fibres without existing or potential cohesive properties
    • D04H1/54—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres from fleeces or layers composed of fibres without existing or potential cohesive properties by welding together the fibres, e.g. by partially melting or dissolving
    • D04H1/542—Adhesive fibres
    • D04H1/544—Olefin series
    • D—TEXTILES; PAPER
    • D04—BRAIDING; LACE-MAKING; KNITTING; TRIMMINGS; NON-WOVEN FABRICS
    • D04H—MAKING TEXTILE FABRICS, e.g. FROM FIBRES OR FILAMENTARY MATERIAL; FABRICS MADE BY SUCH PROCESSES OR APPARATUS, e.g. FELTS, NON-WOVEN FABRICS; COTTON-WOOL; WADDING ; NON-WOVEN FABRICS FROM STAPLE FIBRES, FILAMENTS OR YARNS, BONDED WITH AT LEAST ONE WEB-LIKE MATERIAL DURING THEIR CONSOLIDATION
    • D04H1/00—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres
    • D04H1/40—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres from fleeces or layers composed of fibres without existing or potential cohesive properties
    • D04H1/54—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres from fleeces or layers composed of fibres without existing or potential cohesive properties by welding together the fibres, e.g. by partially melting or dissolving
    • D04H1/56—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres from fleeces or layers composed of fibres without existing or potential cohesive properties by welding together the fibres, e.g. by partially melting or dissolving in association with fibre formation, e.g. immediately following extrusion of staple fibres

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Abstract

The invention belongs to the field of olefin polymerization, and relates to a method for producing high-melt index melt-blown polypropylene by adopting an intermittent liquid phase method and the high-melt index melt-blown polypropylene. The method comprises the following steps: 1) putting hydrogen, propylene, propane and a catalyst into a polymerization kettle; 2) after the feeding is finished, heating the polymerization kettle to a preset polymerization temperature to carry out polymerization reaction; 3) after the polymerization reaction is finished, reducing the pressure of the polymerization kettle, vaporizing unreacted propylene and propane in the polymerization kettle, condensing the obtained gas phase into a liquid phase material through a condenser, and feeding the liquid phase material into a recovery tank; 4) and after recovery, spraying the materials in the polymerization kettle into a flash tank by utilizing the residual pressure in the polymerization kettle to obtain flash gas and polypropylene powder, and discharging the polypropylene powder after discharging the flash gas to obtain the high-melting index melt-blown fabric polypropylene. The method of the invention effectively solves the problem that polypropylene production factories are difficult to produce high-melt index melt-blown polypropylene by using common Ziegler-Natta catalysts.

Description

Method for producing high-melt index melt-blown polypropylene by adopting intermittent liquid phase method and high-melt index melt-blown polypropylene
Technical Field
The invention belongs to the field of olefin polymerization, and particularly relates to a method for producing high-melt-blown polypropylene by a batch liquid phase method, and the high-melt-blown polypropylene prepared by the method.
Background
The melt-blown cloth can be used for filter materials, isolating materials, oil absorption materials, wiping cloth and the like, and is the most core material of the mask. The melt-blown fabric mainly takes polypropylene as a raw material and is composed of superfine fibers, and the diameter of the fibers can reach 1-5 microns. The polypropylene used for the melt-blown fabric is polypropylene with a relatively high melt index, generally more than 1200g/10min, the larger the value, the smaller the molecular weight, the better the processing fluidity of the material, the finer the melt-blown fiber, and the better the filterability of the manufactured melt-blown fabric.
A process for preparing the high-smelting-index polypropylene resin features that the conventional polypropylene is degraded under control to lower its molecular weight and increase smelting index. The polypropylene and the degradation agent such as organic peroxide react in a screw extruder, so that the molecular chain of the polypropylene is broken to reduce the molecular weight of the polypropylene. The preparation process has the advantages of simplicity, convenience, easy operation, good melt fluidity of products, narrow molecular weight distribution, low ash content and the like, and is easy to carry out large-scale industrial production. This is also the method most adopted by manufacturers of modified plastics. However, in this method, decomposition products of the degradation agent such as organic peroxide remain in the polypropylene meltblown, giving odor to the resin and the final meltblown, and deteriorating the stability of polypropylene.
CN202010509795.4 discloses a melt-blown polypropylene composition, a preparation method and application thereof. The melt-blown polypropylene composition comprises the following components in parts by weight: 90-99 parts of polypropylene resin, 0.5-10 parts of fiber-forming adjusting master batch and 0.1-1 part of free radical initiator, wherein the fiber-forming adjusting master batch comprises 30-90 parts of polypropylene resin, 5-35 parts of hyperbranched associative polymer and 5-35 parts of interfacial barrier agent by weight. The melt-blown non-woven fabric fibers produced by the melt-blown polypropylene composition prepared by the invention have uniform diameter, good hand feeling and bulkiness, and simultaneously have good filtration rate, and the safety of the mask is effectively improved. The free radical initiator adopted by the invention is organic peroxide, so the melt-blown polypropylene does not solve the problem caused by the residue of the decomposition product of the organic peroxide.
CN202010198891.1 discloses a melt-blown polypropylene and its preparation method and application, the raw materials of which include polypropylene resin, degradation agent, antioxidant and lubricant, the degradation agent is one or more of hydrogen peroxide, sodium percarbonate, ammonium percarbonate and carbamide peroxide, and also includes one or more of dibenzylidene sorbitol, aryl phosphate and nano amorphous silica as nucleating agent; the degradation agent and the nucleating agent respectively account for 0.05 to 0.5 percent of the mass percentage of the raw materials; the preparation method comprises the following steps: premixing the raw materials, stirring, and then selectively adding a deodorant; melting and granulating by an extruder to obtain the product; also discloses the application of the melt-blown polypropylene in the preparation of melt-blown non-woven fabrics, melt-blown filter elements and sound-absorbing cotton. The melt-blown polypropylene has the advantages of low odor, high electret charge stability and the like. The invention adopts the deodorant to solve the problem caused by the residue of the organic peroxide decomposer, has certain effect, but does not fundamentally eliminate harmful micromolecular substances in the polypropylene resin.
Another method for preparing high melt index polypropylene resin is to change the production process of polypropylene. Conventional Ziegler-Natta catalysts have inadequate hydrogen control properties and do not achieve such high melt indices in conventional polypropylene production processes. By using a metallocene catalyst instead of a conventional Ziegler-Natta catalyst, the process of increasing the hydrogen concentration reduces the molecular weight of the polymer and thus increases the melt index. The metallocene catalysts used in this process are very costly. In the continuous polypropylene production process, when producing high-melt-index polypropylene resin, switching from a common polypropylene product with a melt index of 3g/10min to high-melt-index polypropylene is needed; it is also necessary to switch from high melt index polypropylene to regular polypropylene after production is complete. The switching period in the production process is long, and the produced transition materials are more. At present, the scale of a typical continuous polypropylene production line in China is 20-30 ten thousand tons per year, the demand property of melt-blown polypropylene determines that the product is required by a small-batch order, and the transition material for producing the melt-blown polypropylene by the continuous polypropylene is far more than that of a target product. Due to the huge technical and economic obstacles, there are currently few continuous process polypropylene manufacturers that produce meltblown polypropylene.
Disclosure of Invention
Aiming at the problems, the invention provides a method for producing high-melt index melt-blown polypropylene and the high-melt index melt-blown polypropylene prepared by the method, and the method is an intermittent liquid phase method, and can effectively overcome the problems of poor hydrogen regulation performance of a catalyst and excessive transition materials in continuous polypropylene production.
The first aspect of the invention provides a method for producing high melt-blown polypropylene with high melt index by a batch liquid phase method, which comprises the following steps:
1) putting hydrogen, propylene, propane and a catalyst into a polymerization kettle;
2) after the feeding is finished, heating the polymerization kettle to a preset polymerization temperature to carry out polymerization reaction;
3) after the polymerization reaction is finished, reducing the pressure of a polymerization kettle, vaporizing unreacted propylene and propane in the polymerization kettle, condensing the obtained gas phase into a liquid phase material by a solvent condenser, and feeding the liquid phase material into a solvent recovery tank;
4) and after recovery, spraying the materials in the polymerization kettle into a flash tank by utilizing the residual pressure in the polymerization kettle to obtain flash gas and polypropylene powder, and discharging the polypropylene powder after discharging the flash gas to obtain the high-melting index melt-blown fabric polypropylene.
A second aspect of the invention provides a high melt index meltblown polypropylene prepared by the above process.
The method for producing the high-melt-blown polypropylene effectively solves the problem that polypropylene production factories are difficult to produce the high-melt-blown polypropylene by using the commonly used Ziegler-Natta catalyst.
The method for producing the high-melt-index melt-blown polypropylene does not have the problem of excessive transition materials in continuous polypropylene production factories. Due to the batch liquid phase process, virtually no transition materials are produced by the process of the present invention.
The invention adopts the intermittent liquid phase bulk method production equipment as the existing equipment of the existing small bulk polypropylene production plant, and does not need to additionally increase and modify the equipment, so the method of the invention is easy to be popularized and implemented in the plant for producing polypropylene by using the intermittent liquid phase method.
The typical volume of a propylene polymerization kettle of a small bulk polypropylene production factory adopting the batch liquid phase bulk method is 12-26 cubic meters, and the normal production single batch yield is 2.8-6 tons. Therefore, the high melt index melt-blown fabric polypropylene product produced by the method is very suitable for meeting the characteristic that downstream melt-blown fabric manufacturers need small-batch goods. The melt-blown polypropylene has high production difficulty and high price, and the method can obviously improve the economic benefit of small-body polypropylene production factories.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
Exemplary embodiments of the present invention will be described in more detail by referring to the accompanying drawings.
FIG. 1 is a schematic view of a batch liquid phase bulk process production apparatus used in the process for producing high melt blown polypropylene according to the present invention.
1. A polymerization kettle; 2. a solvent condenser; 3. a solvent recovery tank; 4. a flash tank; 5. a gas holder.
a. Raw materials; b. nitrogen gas; c. polypropylene powder products.
Detailed Description
The following describes in detail specific embodiments of the present invention. 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 invention provides a method for producing high-melt-index melt-blown polypropylene by adopting an intermittent liquid phase method, which comprises the following steps:
1) putting hydrogen, propylene, propane and a catalyst into a polymerization kettle;
2) after the feeding is finished, heating the polymerization kettle to a preset polymerization temperature to carry out polymerization reaction;
3) after the polymerization reaction is finished, reducing the pressure of a polymerization kettle, vaporizing unreacted propylene and propane in the polymerization kettle, condensing the obtained gas phase into a liquid phase material by a solvent condenser, and feeding the liquid phase material into a solvent recovery tank;
4) and after recovery, spraying the materials in the polymerization kettle into a flash tank by utilizing the residual pressure in the polymerization kettle to obtain flash gas and polypropylene powder, and discharging the polypropylene powder after discharging the flash gas to obtain the high-melting index melt-blown fabric polypropylene.
According to the invention, propane and propylene are fed together, and the propane plays a role in diluting the propylene, namely reducing the ratio of the propylene, so that the hydrogen/propylene ratio of the system is improved, and the melt index of a polypropylene product is improved.
Therefore, the relative adding mass of the propane can be determined according to the expected value of the melt index of the polypropylene product, and specifically, in the step 1), the propane fed can account for 10 wt% to 99 wt% of the total mass of the propylene and the propane; preferably, the propane accounts for 20-95 wt% of the total mass of the propylene and the propane; more preferably, the propane accounts for 30 to 90 weight percent of the total mass of the propylene and the propane; more preferably, propane is 35 to 80 wt% based on the total mass of propylene and propane. In the present invention, propane may be fed alone or may be mixed with propylene and fed together.
According to the invention, in the step 2), the polymerization temperature is preferably 50-90 ℃, preferably 60-80 ℃, and more preferably 60-70 ℃; the pressure of the polymerization reaction is 2.3 to 3.8MPa, preferably 2.8 to 3.6 MPa. The temperature of the system is maintained within the above temperature range throughout the polymerization reaction.
According to a preferred embodiment of the present invention, the polymerizer is provided with a jacket for heating and heat-removing the polymerizer to control the polymerization temperature within a predetermined temperature range. Typically, warming the polymerization vessel is accomplished by passing hot water through the jacket of the polymerization vessel; heat removal from the polymerization vessel was achieved by feeding cold water to the jacket of the polymerization vessel. Specifically, in the heating process, a hot water pump is adopted to send hot water to a jacket of a polymerization kettle for heating and heating, and the kettle temperature is increased from normal temperature to polymerization temperature; when the temperature rises to the preset polymerization temperature, the hot water (which is gradually closed in an automatic state) is switched into circulating cooling water (the opening of a circulating cooling water valve is automatically adjusted), the heat released by the polymerization reaction is removed, and the reaction temperature is controlled to be stable.
According to the method of the invention, in the step 3), after the polymerization reaction is finished (generally, the polymerization time or the propylene conversion rate is required), the unreacted propylene and propane in the system are vaporized by reducing the pressure of the polymerization kettle, so as to realize the first step of separation and recovery, wherein the reduction of the pressure of the polymerization kettle is realized by opening a valve connecting the polymerization kettle and a recovery system (namely, opening the recovery system), and the recovery system comprises the solvent condenser and the solvent recovery tank. Usually, the solvent recovery tank is at room temperature, in the initial recovery stage, the gas phase in the polymerization kettle continuously enters the solvent recovery tank from the polymerization kettle, and after the gas phase is balanced, the recovery is finished. At this time, the residual pressure in the polymerization kettle is still remained, preferably, the residual pressure in the polymerization kettle is 0.8 to 1.8MPa, preferably 1.0 to 1.5 MPa.
In the step 3), the liquid phase material which enters the solvent recovery tank after vaporization and condensation is rich in propane, and the liquid phase material can be used as a polymerization raw material again after being added with propylene to be adjusted to a required concentration range.
In the step 4), the flash gas is discharged, so that the adsorption quantity of the combustible gas in the polypropylene powder is reduced, and the second step of separation and recovery is realized. Specific methods of discharging the flash gas: firstly, pressure relief is carried out to a gas holder: opening a valve between the flash tank and the gas holder to discharge gas in the flash tank into the gas holder, and reducing the pressure of the flash tank to the pressure of the gas holder; then, the flammable gas in the polypropylene powder is further reduced by adopting vacuum pumping or nitrogen replacement, and the pumped gas or the gas after nitrogen replacement also enters a gas cabinet. The gas in the gas holder is recycled or treated harmlessly according to small-body polypropylene production factory equipment. The vacuumizing time or the nitrogen replacement times are based on the standard that the content of combustible gas in the flash tank is qualified. And when the combustible gas content in the flash tank is qualified, discharging the polypropylene powder out of the flash tank, and feeding the polypropylene powder into a powder bin or packaging the polypropylene powder. And then, testing the powder product for melt index and the like, and grading the product according to the test result.
The catalyst of the present invention is not particularly limited, and may be any known polypropylene catalyst capable of polymerizing propylene, such as a metallocene catalyst or a Ziegler-Natta catalyst. The process of the present invention is particularly suitable for use with Ziegler-Natta catalysts, more preferably Ziegler-Natta catalysts with high stereoselectivity. The catalyst can prepare propylene polymer with isotactic index greater than 95%.
According to the method of the present invention, the Ziegler Natta catalyst having high stereoselectivity may be any of various catalysts commonly used in the art which are capable of catalyzing propylene to undergo isotactic polymerization. Generally, the ziegler natta catalyst with high stereoselectivity comprises: (1) the titanium-containing solid catalyst active component contains magnesium, titanium, halogen and an internal electron donor; (2) an organoaluminum compound co-catalyst component; and (3) optionally an external electron donor component.
According to a preferred embodiment of the present invention, the internal electron donor is at least one of diether compounds represented by formula I,
Figure BDA0002740434270000061
in the formula I, R1And R2Are the same or different and are each independently selected from C1-C20Straight chain alkyl group of (1), C3-C20Branched alkyl of C3-C20Cycloalkyl of, C6-C20Aryl of (C)7-C20Alkylaryl ofOr C7-C20Aralkyl group of (1); r3、R4、R5And R6Identical or different, each independently selected from hydrogen, halogen atom, C1-C20Straight chain alkyl group of (1), C3-C20Branched alkyl of C3-C20Cycloalkyl of, C6-C20Aryl of (C)7-C20Aralkyl or C7-C20Alkylaryl of, R3-R6Optionally linked to form a ring;
preferably, the diether compound is selected from the group consisting of 2- (2-ethylhexyl) -1, 3-dimethoxypropane, 2-isopropyl-1, 3-dimethoxypropane, 2-butyl-1, 3-dimethoxypropane, 2-sec-butyl-1, 3-dimethoxypropane, 2-cyclohexyl-1, 3-dimethoxypropane, 2-phenyl-1, 3-dimethoxypropane, 2- (2-phenylethyl) -1, 3-dimethoxypropane, 2- (2-cyclohexylethyl) -1, 3-dimethoxypropane, 2- (p-chlorophenyl) -1, 3-dimethoxypropane, 2- (diphenylmethyl) -1, 3-dimethoxypropane, 2-dicyclohexyl-1, 3-dimethoxypropane, 2-dicyclopentyl-1, 3-dimethoxypropane, 2-diethyl-1, 3-dimethoxypropane, 2-dipropyl-1, 3-dimethoxypropane, 2-diisopropyl-1, 3-dimethoxypropane, 2-dibutyl-1, 3-dimethoxypropane, 2-methyl-2-propyl-1, 3-dimethoxypropane, 2-methyl-2-benzyl-1, 3-dimethoxypropane, 2-methyl-2-ethyl-1, 3-dimethoxypropane, 2-dimethyl-2-propyl-dimethoxypropane, 2-dimethyl-propyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-2-propyl-dimethoxypropane, 2-propyl-dimethyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-1, 2-dimethyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-1, 2-dimethyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-dimethyl-1, 2-dimethyl-propyl-dimethyl-propyl, 2, and the same, 2, 2-methyl-2-isopropyl-1, 3-dimethoxypropane, 2-methyl-2-phenyl-1, 3-dimethoxypropane, 2-methyl-2-cyclohexyl-1, 3-dimethoxypropane, 2-bis (2-cyclohexylethyl) -1, 3-dimethoxypropane, 2-methyl-2-isobutyl-1, 3-dimethoxypropane, 2-methyl-2- (2-ethylhexyl) -1, 3-dimethoxypropane, 2-diisobutyl-1, 3-dimethoxypropane, 2-diphenyl-1, 3-dimethoxypropane, 2-dibenzyl-1, 3-dimethoxypropane, 2-bis (cyclohexylmethyl) -1, 3-dimethoxypropane, 2-isobutyl-2-isopropyl-1, 3-dimethoxypropane, 2- (1-methylbutyl) -2-isopropyl-1, 3-dimethoxypropane, 2-isopropyl-2-isoamyl-1, 3-dimethoxypropane, 2-phenyl-2-isopropyl-1, 3-dimethoxypropane, 2-phenyl-2-sec-butyl-1, 3-dimethoxypropane, 2-benzyl-2-isopropyl-1, 3-dimethoxypropane, 2-cyclopentyl-2-isopropyl-1, at least one of 3-dimethoxypropane, 2-cyclopentyl-2-sec-butyl-1, 3-dimethoxypropane, 2-cyclohexyl-2-isopropyl-1, 3-dimethoxypropane, 2-cyclohexyl-2-sec-butyl-1, 3-dimethoxypropane, 2-isopropyl-2-sec-butyl-1, 3-dimethoxypropane, 2-cyclohexyl-2-cyclohexylmethyl-1, 3-dimethoxypropane and 9, 9-bis (methoxymethyl) fluorene; preferably 2-isopropyl-2-isoamyl-1, 3-dimethoxypropane, 9-bis (methoxymethyl) fluorene, 2-isobutyl-2-isopropyl-1, 3-dimethoxypropane, 2-dicyclopentyl-1, 3-dimethoxypropane, 2-diphenyl-1, 3-dimethoxypropane, 2-diisobutyl-1, 3-dimethoxypropane; further preferably 2-isopropyl-2-isopentyl-1, 3-dimethoxypropane and/or 9, 9-bis (methoxymethyl) fluorene.
Specific examples of such active solid catalyst-containing components that may be used are disclosed in CN85100997, CN98126383.6, CN98111780.5, CN98126385.2, CN93102795.0, CN00109216.2, CN99125566.6, CN99125567.4, CN 02100900.7.
The organoaluminum compound which is the cocatalyst component of the catalyst is preferably an alkylaluminum compound, more preferably a trialkylaluminum, including in particular but not limited to: trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-butylaluminum, trioctylaluminum, etc.), diethylaluminum monochloride, diisobutylaluminum monochloride, ethylaluminum dichloroide, and ethylaluminum dichloroide.
The external electron donor compound as optional catalyst component is preferably an organosilicon compound having the general formula RnSi(OR')4-nWherein 0 < n.ltoreq.3, wherein R and R' are the same or different and are each independently selected from alkyl, cycloalkyl, aryl and haloalkyl groups, and R may also be halogen or hydrogen atom. Specifically, the organosilicon compound may be, but is not limited to: tetramethoxysilane, tetraethoxysilane, trimethylmethoxysilane, trimethylethoxysilane, trimethylphenoxysilane, dimethyldimethoxysilane, dimethyldiethoxysilane, methyl-tert-butyldimethoxysilane, methylisopropyldimethoxysilaneAn alkane, diphenoxydimethoxysilane, diphenyldiethoxysilane, phenyltrimethoxysilane, phenyltriethoxysilane, vinyltrimethoxysilane, cyclohexylmethyldimethoxysilane, dicyclopentyldimethoxysilane, diisopropyldimethoxysilane, diisobutyldimethoxysilane, 2-ethylpiperidinyl-2-t-butyldimethoxysilane, (1,1, 1-trifluoro-2-propyl) -2-ethylpiperidinyldimethoxysilane, (1,1, 1-trifluoro-2-propyl) -methyldimethoxysilane.
According to the present invention, the amount of each component of the Ziegler Natta catalyst can be any amount conventionally used in the art, and is not particularly limited in the present invention. For example, the ratio of the titanium-containing solid catalyst active component to the organoaluminum compound co-catalyst component is 1:25 to 1:1000 in terms of Ti/Al molar ratio. The ratio of the organoaluminum compound to the organosilicon compound can be 3:1 to 100:1, in terms of Al/Si molar ratio.
The amount of the catalyst used in the present invention is not particularly limited, and can be determined in accordance with the single pot yield and the catalyst activity. The addition amount of the hydrogen can increase the kettle pressure to 0.4-1.2 MPa.
The invention also provides the high melt index melt-blown polypropylene prepared by the method.
The present invention will be further described with reference to the following examples, but the scope of the present invention is not limited to these examples.
In the following examples and comparative examples, polypropylene catalysts comprising a main catalyst and a cocatalyst were used, wherein,
the main catalyst (active solid catalyst component containing titanium) is obtained by adopting the method described in example 1 in Chinese patent CN 201210426370.2. Specifically, after a 16L pressure-resistant reactor equipped with a stirrer was sufficiently replaced with nitrogen, 10L of ethanol, 300mL of 2-ethylhexanol, 11.2g of iodine, 8g of magnesium chloride and 640g of magnesium powder were charged into the reactor. The system is heated to 75 ℃ while stirring, and the reflux reaction is carried out until no hydrogen is discharged. The reaction was stopped, washed with 3L of ethanol, filtered and dried to obtain the magnesium alkoxide support. 650g of an alkoxy magnesium carrier, 3250mL of toluene and 65mL of 2-isopropyl-2-isoamyl-1, 3-dimethoxypropane were prepared as a suspension. Adding 2600mL of toluene and 3900mL of titanium tetrachloride into a 16L pressure-resistant reaction kettle repeatedly replaced by high-purity nitrogen, heating to 80 ℃, adding the prepared suspension into the kettle, keeping the temperature for 1 hour, adding 65mL of 2-isopropyl-2-isoamyl-1, 3-dimethoxypropane, slowly heating to 110 ℃, keeping the temperature for 2 hours, and performing pressure filtration to obtain a solid. The resulting solid was treated with a mixture of toluene 5070mL and titanium tetrachloride 3380mL at 110 ℃ for 1 hour with stirring, and then treated 3 times. And (4) performing filter pressing, washing the obtained solid with hexane for 4 times, and performing filter pressing and drying to obtain the catalyst solid component, wherein 6000mL of the solid is obtained each time.
The cocatalyst is triethyl aluminum, and is prepared into 1.0mol/L for use.
The experimental results in the examples were obtained according to the following test methods, which are all operated at room temperature environment without particular limitation:
melt index (MFR): measured according to GB/T3682.1-2018 at 230 ℃ under a load of 2.16 kg.
Isotacticity (II): determined according to the method described in GB/T2412-2008.
Xylene solubles content: determined according to GB/T24282-.
The following examples and comparative examples each employ a batch liquid phase bulk process production apparatus as shown in FIG. 1. The equipment comprises a polymerization kettle 1, a solvent condenser 2, a solvent recovery tank 3, a flash tank 4 and a gas holder 5, wherein the top of the polymerization kettle 1 is sequentially connected with the solvent condenser 2 and the solvent recovery tank 3, the bottom of the polymerization kettle 1 is connected with the flash tank 4, and the top of the flash tank 4 is connected with the gas holder 5; the raw material feeding pipeline is connected with the polymerization kettle 1, the nitrogen feeding pipeline is connected with the lower portion of the flash tank 4, a polypropylene powder product discharge pipeline is arranged at the bottom of the flash tank 4, the solvent condenser 2 and the solvent recovery tank 3 form a recovery system, and valves are arranged on the raw material feeding pipeline, the nitrogen feeding pipeline, the polypropylene powder product discharge pipeline, a pipeline between the polymerization kettle 1 and the recovery system, a pipeline between the polymerization kettle 1 and the flash tank 4, and a pipeline between the flash tank 4 and the gas holder 5. The polymerization vessel 1 had a volume of 5L and was externally provided with a jacket (not shown).
Example 1
Hydrogen was added to the polymerization vessel to raise the vessel pressure to 0.4MPa, and 21.7mg of a polypropylene procatalyst and 1.75ml of a triethylaluminum solution were charged into the polymerization vessel with a mixture of 1.0 liter of propylene and 1.0 liter of propane at room temperature. The temperature of the polymerization kettle is raised by jacket hot water of the polymerization kettle, and when the temperature of the polymerization kettle reaches 65 ℃, the flow of cooling water is adjusted according to the polymerization temperature of propylene, so that the polymerization temperature of the propylene is maintained to be stable at 65 ℃. At the moment, the gauge pressure of the polymerization kettle is increased to 3.1MPa, after the polymerization reaction is carried out for 34 minutes, a valve for connecting the polymerization kettle and a recovery system is opened, the pressure of the polymerization kettle is released, unreacted propylene and propane are vaporized in the polymerization kettle, the obtained gas phase is condensed into liquid phase material by a solvent condenser, the liquid phase material enters a solvent recovery tank, and when the kettle pressure is reduced to 1.5MPa, the recovery is stopped. Discharging gas and polypropylene powder in the kettle into a flash tank, opening a valve between the flash tank and a gas holder to discharge the gas in the flash tank into the gas holder, reducing the pressure of the flash tank to normal pressure, then filling nitrogen to 0.4MPa, then discharging the gas after nitrogen replacement into the gas holder, discharging the powder in the kettle and weighing after 3 times of nitrogen replacement, thus obtaining 374g of polypropylene powder. The polypropylene powder was tested and the results are shown in Table 1.
Example 2
Hydrogen was added to the polymerization vessel to raise the vessel pressure to 0.5MPa, and 22.5mg of a polypropylene procatalyst and 1.75ml of a triethylaluminum solution were charged into the polymerization vessel with a mixture of 1.3 liters of propylene and 0.7 liters of propane at room temperature. The temperature of the polymerization kettle is raised by jacket hot water of the polymerization kettle, and when the temperature of the polymerization kettle reaches 70 ℃, the flow of cooling water is adjusted according to the polymerization temperature of propylene, so that the polymerization temperature of the propylene is maintained to be stable at 70 ℃. At the moment, the gauge pressure of the polymerization kettle is increased to 3.7MPa, after the polymerization reaction is carried out for 60 minutes, a valve for connecting the polymerization kettle and a recovery system is opened, the pressure of the polymerization kettle is released, unreacted propylene and propane are vaporized in the polymerization kettle, the obtained gas phase is condensed into liquid phase material by a solvent condenser, the liquid phase material enters a solvent recovery tank, and when the kettle pressure is reduced to 1.5MPa, the recovery is stopped. Discharging gas and polypropylene powder in the kettle into a flash tank, opening a valve between the flash tank and a gas holder to discharge the gas in the flash tank into the gas holder, reducing the pressure of the flash tank to normal pressure, then filling nitrogen to 0.4MPa, then discharging the gas after nitrogen replacement into the gas holder, discharging the powder in the kettle and weighing after 3 times of nitrogen replacement, thus obtaining 264g of polypropylene powder. The polypropylene powder was tested and the results are shown in Table 1.
Example 3
Hydrogen was added to the polymerization vessel to raise the vessel pressure to 0.8MPa, and 11.3mg of a polypropylene procatalyst and 1.75ml of a triethylaluminum solution were charged into the polymerization vessel with a mixture of 0.6 liter of propylene and 1.4 liters of propane at room temperature. The temperature of the polymerization kettle is raised by jacket hot water of the polymerization kettle, and when the temperature of the polymerization kettle reaches 65 ℃, the flow of cooling water is adjusted according to the polymerization temperature of propylene, so that the polymerization temperature of the propylene is maintained to be stable at 65 ℃. At the moment, the gauge pressure of the polymerization kettle is increased to 3.6MPa, after the polymerization reaction is carried out for 60 minutes, a valve for connecting the polymerization kettle and a recovery system is opened, the pressure of the polymerization kettle is released, unreacted propylene and propane are vaporized in the polymerization kettle, the obtained gas phase is condensed into liquid phase material by a solvent condenser, the liquid phase material enters a solvent recovery tank, and when the kettle pressure is reduced to 1.5MPa, the recovery is stopped. Discharging gas and polypropylene powder in the kettle into a flash tank, opening a valve between the flash tank and a gas holder to discharge the gas in the flash tank into the gas holder, reducing the pressure of the flash tank to normal pressure, then filling nitrogen to 0.4MPa, then discharging the gas after nitrogen replacement into the gas holder, discharging the powder in the kettle and weighing after 3 times of nitrogen replacement, thus obtaining 165g of polypropylene powder. The polypropylene powder was tested and the results are shown in Table 1.
Example 4
Hydrogen was added to the polymerization vessel to raise the vessel pressure to 1.1MPa, and 15.4mg of a polypropylene procatalyst and 1.75ml of a triethylaluminum solution were charged into the polymerization vessel with a mixture of 0.8 liter of propylene and 1.2 liters of propane at room temperature. The temperature of the polymerization kettle is raised by jacket hot water of the polymerization kettle, and when the temperature of the polymerization kettle reaches 60 ℃, the flow of cooling water is adjusted according to the polymerization temperature of propylene, so that the polymerization temperature of the propylene is maintained to be stable at 60 ℃. At the moment, the gauge pressure of the polymerization kettle is increased to 3.6MPa, after the polymerization reaction is carried out for 60 minutes, a valve for connecting the polymerization kettle and a recovery system is opened, the pressure of the polymerization kettle is released, unreacted propylene and propane are vaporized in the polymerization kettle, the obtained gas phase is condensed into liquid phase material by a solvent condenser, the liquid phase material enters a solvent recovery tank, and when the kettle pressure is reduced to 1.5MPa, the recovery is stopped. Discharging gas in the kettle and the polypropylene powder into a flash tank, opening a valve between the flash tank and a gas holder to discharge the gas in the flash tank into the gas holder, reducing the pressure of the flash tank to normal pressure, then filling nitrogen to 0.4MPa, then discharging the gas after nitrogen replacement into the gas holder, discharging the powder in the kettle after nitrogen replacement is carried out for 3 times, and weighing to obtain 152g of polypropylene powder. The polypropylene powder was tested and the results are shown in Table 1.
Comparative example 1
Hydrogen was added to the polymerization vessel to raise the vessel pressure to 0.5MPa, and 10.7mg of a polypropylene main catalyst and 1.75ml of a triethylaluminum solution were charged into the polymerization vessel with 2.0 liters of propylene at room temperature. The temperature of the polymerization kettle is raised by jacket hot water of the polymerization kettle, and when the temperature of the polymerization kettle reaches 70 ℃, the flow of cooling water is adjusted according to the polymerization temperature of propylene, so that the polymerization temperature of the propylene is maintained to be stabilized at 70 ℃. At the moment, the gauge pressure of the polymerization kettle is increased to 3.8MPa, after the polymerization reaction is carried out for 60 minutes, a valve for connecting the polymerization kettle and a recovery system is opened, the pressure of the polymerization kettle is released, unreacted propylene is vaporized in the polymerization kettle, the obtained gas phase is condensed into liquid phase material by a solvent condenser, the liquid phase material enters a solvent recovery tank, and when the kettle pressure is reduced to 1.5MPa, the recovery is stopped. Discharging gas in the kettle and the polypropylene powder into a flash tank, opening a valve between the flash tank and a gas holder to discharge the gas in the flash tank into the gas holder, reducing the pressure of the flash tank to normal pressure, then filling nitrogen to 0.4MPa, then discharging the gas after nitrogen replacement into the gas holder, discharging the powder in the kettle and weighing after 3 times of nitrogen replacement, thus obtaining 470g of polypropylene powder. The polypropylene powder was tested and the results are shown in Table 1.
Comparative example 2
Hydrogen was added to the polymerization vessel to raise the vessel pressure to 0.8MPa, and 18.8mg of a polypropylene main catalyst and 1.75ml of a triethylaluminum solution were charged into the polymerization vessel with 2.0 liters of propylene at room temperature. The temperature of the polymerization kettle is raised by jacket hot water of the polymerization kettle, and when the temperature of the polymerization kettle reaches 65 ℃, the flow of cooling water is adjusted according to the polymerization temperature of propylene, so that the polymerization temperature of the propylene is maintained to be stable at 65 ℃. At the moment, the gauge pressure of the polymerization kettle is increased to 3.6MPa, after the polymerization reaction is carried out for 60 minutes, a valve for connecting the polymerization kettle and a recovery system is opened, the pressure of the polymerization kettle is released, unreacted propylene is vaporized in the polymerization kettle, the obtained gas phase is condensed into liquid phase material by a solvent condenser, the liquid phase material enters a solvent recovery tank, and when the kettle pressure is reduced to 1.5MPa, the recovery is stopped. Discharging gas and polypropylene powder in the kettle into a flash tank, opening a valve between the flash tank and a gas holder to discharge the gas in the flash tank into the gas holder, reducing the pressure of the flash tank to normal pressure, then filling nitrogen to 0.4MPa, then discharging the gas after nitrogen replacement into the gas holder, discharging the powder in the kettle and weighing after 3 times of nitrogen replacement, thus obtaining 445g of polypropylene powder. The polypropylene powder was tested and the results are shown in Table 1.
TABLE 1 analysis results of powder lot
Figure BDA0002740434270000131
Figure BDA0002740434270000141
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
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.

Claims (13)

1. A method for producing high-melt-index melt-blown polypropylene by adopting a batch liquid phase method is characterized by comprising the following steps:
1) putting hydrogen, propylene, propane and a catalyst into a polymerization kettle;
2) after the feeding is finished, heating the polymerization kettle to a preset polymerization temperature to carry out polymerization reaction;
3) after the polymerization reaction is finished, reducing the pressure of a polymerization kettle, vaporizing unreacted propylene and propane in the polymerization kettle, condensing the obtained gas phase into a liquid phase material by a solvent condenser, and feeding the liquid phase material into a solvent recovery tank;
4) and after recovery, spraying the materials in the polymerization kettle into a flash tank by utilizing the residual pressure in the polymerization kettle to obtain flash gas and polypropylene powder, and discharging the polypropylene powder after discharging the flash gas to obtain the high-melting index melt-blown fabric polypropylene.
2. The method according to claim 1, wherein in the step 1), the propane is fed in an amount of 10-99 wt% of the total mass of the propylene and the propane; preferably, the propane accounts for 20-95 wt% of the total mass of the propylene and the propane; more preferably, the propane accounts for 30 to 90 weight percent of the total mass of the propylene and the propane; more preferably, propane is 35 to 80 wt% based on the total mass of propylene and propane.
3. The process according to claim 1, wherein in step 2), the polymerization temperature is 50 to 90 ℃, preferably 60 to 80 ℃, more preferably 60 to 70 ℃; the pressure of the polymerization reaction is 2.3 to 3.8MPa, preferably 2.8 to 3.6 MPa.
4. The process as claimed in claim 1, wherein the polymerizer is provided with a jacket for heating and heat-removing the polymerizer to control the polymerization temperature within a predetermined temperature range.
5. The process of claim 1, wherein in step 3), the reducing the polymerizer pressure is achieved by opening a valve connecting the polymerizer with a recovery system comprising the solvent condenser and the solvent recovery tank.
6. The process of claim 1, wherein the liquid phase feed to the solvent recovery tank is optionally blended and returned to the polymerization vessel as a feed.
7. The method according to claim 1, wherein in the step 4), the residual pressure in the polymerization vessel is 0.8 to 1.8MPa, preferably 1.0 to 1.5 MPa.
8. The method as claimed in claim 1, wherein in the step 4), the flash gas is discharged by decompression to a gas holder and then vacuumization or nitrogen replacement is carried out; the pumped flash gas or the gas after nitrogen replacement enters a gas holder.
9. The method according to any of claims 1-8, wherein the catalyst is a Ziegler-Natta catalyst, preferably a Ziegler-Natta catalyst with high stereoselectivity.
10. The method according to claim 9, wherein the ziegler natta catalyst having high stereoselectivity comprises: (1) a titanium-containing solid catalyst active component containing magnesium, titanium, halogen and an internal electron donor; (2) an organoaluminum compound co-catalyst component; and (3) optionally an external electron donor component.
11. The method of claim 10, wherein the internal electron donor is at least one of diether compounds represented by formula I,
Figure FDA0002740434260000021
in the formula I, R1And R2Are the same or different and are each independently selected from C1-C20Straight chain alkane of (2)Base, C3-C20Branched alkyl of C3-C20Cycloalkyl of, C6-C20Aryl of (C)7-C20Alkylaryl or C of7-C20Aralkyl group of (1); r3、R4、R5And R6Identical or different, each independently selected from hydrogen, halogen atom, C1-C20Straight chain alkyl group of (1), C3-C20Branched alkyl of C3-C20Cycloalkyl of (C)6-C20Aryl of (C)7-C20Aralkyl or C7-C20Alkylaryl of, R3-R6Optionally linked to form a ring;
preferably, the diether compound is selected from the group consisting of 2- (2-ethylhexyl) -1, 3-dimethoxypropane, 2-isopropyl-1, 3-dimethoxypropane, 2-butyl-1, 3-dimethoxypropane, 2-sec-butyl-1, 3-dimethoxypropane, 2-cyclohexyl-1, 3-dimethoxypropane, 2-phenyl-1, 3-dimethoxypropane, 2- (2-phenylethyl) -1, 3-dimethoxypropane, 2- (2-cyclohexylethyl) -1, 3-dimethoxypropane, 2- (p-chlorophenyl) -1, 3-dimethoxypropane, 2- (diphenylmethyl) -1, 3-dimethoxypropane, 2-dicyclohexyl-1, 3-dimethoxypropane, 2-dicyclopentyl-1, 3-dimethoxypropane, 2-diethyl-1, 3-dimethoxypropane, 2-dipropyl-1, 3-dimethoxypropane, 2-diisopropyl-1, 3-dimethoxypropane, 2-dibutyl-1, 3-dimethoxypropane, 2-methyl-2-propyl-1, 3-dimethoxypropane, 2-methyl-2-benzyl-1, 3-dimethoxypropane, 2-methyl-2-ethyl-1, 3-dimethoxypropane, 2-dimethyl-2-propyl-dimethoxypropane, 2-dimethyl-propyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-2-propyl-dimethoxypropane, 2-propyl-dimethyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-1, 2-dimethyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-1, 2-dimethyl-1, 3-dimethoxypropane, 2-dimethyl-propyl-dimethyl-1, 2-dimethyl-propyl-dimethyl-propyl, 2, and the same, 2, 2-methyl-2-isopropyl-1, 3-dimethoxypropane, 2-methyl-2-phenyl-1, 3-dimethoxypropane, 2-methyl-2-cyclohexyl-1, 3-dimethoxypropane, 2-bis (2-cyclohexylethyl) -1, 3-dimethoxypropane, 2-methyl-2-isobutyl-1, 3-dimethoxypropane, 2-methyl-2- (2-ethylhexyl) -1, 3-dimethoxypropane, 2-diisobutyl-1, 3-dimethoxypropane, 2-diphenyl-1, 3-dimethoxypropane, 2-dibenzyl-1, 3-dimethoxypropane, 2-bis (cyclohexylmethyl) -1, 3-dimethoxypropane, 2-isobutyl-2-isopropyl-1, 3-dimethoxypropane, 2- (1-methylbutyl) -2-isopropyl-1, 3-dimethoxypropane, 2-isopropyl-2-isoamyl-1, 3-dimethoxypropane, 2-phenyl-2-isopropyl-1, 3-dimethoxypropane, 2-phenyl-2-sec-butyl-1, 3-dimethoxypropane, 2-benzyl-2-isopropyl-1, 3-dimethoxypropane, 2-cyclopentyl-2-isopropyl-1, at least one of 3-dimethoxypropane, 2-cyclopentyl-2-sec-butyl-1, 3-dimethoxypropane, 2-cyclohexyl-2-isopropyl-1, 3-dimethoxypropane, 2-cyclohexyl-2-sec-butyl-1, 3-dimethoxypropane, 2-isopropyl-2-sec-butyl-1, 3-dimethoxypropane, 2-cyclohexyl-2-cyclohexylmethyl-1, 3-dimethoxypropane and 9, 9-bis (methoxymethyl) fluorene; preferably at least one of 2-isopropyl-2-isoamyl-1, 3-dimethoxypropane, 9-bis (methoxymethyl) fluorene, 2-isobutyl-2-isopropyl-1, 3-dimethoxypropane, 2-dicyclopentyl-1, 3-dimethoxypropane, 2-diphenyl-1, 3-dimethoxypropane and 2, 2-diisobutyl-1, 3-dimethoxypropane; further preferably 2-isopropyl-2-isopentyl-1, 3-dimethoxypropane and/or 9, 9-bis (methoxymethyl) fluorene.
12. The process of claim 10, wherein the ratio of the titanium-containing solid catalyst active component to the organoaluminum compound co-catalyst component is from 1:25 to 1:1000 in terms of Ti/Al molar ratio.
13. A high melt index meltblown polypropylene produced by the process of any of claims 1-12.
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