CN101195669B - Method for producing partial fluorine ethylene polymer - Google Patents
Method for producing partial fluorine ethylene polymer Download PDFInfo
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- CN101195669B CN101195669B CN200610119030XA CN200610119030A CN101195669B CN 101195669 B CN101195669 B CN 101195669B CN 200610119030X A CN200610119030X A CN 200610119030XA CN 200610119030 A CN200610119030 A CN 200610119030A CN 101195669 B CN101195669 B CN 101195669B
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Abstract
The invention relates to a preparation method of vinylidene fluoride polymer, which comprises (a), providing vinylidene fluoride and aqueous dispersion of any comonomer, (b), adding chain transfer agent and initiator of initial quantity, to process polymerization at the reaction pressure of 2-5MPa and temperature of 60-120DEG C, (c), adding left initiator in turn as following (i) when the ratio of initial quantity is lower than 10mass%, the left amount is added uniformly in 10 times, (ii) when the ratio of initial quantity is 10-30mass%, the left amount is added uniformly in 4 times, (iii) when the ratio of initial quantity is 30-50mass%, the left amount is added uniformly in 2 times, (iv) when the ratio of initial quantity is higher than 50mass%, the left amount is added in one time.
Description
Technical field
The present invention relates to a kind of vinylidene fluoride homopolymer or multipolymer and preparation method thereof.
Background technology
In the polymerization process of vinylidene, in order to obtain polyvinylidene fluoride homopolymer or the multipolymer that certain molecular weight and/or certain molecular weight distribute, method commonly used is the consumption or the adding mode of control initiator, chain-transfer agent.
U.S. Pat 4,076,929 have described a kind of use ditertiary butyl peroxide (being called for short DTBP) as initiator, at high temperature carries out method of emulsion polymerization.It adds earlier partial monosomy and initiator, after question response begins, then adds monomer and initiator continuously with certain speed, when the monomer that adds reach required adding monomer total amount 50% after, stop to add initiator.What it finally obtained is a kind of polyvinylidene difluoride (PVDF) product of bimodal distribution.Wherein high-molecular weight partly accounts for 30～70%.The polyvinylidene difluoride (PVDF) (PVDF) that makes by this method has the molecular weight distribution of non-constant width.
U.S. Pat 5,095,081 discloses a kind of polymerization process that in batches adds chain-transfer agent, and it adds monomer and whole initiator of part at the beginning of reaction, and the every increase by 10% of subsequent transformation rate just adds a part of chain-transfer agent.Can make the narrower polyvinylidene difluoride (PVDF) product of molecular weight distribution by this method, it has high-mechanical property and high thermo-chemical stability.
U.S. Pat 4,569,978 to disclose a kind of be the emulsion polymerisation process of molecular weight regulator with the trichloromethane, its main polymerization process is to add partial monosomy so that pressure reaches reaction pressure at the beginning of reaction, add a part of chain-transfer agent and initiator subsequently, remaining chain-transfer agent and initiator add along with vinylidene (VDF) monomer according to given pace.Can obtain the polyvinylidene difluoride (PVDF) product of different melt viscosities by the add-on of regulating chain-transfer agent and initiator.Can make medium and polyvinylidene difluoride (PVDF) product low melting viscosity by this kind method.
Chinese patent CN1583809A discloses a kind of vinylidene polymerization process, and its main characteristic is to add partial monosomy at the beginning of the reaction.Add whole chain-transfer agents and a part of organic initiators afterwards, reaction starts the back and further adds initiator, when the transformation efficiency of polyreaction reaches 2～65%, stops to add initiator.It has and US 4,076 929 similar bimodal distributions the polyvinylidene difluoride (PVDF) product that obtains by this method.
Though prior art is by control initiator, the consumption of chain-transfer agent or the polyvinylidene difluoride (PVDF) that the adding mode can obtain having certain molecular weight and/or molecular weight distribution, but still need to develop a kind of new polymerization process, use this method guaranteeing obtaining vinylidene fluoride homopolymer unimodal or bimodal, moderate molecular weight distribution or multipolymer under the prerequisite of required weight-average molecular weight.
The content of invention
An object of the present invention is to provide a kind of polymerization process, this method can guarantee to obtain vinylidene fluoride homopolymer unimodal or bimodal, moderate molecular weight distribution or multipolymer under certain weight-average molecular weight condition.
Another object of the present invention provides vinylidene fluoride homopolymer or the multipolymer that is applicable to film field and electric field.
Therefore, one aspect of the present invention provides a kind of preparation method of partial fluorine ethylene polymer, and it comprises the steps:
(a) provide the water dispersion of vinylidene with other comonomer of choosing wantonly;
(b) add chain-transfer agent and a part of initiator in described water dispersion, be controlled at 2～5MPa in reaction pressure, temperature is controlled at carries out polyreaction under 60～120 ℃;
(c) add the initiator of surplus as follows in batches:
(i) if initial add-on W
0Proportion is lower than 10 weight %, and then remainder divides average the adding 10 times;
If (ii) initial add-on W
0Proportion is between 10～30 weight %, and then remainder divides average the adding 4 times;
If (iii) initial add-on W
0Proportion is between 30～50 weight %, and then remainder divides average the adding 2 times;
If (iv) initial add-on W
0Proportion is higher than 50 weight %, then the adding of 1 property of remainder;
(d) after reaction finishes, reclaim all unreacted monomers.
Another aspect of the present invention provides the polyvinylidene difluoride (PVDF) that a kind of vinylidene content is not less than 80 moles of %, its melt flow rate (MFR) 0.1～20g/10min, between primary particle diameter 0.1～1um, weight-average molecular weight is 40～120 myriagram/moles, and the molecular weight distribution coefficient is 1.5～4.
Embodiment
The invention provides a kind of preparation method of partial fluorine ethylene polymer, described partial fluorine ethylene polymer can be the homopolymer of vinylidene or the multipolymer that vinylidene content is not less than the vinylidene of 80 moles of %.
The comonomer that is applicable to the present invention and vinylidene copolymerization is without particular limitation, it can be selected from the vinyl compound that can carry out free radical or ionic copolymerization with vinylidene, for example, described comonomer can be the comonomer that is connected with a fluorine atom on the vinyl at least, contains fluoroalkyl or fluoroalkoxy, the example of described comonomer can referring to, Chinese patent CN1583809 (see its page 3 14～18 row) for example, the document is inserted this paper as the part of specification sheets of the present invention by reference.
In a better example of the present invention, the indefiniteness example of described comonomer has, for example vinyl fluoride, trifluoro-ethylene, trifluorochloroethylene, tetrafluoroethylene, 3,3,3-trifluoro propene, R 1216, perfluoroalkyl vinyl ether: as perfluoro methyl vinyl ether, perfluoroethylvinyl ether, perfluor (2,2-dimethyl-1,3-Dloxole diene) or two kinds or multiple above-mentioned monomeric mixture.
The method that the present invention prepares partial fluorine ethylene polymer comprises the step that forms the vinylidene and the water dispersion of other comonomer of choosing wantonly.The method that is used to form the monomer aqueous dispersions is without particular limitation, and it can be any ordinary method of this area.For example, letex polymerization, suspension polymerization.
In order to improve the dispersiveness of monomer in water, also can in dispersion system, add dispersion agent.Described dispersion agent is without particular limitation, if can make monomer disperse form homogeneous dispersion and do not influence subsequently polyreaction or the final performance of the polymkeric substance that makes of influence.In a better example of the present invention, described dispersion agent has general formula X C
nF
2nCOOM, wherein X is fluorine atom or hydrogen atom, and n is 4～12 integer, and M is hydrogen ion or alkalimetal ion or ammonium ion, be preferably, described dispersion agent is selected from perfluor caproic acid potassium, perfluor Sodium n-caproate, perfluor caproic acid ammonium, perfluor valeric acid potassium, perfluor natrium valericum, perfluor ammonium valerianate etc.
In the present invention, the add-on of dispersion agent is without particular limitation, if can make monomer disperse form homogeneous dispersion and do not influence subsequently polyreaction or the final performance of the polymkeric substance that makes of influence.In a better example of the present invention, by 100 weight parts monomers raw materials, the add-on of dispersion agent is 0.01～2 weight part, is preferably the 0.05-1.2 weight part, more preferably the 0.1-1.0 weight part.
In order to improve the stability of monomer dispersion liquid, also in order to prevent sticking wall, also can in described monomer dispersion liquid, add paraffin simultaneously.The add-on of paraffin does not have special restriction, as long as can make monomer liquid stable, wall sticking phenomenon does not take place and do not influence subsequently polyreaction or the final performance of the polymkeric substance that makes of influence get final product.In a better example of the present invention, by 100 weight parts monomers raw materials, the add-on of described paraffin is 0.1～5, is preferably 0.3～3.5, more preferably 0.5～2.5.
In the dispersion of the present invention, the content of comonomer should make in the final copolymer the unitary content of vinylidene fluoride monomers account for 80 moles of % or more than.In a better example of the present invention, by 100 molar part mix monomers, the content of comonomer is 0～20, is preferably 5～10 molar part.
The preparation method of partial fluorine ethylene polymer of the present invention also comprises subsequently to add chain-transfer agent and the part initiator step with initiated polymerization in reaction system.
Be applicable to that initiator of the present invention can be this area polymerization starter commonly used.Described initiator comprises no organic initiators and organic initiators:
No organic initiators mainly comprises Sodium Persulfate, Potassium Persulphate, ammonium persulphate or the like;
Organic initiators mainly comprises superoxide, the special pentyl ester of di-t-butyl peroxide (DTBP), peroxidation trimethylacetic acid uncle fourth fat or peroxidation trimethylacetic acid for example, and peroxycarbonates, for example peroxy dicarbonate diethyl ester, peroxy dicarbonate diisopropyl fat (IPP), peroxy dicarbonate di-n-propyl ester (NPP), peroxy dicarbonate two (4-tert-butylcyclohexyl) ester.
By 100 weight part vinylidene fluoride monomers or copolymerization mix monomer, the consumption of total initiator is 0.05～5 weight part, and the consumption of the initial initiator that adds accounts for the 10-60 weight % of total amount, is preferably 10-50 weight %, more preferably 10-40 weight %.
Be applicable to that chain-transfer agent of the present invention can be any compound that can continue the vinylidene polyreaction, for example, alcohols chain-transfer agent such as Virahol; Ketone chain-transfer agent such as acetone; Lipid chain-transfer agent such as ethyl acetate, methyl acetate, diethyl malonate, methylcarbonate, diethyl carbonate; Halogen alkane chain transfer agent such as chloroform, CFC-11, CFC-12, CFC-22, HCFC-123; Aliphatics alkane chain transfer agent such as methylcyclopentane, methylcyclohexane or the like.
By the inclined to one side raw material monomer of 100 weight parts, total consumption of described chain-transfer agent is 0.01～3 weight part, is preferably the 0.05-2.5 weight part, more preferably the 0.1-1.5 weight part.
Polyvinylidene fluoride polymer of the present invention also comprises the step of in batches adding all the other initiators.Additional way is as described below:
If a) initial add-on W
0Proportion is lower than 10 weight % in whole initiators, and then remainder divides average the adding 10 times.Promptly the transformation efficiency whenever reaction reaches the initiator that disposable adding in 9% o'clock accounts for remainder 1/10th;
B) if initial add-on W
0When proportion was between 10～30 weight % in whole initiators, then remainder divided average the adding 4 times.Promptly the transformation efficiency whenever reaction reaches the initiator that disposable adding in 20% o'clock accounts for remainder 1/4th;
C) if initial add-on W
0When proportion was between 30～50 weight % in whole initiators, then remainder divided average the adding 2 times.Promptly the transformation efficiency whenever reaction reaches the initiator that disposable adding in 33% o'clock accounts for remainder 1/2nd;
D) if initial add-on W
0When proportion was higher than 50 weight % in whole initiators, then remainder divided 1 adding.Promptly when reaction conversion ratio reaches 50%, the initiator of disposable adding residual content.
In the present invention, term " transformation efficiency " is meant and consumes monomer mass and total ratio that consumes monomer mass.
The present invention intermittently adds initiator in batches but not adds initiator as prior art in batches continuously in the vinylidene polymerization process.Adding number of times decides according to initial add-on.Allow the initiator concentration in the reaction process to have certain fluctuation to make molecular weight distribution unlikely too narrow on the one hand thereby intermittently add initiator in batches, thereby can make and keep initiator concentration to be in making molecular weight distribution unlikely too wide within the scope by adding initiator again on the other hand.
In the present invention, term " in batches intermittently add initiator " is meant initiator is added polymerization system in batches that reinforced method is that moment adds a collection of initiator once when arriving regular hour point (perhaps reaching certain transformation efficiency).
In the present invention, term " adds initiator continuously in batches " and is meant initiator is added polymerization system in batches, and reinforced method is to add a collection of initiator in the timed interval at each section.For example, the speed with 0.1 gram/minute adds initiator.
The initiator of being added can be identical with the initiator of initial adding or inequality in the present invention.In a better example of the present invention, the initiator of being added can be identical with the initiator of initial adding.
Reaction pressure is controlled at 2～6MPa in the present invention, preferred 2.5～5MPa, and temperature is controlled at 60～150 ℃, is preferably to carry out polyreaction under 100～140 ℃.
The present invention replaces the method that in batches adds initiator continuously of the prior art with the method that intermittently adds initiator in batches.The present invention has kept prior art to add the advantage of initiator method continuously in batches, promptly makes in the polymerization process by adding initiator that initiator concentration remains in certain scope in the concrete system, thereby makes molecular weight distribution unlikely too wide.
On the other hand, the method that utilization of the present invention intermittently adds initiator in batches makes in the polymerization process that initiator concentration has certain fluctuation in the polymerization system in above-mentioned concentration range, has solved the too narrow defective that is difficult to satisfy some specific end use requirement of molecular weight distribution in the art methods.
The present invention adds the molecular weight of chain-transfer agent with controlling polymers when polyreaction begins, make it to be unlikely excessive, add the initiation reaction of part initiator by the initial stage then, control initiator concentration in the system in the reaction process by adding initiator afterwards, thereby speed of response is kept within the specific limits, and then control final molecular weight distribution.Finally can guarantee to obtain vinylidene fluoride homopolymer unimodal or bimodal, moderate molecular weight distribution or multipolymer under certain weight-average molecular weight condition.
In addition, because the requirement of Application Areas aspect, vinylidene fluoride homopolymer that primary particle size is less or multipolymer have better dissolution with solvents ability.The vinylidene fluoride homopolymer or the multipolymer that make by the present invention are more suitable in film field and electric field.
The vinylidene fluoride homopolymer that the present invention makes, its melt flow rate (MFR) 0.1～20g/10min is preferably 0.2～12g/10min.Between primary particle diameter 0.1～1 μ m, be preferably between primary particle diameter 0.2～0.7 μ m, weight-average molecular weight is 40～120 myriagram/moles, is preferably 60～100 myriagram/moles, and molecular weight distribution coefficient 1.5～9 is preferably 2～6.
The vinylidene fluoride copolymers that the present invention makes, its comonomer are selected from the vinyl compound that can carry out free radical or ionic copolymerization with vinylidene, and its melt flow rate (MFR) 0.1～20g/10min is preferably 0.2～12g/10min.Between primary particle diameter 0.1～1 μ m, be preferably between primary particle diameter 0.2～0.7 μ m, weight-average molecular weight is 40～120 myriagram/moles, is preferably 60～100 myriagram/moles, and molecular weight distribution coefficient 1.5～9 is preferably 2～6.Wherein the content of vinylidene fluoride monomers is not less than 80%.
Further specify the present invention below by embodiment.
Embodiment
Embodiment 1
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.The closed reaction still vacuumizes and replaces with vinylidene fluoride monomers, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 115 ℃, replenish vinylidene fluoride monomers absolute pressure to the reactor and maintain 5MPa with the speed of 90rpm.Add 2 gram DTBP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 5MPa by adding vinylidene fluoride monomers.The every increase by 20% of transformation efficiency is afterwards added 4 times with regard to disposable interpolation 2.5 gram DTBP, adds 10 grams altogether.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Embodiment 2
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.The closed reaction still vacuumizes and replaces with vinylidene fluoride monomers, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 140 ℃, replenish vinylidene fluoride monomers absolute pressure to the reactor and maintain 5MPa with the speed of 90rpm.Add 4 gram DTBP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 5MPa by adding vinylidene fluoride monomers.The every increase by 33% of transformation efficiency is afterwards added 2 times with regard to disposable interpolation 4 gram DTBP, adds 8 grams altogether.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Embodiment 3
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.The closed reaction still vacuumizes and replaces with vinylidene fluoride monomers, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 125 ℃, replenish vinylidene fluoride monomers absolute pressure to the reactor and maintain 4.5MPa with the speed of 90rpm.Add 6 gram DTBP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 4.5MPa by adding vinylidene fluoride monomers.Reach 50% o'clock disposable interpolation 6 gram DTBP at transformation efficiency afterwards.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Embodiment 4
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.The closed reaction still vacuumizes and replaces with vinylidene fluoride monomers, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 115 ℃, replenish vinylidene fluoride monomers absolute pressure to the reactor and maintain 5MPa with the speed of 90rpm.Add 1.7 gram IPP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 5MPa by adding vinylidene fluoride monomers.The every increase by 20% of transformation efficiency is afterwards added 4 times with regard to disposable interpolation 0.42 gram IPP, adds 1.68 grams altogether.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Embodiment 5
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.The closed reaction still vacuumizes and replaces with vinylidene fluoride monomers, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 100 ℃, replenish vinylidene fluoride monomers absolute pressure to the reactor and maintain 5MPa with the speed of 90rpm.Add 1 gram NPP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 5MPa by adding vinylidene fluoride monomers.The every increase by 33% of transformation efficiency is afterwards added 2 times with regard to disposable interpolation 1 gram NPP, adds 2 grams altogether.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Embodiment 6
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.The closed reaction still vacuumizes and replaces with vinylidene fluoride monomers, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 130 ℃, replenish vinylidene fluoride monomers absolute pressure to the reactor and maintain 5MPa with the speed of 90rpm.Add 1 gram DTBP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 5MPa by adding vinylidene fluoride monomers.The every increase by 9% of transformation efficiency is afterwards added 10 times with regard to disposable interpolation 1.1 gram DTBP, adds 10 grams altogether.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Comparative example 1
Carrying out polyreaction with the method identical with embodiment 1, is that initial DTBP adds 3 grams, in 1 hour, with 0.15 gram/minute, adds the residue initiator thereafter.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Comparative example 2
Carrying out polyreaction with the method identical with embodiment 1, is after initial DTBP adds 2 grams, and all the other then when the every increase by 33% of transformation efficiency, add each 5 grams, totally 10 grams at twice.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Comparative example 3
Carrying out polyreaction with the method identical with embodiment 1, is after initial DTBP adds 3 grams, and all the other then when the every increase by 10% of transformation efficiency, divide 9 adding, and each 1 restrains, and totally 9 restrains.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Embodiment 7
In 10 liters of horizontal reacting stills, adding 7000 gram deionized waters, 5 gram Potassium perfluorooctanoates and 5 gram melting ranges are the paraffin about 58 ℃.Add 5% R 1216 gas in vinylidene gas, both are standby behind premix.The closed reaction still vacuumizes and replaces with mix monomer, and the oxygen level in reactor is smaller or equal to 10ppm.Begin then to stir, temperature of reaction kettle is risen to 115 ℃, replenish mixed gas absolute pressure to the reactor and maintain 4.5MPa with the speed of 90rpm.Add 1 gram NPP and 1.4g ethyl acetate successively, the beginning polyreaction.Make reacting kettle inner pressure at 4.5MPa by adding vinylidene fluoride monomers.The every increase by 33% of transformation efficiency is afterwards added 2 times with regard to disposable interpolation 1 gram NPP, adds 2 grams altogether.When the reactor emulsion solid content reaches 18%, finish reaction.
Adopt the GPC method to measure the molecular weight and the distribution thereof of partial fluorine ethylene polymer.Solvent uses DMF.Probe temperature is 70 ℃.
Press GB/T3682-2000 standard test melt flow rate (MFR) (MFR).Probe temperature is 230 ℃, and load-carrying is 10 kilograms.
Adopt the size of laser particle analyzer test primary particle diameter.The results are shown in table 1.
Table 1
| Embodiment | MFR | Weight-average molecular weight | Distribution coefficient | Primary particle size/um |
| Embodiment 1 | 1.2 | 62.3 | 2.6 | 0.34 |
| Embodiment 2 | 1.4 | 54.8 | 2.5 | 0.33 |
| Embodiment 3 | 1.1 | 58.1 | 3.1 | 0.34 |
| Embodiment 4 | 15.1 | 37.9 | 2.1 | 0.26 |
| Embodiment 5 | 6.2 | 63 | 2.8 | 0.28 |
| Embodiment 6 | 1.0 | 56.5 | 3.1 | 0.31 |
| Comparative example 1 | 0.8 | 65 | 4.6 | 0.38 |
| Comparative example 2 | 0.5 | 78.2 | 4.2 | 0.37 |
| Comparative example 3 | 1.1 | 43.5 | 1.4 | 0.52 |
| Embodiment 7 | 5.3 | 71.6 | 3.3 | 0.41 |
More above-mentioned test-results as can be known, compare with the method that adds initiator continuously of prior art in batches, the method that adopts the present invention in batches intermittently to add initiator can obtain more moderate vinylidene fluoride homopolymer of distribution coefficient and multipolymer, and primary particle size is littler.Therefore, the partial fluorine ethylene polymer product that makes with the inventive method is applicable to the purposes that some is special, for example can be used for film field and electric field.
Claims (18)
1. the preparation method of a partial fluorine ethylene polymer, it comprises the steps:
(a) provide the water dispersion of vinylidene with other comonomer of choosing wantonly;
(b) initiator of adding chain-transfer agent and original bulk in described water dispersion is controlled at 2～6MPa in reaction pressure, and temperature is controlled at carries out polyreaction under 60～150 ℃;
(c) add the initiator of surplus as follows in batches:
(i) if described original bulk W
0Proportion is lower than 10 weight %, and then remainder divides average the adding 10 times, i.e. disposable adding accounts for the initiator of remainder 1/10th during the every increase by 9% of Fan Ying transformation efficiency;
If (ii) described original bulk W
0Proportion is between 10 between less than 30 weight %, and then remainder divides average the adding 4 times, i.e. disposable adding accounts for the initiator of remainder 1/4th during the every increase by 20% of Fan Ying transformation efficiency;
If (iii) described original bulk W
0Proportion is between 30～50 weight %, and then remainder divides average the adding 2 times, i.e. disposable adding accounts for the initiator of remainder 1/2nd during the every increase by 33% of Fan Ying transformation efficiency;
If (iv) described original bulk W
0Proportion is higher than 50 weight %, then 1 property of remainder adding, and promptly when reaction conversion ratio reaches 50%, the initiator of disposable adding residual content.
2. the method for claim 1 is characterized in that described dispersion contains dispersion agent, and described dispersion agent is a fluorochemical surfactant.
3. method as claimed in claim 2, by 100 weight parts monomers raw materials, the add-on of dispersion agent is 0.01～2 weight part, described fluorochemical surfactant has general formula X C
nF
2nCOOM, wherein X is fluorine atom or hydrogen atom, and n is 4～12 integer, and M is hydrogen ion or alkalimetal ion or ammonium ion.
4. as each described method in the claim 1～3, it is characterized in that described initiator is a peroxide initiator, by 100 weight parts monomers raw materials, total consumption of described peroxide initiator is 0.05～5 weight part.
5. method as claimed in claim 4 is characterized in that described peroxide initiator is selected from persulphate or peroxyester compounds.
6. method as claimed in claim 5 is characterized in that described peroxyester compounds is the peroxycarbonates compounds.
7. as each described method in the claim 1～3, it is characterized in that by 100 weight parts monomers raw materials, total consumption of described chain-transfer agent is 0.01～3 weight part, and described chain-transfer agent is selected from alcohols, ketone, ester class, Halogen alkane, aliphatics alkane compound.
8. method as claimed in claim 5 is characterized in that described persulphate is selected from Potassium Persulphate, ammonium persulphate, Sodium Persulfate; Described peroxyester compounds is selected from the peroxidation trimethylacetic acid tert-butyl ester or the special pentyl ester of peroxidation trimethylacetic acid.
9. method as claimed in claim 6 is characterized in that described peroxycarbonates compounds is selected from peroxy dicarbonate diethyl ester, di-isopropyl peroxydicarbonate, peroxy dicarbonate di-n-propyl ester, peroxy dicarbonate two (4-tertiary butyl cyclohexyl) ester.
10. method as claimed in claim 7 is characterized in that described alcohol compound is selected from Virahol; Described ketone is selected from acetone; Described ester compound is selected from ethyl acetate, methyl acetate, diethyl malonate, methylcarbonate, diethyl carbonate; Described Halogen alkane compound is selected from CHCl
3, CCl
3F, CCl
2F
2, CHClF
2, CHCl
2CF
3Described aliphatics alkane is selected from methylcyclopentane, methyl cyclohexanol.
11. as arbitrary described method in the claim 1～3, it is characterized in that polymeric reaction temperature is 100～140 ℃, the pressure of polyreaction is 2.5～5MPa.
12. as each described method in the claim 1～3, it is characterized in that described comonomer is selected from vinyl fluoride, trifluoro-ethylene, trifluorochloroethylene, tetrafluoroethylene, 3,3,3-trifluoro propene, R 1216, perfluoroalkyl vinyl ether, perfluor (2,2-dimethyl-1,3-Dloxole diene) or its mixture.
13. method as claimed in claim 12 is characterized in that described perfluoroalkyl vinyl ether is selected from perfluoro methyl vinyl ether or perfluoroethylvinyl ether.
14. partial fluorine ethylene polymer that makes with the described method of claim 1, wherein the unitary content of vinylidene fluoride monomers surpasses 80 moles of %, melt flow rate (MFR) 0.1～the 20g/10min of described polymkeric substance, between primary particle diameter 0.1～1 μ m, weight-average molecular weight is 40～120 myriagram/moles, molecular weight distribution coefficient 1.5～9.
15. polymkeric substance as claimed in claim 14 is characterized in that its melt flow rate (MFR) 0.2～12g/10min, between primary particle diameter 0.2～0.7 μ m, weight-average molecular weight is 60～100 myriagram/moles, molecular weight distribution coefficient 2～6.
16. as claim 14 or 15 described polymkeric substance, it is characterized in that described polymkeric substance contains comonomer unit, described comonomer unit is derived from the vinyl compound that can carry out free radical or ionic copolymerization with vinylidene.
17. polymkeric substance as claimed in claim 16, it is characterized in that described monomeric unit is derived from vinyl fluoride, trifluoro-ethylene, trifluorochloroethylene, tetrafluoroethylene, 3,3,3-trifluoro propene, R 1216, perfluoroalkyl vinyl ether, perfluor (2,2-dimethyl-1,3-Dloxole diene) or its mixture.
18. polymkeric substance as claimed in claim 17 is characterized in that described perfluoroalkyl vinyl ether is selected from perfluoro methyl vinyl ether or perfluoroethylvinyl ether.
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| CN102585078B (en) * | 2012-01-13 | 2013-11-20 | 浙江孚诺林化工新材料有限公司 | Vinylidene fluoride copolymer used as solar back panel film and preparation method of vinylidene fluoride copolymer |
| CN103351446B (en) * | 2013-07-25 | 2015-08-26 | 中昊晨光化工研究院有限公司 | A kind of preparation method of high-tensile-strengtpolyvinylidene polyvinylidene fluoride |
| CN103739756B (en) * | 2013-12-04 | 2016-08-17 | 中昊晨光化工研究院有限公司 | A kind of polyvinylidene fluoride polymer preparation method improving heat stability |
| CN103665239A (en) * | 2013-12-17 | 2014-03-26 | 常熟丽源膜科技有限公司 | Preparation method of polyvinylidene fluoride with high tensile strength |
| CN103755858B (en) * | 2013-12-30 | 2016-04-27 | 山东华夏神舟新材料有限公司 | A kind of solution polymerization process of polyvinylidene fluoride copolymer |
| CN104151457B (en) * | 2014-08-11 | 2017-10-27 | 东莞市长安东阳光铝业研发有限公司 | A kind of method for preparing Kynoar |
| CN113861326A (en) * | 2020-06-30 | 2021-12-31 | 中昊晨光化工研究院有限公司 | Method for controlling Mooney viscosity of peroxide vulcanized fluororubber |
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| US3857827A (en) * | 1974-01-25 | 1974-12-31 | Pennwalt Corp | Method of preparing high-quality vinylidene fluoride polymer in aqueous emulsion |
| US5569728A (en) * | 1994-03-21 | 1996-10-29 | Ausimont, S.P.A. | (co)polymerization process in suspension for preparing hydrogen containing thermoplastic fluoropolymers |
| CN1532212A (en) * | 2003-01-23 | 2004-09-29 | ���з��ɹ�˾ | Process for preparing polymeta fluoro ethylene |
| CN1583809A (en) * | 2004-06-09 | 2005-02-23 | 上海三爱富新材料股份有限公司 | Vinylidene polyme and preparing method thereof |
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| US3857827A (en) * | 1974-01-25 | 1974-12-31 | Pennwalt Corp | Method of preparing high-quality vinylidene fluoride polymer in aqueous emulsion |
| US5569728A (en) * | 1994-03-21 | 1996-10-29 | Ausimont, S.P.A. | (co)polymerization process in suspension for preparing hydrogen containing thermoplastic fluoropolymers |
| CN1532212A (en) * | 2003-01-23 | 2004-09-29 | ���з��ɹ�˾ | Process for preparing polymeta fluoro ethylene |
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