CN1406995A - Polyacetal copolymer production - Google Patents
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- CN1406995A CN1406995A CN 02131504 CN02131504A CN1406995A CN 1406995 A CN1406995 A CN 1406995A CN 02131504 CN02131504 CN 02131504 CN 02131504 A CN02131504 A CN 02131504A CN 1406995 A CN1406995 A CN 1406995A
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Abstract
The present invention relates to a method for producing a polyacetal copolymer by polymerizing a trioxane, used as a main monomer, with a cyclic ether and/or a cyclic formal having at least a carbon-carbon bond, used as a comonomer, which comprises copolymerizing by the use of a specified hetero-polyacid as a polymerization catalyst, adding a solid basic compound as a deactivator of the catalyst to the reaction product obtained, and then, conducting a melt-kneading treatment of the addition mixture to deactivate the catalyst, and according to the present invention, a polyacetal copolymer is produced having an extremely little amount of an unstable terminal part, being very stable to heat, and being least in a releasing amount of aldehyde therefrom, using a simple process in which deactivation of a catalyst can briefly be conducted, a washing operation is unnecessary and a high polymerization yield can be obtained.
Description
Invention field
The present invention relates to trioxane and comonomer and in the presence of the heteropolyacid polymerizing catalyst, after the copolymerization, in the copolymerization product, add the manufacture method that the solid alkaline compound makes the Copolyacetal of catalyst deactivation.
According to the present invention, can simplify manufacturing process, and can obtain superior in quality Copolyacetals such as thermostability, low formaldehyde discharging amount.
Background technology
At present, as the manufacture method of Copolyacetal, be known that the Yi trioxane is as main monomer, with the cyclic ether that contains at least one carbon-carbon bond and/or the cyclic formals cationic copolymerization as comonomer.
As the cation activity catalyzer that is used for these copolymerizations, suggestion is Lewis acid, the halogenide of boron, tin, titanium, phosphorus, arsenic and antimony particularly, for example boron trifluoride, tin tetrachloride, titanium tetrachloride, phosphorus pentachloride, phosphorus pentafluoride, arsenic pentafluoride and antimony pentafluoride, and complex compound or salt like compound; Protonic acid, for example perchloro-acid; The ester of the ester of protonic acid, particularly protonic acid and lower aliphatic alcohols, for example perchloro-tert-butyl acrylate; The acid anhydride of protonic acid; the mixed anhydride of protonic acid and lower aliphatic carboxylic acid particularly; for example ethanoyl perchloro-acid esters, or trimethylammonium oxygen father-in-law phosphofluoric acid ester, triphenyl-methyl hexafluoroarsenate ester, ethanoyl Tetrafluoroboric acid ester, ethanoyl phosphofluoric acid ester and ethanoyl hexafluoroarsenate ester etc.Wherein, boron trifluoride or boron trifluoride and organic compound for example the coordination compound of ethers industrially also be extensive use of as being the most general as the polymerizing catalyst of main monomer with trioxane.
But, adopt the general polymerizing catalysts that use such as boron trifluoride class, must be many amount (for example with respect to total monomer be 40ppm or more than), the inactivation of polymerization rear catalyst is handled and is carried out very difficultly, handle even carry out inactivation, since residual from the material in the catalyzer, also can promote to decompose, the polymerization yield and the polymerization degree etc. are limited, occur existing the unstable terminal part of a great deal of in addition and the numerous and diverse problems such as stabilization operation of needs.
Disclose in the Te Kaiping 1-170610 communique and used the manufacture method of heteropolyacid as catalyzer, amines such as end polymeric reaction system interpolation preferred ammonia of mixing or triethylamine, tri-n-butylamine, hindered amine are disclosed, perhaps the oxyhydroxide of basic metal, alkaline-earth metal, organic acid salt (for example soap) wait other known catalyst deactivation agent, by interpolation contain these deactivators solution, handle and to make in the polymerizing catalyst and inactivation.But, in the method, add the aqueous solution stopped reaction of the deactivator as the water that contains 0.1% Tributylamine, be crushed to simultaneously below 200 orders, carry out washing with acetone and drying.
That is, in adopting the copolymerization process of above-mentioned catalyzer, the inactivationization of the catalyzer after the polymerization is important, if inactivation is insufficient, then promotes to generate the decomposition of multipolymer, becomes the bigger reason of the multipolymer stability that infringement generates thereafter.Therefore, for the inactivation that fully carries out catalyzer is handled, add a large amount of deactivator solution in the product after polymerization, fully clean and remove the residue that comes from residual monomer and catalyzer, thereafter separate multipolymer and treatment solution, drying perhaps reclaims monomer etc. from ablution, need extremely numerous and diverse operation, economically neither be desirable.
Be accompanied by the numerous and diverse of this catalyst deactivation processing in order to save, also advise in the multipolymer that generates, adding the method (special public clear 55-42085 communique etc.) of trivalent phosphorous compound and the method (spy opens clear 62-257922 communique etc.) of adding hindered amine compound, but these methods all with the present general known polymerizing catalyst of similar boron trifluoride class catalyzer as object, if research according to the inventor, can not carry out sufficient inactivation, the multipolymer that obtains good thermal stability is very difficult.
If the polymerization yield when particularly improving polymerization, the polymkeric substance of generation becomes more unsettled material, needs numerous and diverse stabilization treatment in the back operation, can't simplify the end operation, and its stability is also limited and undesirable qualitatively in addition.
The object of the present invention is to provide and finish the inactivation that can carry out catalyzer simply, also do not need to clean the simple method of operation in addition, also high, the unstable terminal part of polymerization yield is few, to the method for the few manufacturing Copolyacetal of heat also stabilizer pole, formaldehyde discharging amount.
Summary of the invention
The inventor in order to achieve the above object, kind and its corresponding method for deactivating to catalyzer have carried out wholwe-hearted research, found that, particularly use heteropolyacid as catalyzer, though its feature as catalyzer has very strong polymerization activity, but with solution state but directly do not add basic cpd and carry out fusion and mix and rub processing with solid state as long as in its reaction product (being also referred to as thick multipolymer) be not, just can make catalyst deactivation easily and steadily by the utmost point, thereby achieve the above object, and finished the present invention thus.
Promptly, the 1st content of the present invention is, a kind of manufacture method of Copolyacetal is provided, its Yi trioxane as main monomer (a), with the cyclic ether that contains at least one carbon-carbon bond and/or cyclic formals as comonomer (b), make Copolyacetal, it is characterized in that, use the heteropolyacid of following general formula (1) expression to carry out copolymerization as catalyst for polymerization (c), add solid alkaline compound (d) in reaction product, fusion mixes rubs processing, make catalyzer (c) inactivation
H
m[M
1 x·M
2 yO
z]·nH
2O????(1)
In the formula, M
1Expression is by being selected from a kind of or two kinds elementary composition central element among P and the Si, M
2Expression is selected from more than one the coordination element among W, Mo and the V, x:1-10, y:6-40, z:10-100, the integer that m:1 is above, n:0-50.
The 2nd content of the present invention be, in the manufacture method of above-mentioned Copolyacetal, comonomer (b) is selected from 1,3-dioxolane, glycol ether formal, 1,4-butyleneglycol formal, 1, at least a in 3-diox and the oxyethane.
The 3rd content of the present invention is, in the manufacture method of the 1st or the 2nd described Copolyacetal of the present invention, the heteropolyacid of general formula (1) expression is selected from least a in phospho-molybdic acid, phospho-wolframic acid, P-Mo-Wo acid, molybdovanaphosphoric acid, P-Mo-Wo-V acid, tungstovanadophosphoric acid, silicotungstic acid, silicomolybdic acid, silicon molybdenum wolframic acid and the silicon molybdenum tungsten vanadic acid.
The 4th content of the present invention is, in the 1st～3 of the present invention in the manufacture method of each described Copolyacetal, described solid alkaline compound (d) is selected from least a in triazine ring compound, polymeric amide and the mineral alkali of containing of amino with amino or replacement.
The 5th content of the present invention be, in the manufacture method of the 4th described Copolyacetal of the present invention, the triazine ring compound that contains of described amino with amino or replacement is selected from least a in melamine, melamine resin, CTU guanamines and the CMTU guanamines.
The 6th content of the present invention be, in the manufacture method of the 4th described Copolyacetal of the present invention, described polymeric amide is selected from least a in nylon 6, nylon 12, nylon 4/6, nylon 6/6, nylon 6/10, the nylon 6/12.
The 7th content of the present invention be, in the manufacture method of the 4th described Copolyacetal of the present invention, described mineral alkali is selected from least a in alkali metal compound or the alkali earth metallic compound.
The 8th content of the present invention is, in the 1st～7 of the present invention in the manufacture method of each described Copolyacetal, make in advance after the solution of main monomer (a), comonomer (b) and catalyzer (c) mixes under liquid phase state, be supplied to poly-unit.
The 9th content of the present invention is in the manufacture method of each described Copolyacetal, to mix catalyzer (c) inactivation of rubbing processing by fusion and carry out in the presence of antioxidant in the 1st～8 of the present invention.
Embodiment
Below the present invention is described in detail.
Among the present invention,, use the cyclic trimer Ji trioxane of formaldehyde as main monomer (a).
In addition, among the present invention, as comonomer (b), use the cyclic ether and/or the cyclic formals that contain at least one carbon-carbon bond, any one can use the known comonomer of the existing Yu of can be used for trioxane copolymerization.As the example of the representative of such cyclic ether and cyclic formals, for example can enumerate 1,3-dioxolane, glycol ether formal, 1,4-butyleneglycol formal, 1,3-diox, oxyethane, propylene oxide, epichlorohydrin etc.Wherein, preferred 1,3-dioxolane, glycol ether formal, 1,4-butyleneglycol formal, 1,3-diox, oxyethane etc.
In addition, also can use for example beta-propiolactone and vinyl compound vinylbenzene etc. for example of cyclic ester.In addition, the comonomer as being used to form a chain and corsslinking molecular structure copolymer also can use the such compound that contains 2 above polymerizability ring-type ethers or cyclic formals base of alkylidene group-diglycidylether and two formals.For example, can enumerate butyleneglycol secondary methylglycerin(e) base ether, butanediol diglycidyl ether etc.
The amount that is used for the present invention's copolymerization usefulness (b) is 0.1～20 mole of % with respect to trioxane, is preferably 0.2～10 mole of %.0.1 mole of % of less than, unsettled terminal part increases and bad stability, if excessive in addition, the multipolymer deliquescing of generation, fusing point reduce, this is not desirable.
Also have, in polymerization process of the present invention, also can further add according to purpose and to be used to regulate for example methylal low-molecular-weight linear acetal etc. like this of the known chain-transfer agent of the polymerization degree.In addition, preferably there is not the impurity state of water, methyl alcohol, formic acid etc. for example that contains active hydrogen in fact in polymerization reaction system, and for example these impurity are approximately below the 10ppm.
Heteropolyacid is the general name of the polyacid that generates of different types of oxygen acid dehydrating condensation, and there is specific different types of element in the center, have can with Sauerstoffatom covalency and condensation acidic group can condensation monokaryon or multinuclear complex ion.Such heteronuclear dehydroamino acid generally can be represented with above-mentioned general formula (1).
As the catalyst for polymerization among the present invention (c), especially effectively heteropolyacid is in some cases, the central element (M in the above-mentioned composition formula
1) by being selected from a kind of of P and Si or two kinds of elements constitute, coordination element (M
2) situation about constituting by more than one the element (being preferably W and Mo especially) that is selected from W, Mo and V.Object lesson as these heteropolyacids is phospho-molybdic acid, phospho-wolframic acid, P-Mo-Wo acid, molybdovanaphosphoric acid, P-Mo-Wo-V acid, tungstovanadophosphoric acid, silicotungstic acid, silicomolybdic acid, silicon molybdenum wolframic acid, silicon molybdenum tungsten vanadic acid etc.Wherein preferably silicomolybdic acid, silicotungstic acid, phospho-molybdic acid, phospho-wolframic acid.
The usage quantity of above-mentioned catalyzer (c), also different according to its kind, in addition, appropriate change can telo merization, but be the scope of 0.05～100ppm (following expression w/w ppm) generally with respect to answering the monomeric total amount of polymeric, preferred 0.1～50ppm.In addition, phospho-molybdic acid, phospho-wolframic acid etc. are pretended the heteropolyacid of usefulness so very much, and the usage quantity of 0.1～10ppm is just enough.Even a spot of like this catalyzer also can copolymerization, the main chain that only stays on a small quantity the polymkeric substance that causes by catalyzer undesirable reaction such as decomposes, depolymerize, this is for the unsettled manthanoate terminal group of inhibition (O-CH=O), hemiacetal terminal group (O-CH
2-OH) generation of grade is resultful, in addition, also is favourable economically.
In order to react equably, catalyzer (c) is preferably used not to be had dysgenic inert solvent dilution, is added in main monomer (a) and/or the comonomer (b) and uses polymerization.As above-mentioned inert solvent, preferred specifiable be that carbonatomss such as formic acid, acetic acid, propionic acid, butyric acid are that carbonatomss such as the low molecular weight carboxylic acid of 1-10 and methyl alcohol, ethanol, 1-propyl alcohol, 2-propyl alcohol, 1-butanols, 2-butanols, 2-methyl isophthalic acid-propyl alcohol, 2-methyl-2-propyl alcohol, 1-amylalcohol, 3-methyl isophthalic acid-butanols, 1-hexanol are the ester that the low-molecular-weight pure condensation of 1-10 obtains; Acetone, 2-butanone, 2 pentanone, propione, methyl-n-butyl ketone, 3-hexanone, methyl iso-butyl ketone (MIBK), methyl-carbonatomss such as tertiary butyl ketone are the low-molecular-weight ketone of 1-10, but are not limited to these.If also consider industrial availability etc., optimal is methyl-formiate, ethyl formate, ritalin, vinyl acetic monomer, N-BUTYL ACETATE, acetone, 2-butanone, methyl iso-butyl ketone (MIBK) etc.
Polymerizing catalyst (c) is fit to the concentration dissolving with 1-30 w/w % in above-mentioned inert solvent, but is not limited thereto.
In addition, in polymerization system, be added on main monomer (a) and comonomer (b) and molecular weight regulator etc. partly or entirely in dissolve the solution of specified amount catalyzer in advance method also be preferable methods.
Polymerization process of the present invention can adopt equipment and the method same with having known trioxane copolymerization now to carry out.That is, in intermittent type, continous way, the semi continuous any can, generally use liquid monomer, carry out the method that polymeric obtains powder agglomates shape solid polymkeric substance simultaneously.
As the poly-unit that can be used among the present invention, can use the reactive tank of the subsidiary stirrer of general use in the intermittent type, in addition, as continous way, can use blender, the continuously extruded mixing machine of 2 axial spiral types, 2 vane type continuous mixers, other so far propose continuous polymerization units such as De trioxane, the polymerization machine that perhaps also can make up type more than 2 kinds uses.
Polymerization process does not limit especially, but as the inventor at first proposes (spy opens flat 11-302349 communique), if keep liquid phase state and thorough mixing trioxane, comonomer in advance and as the heteropolyacid of polymerizing catalyst, the reaction raw materials mixed solution that obtains is supplied to poly-unit carry out copolyreaction, can reduce the catalytic amount that needs, the result is favourable for obtaining the less Copolyacetal of formaldehyde discharging amount, is more suitable polymerization process.In being 60-120 ℃ temperature range, polymerization temperature carries out.
In the present invention, after the polymerization when the inactivation that carries out catalyzer is handled, unreacted monomer is few more good more, unreacted monomer (total of expression main monomer (a) and comonomer (b)) in multipolymer slightly is below the 10 weight %, further be below the 5 weight %, be preferably below the 3 weight % especially.This is because the present invention is not carrying out the cleaning as main purpose of thick multipolymer, so mostly residual monomer is undesirable.In order to reduce unreacted monomer, generally percent polymerization can be done certain raising, this uses the amount and the polymerization time (the continous way middle finger residence time) of catalyzer to reach easily by suitably regulating under situation of the present invention, owing to use active high heteropolyacid catalyst, in the relatively shorter time even therefore a spot of catalyzer also can reach.In addition, after the copolyreaction, the monomer that evaporation section is remaining makes it gasification and removes, and also can reach the remaining amount of monomer of regulation.
Also have, in the copolymerization or after the copolymerization, the unreacted trioxane and the comonomer that are recovered as gas liquefy sometimes, also can directly re-use as the part material monomer sometimes, and this situation is both economical.
Then, copolyreaction finishes the thick multipolymer obtain, does not clean and waits directly interpolation as the solid alkaline compound (d) of deactivator, carries out usually that fusion is mixed rubs processing, finishes the inactivation of catalyzer.
As solid alkaline compound (d), the solid state compound performance effect with alkalescence just can be used, and still preferably, is selected from least a in the compound that contains triazine ring, polymeric amide and the mineral alkali with amino or substituted-amino.
As the above-mentioned compound that contains triazine ring with amino or substituted-amino, (3, [2-(3 for 9-two can to enumerate preferably melamine, melamine resin, CTU guanamines, 5-diamino-2,4, the 6-triazinyl) ethyl]-2,4,8,10-four oxygen spiral shells [5,5] undecane, CMTU guanidine alkane (3,9-two [1-(and 3,5-diamino-2,4, the 6-triazinyl) methyl]-2,4,8,10-four oxygen spiral shell [5,5] undecanes), 3,9-two [1-(3,5-diamino-2,4, the 6-triazinyl)-1, the 1-dimethyl ethyl]-2,4,8,10-four oxygen spiral shell [5,5] undecanes etc.These can mix use more than 2 kinds and have not big harm.
As polymeric amide, specifiable is for example nylon 6, nylon 12, nylon 4/6, nylon 6/6, nylon 6/10, nylon 6/12 etc.These can mix use more than 2 kinds and not have obstruction.
As mineral alkali, specifiable is alkali metal compound or alkali earth metal compound, and specifiable specifically is metal oxides such as CaO, MgO; Ca (OH)
2, Mg (OH)
2Deng metal hydroxides; Na
2CO
3, K
2CO
3, CaCO
3, MgCO
3Deng metal inorganic hydrochlorates such as the borate of metal carbonate and these metals and phosphoric acid salt etc., preferably calcium hydroxide, magnesium oxide and yellow soda ash.These can mix use more than 2 kinds and not have obstruction.
The addition of solid alkaline compound (d), so long as be enough to make in the catalyzer and the amount of inactivation, restriction especially, but be 10～10000ppm, be preferably 100～2000ppm with respect to thick multipolymer usually.
In addition, when adding solid alkaline compound (d), thick multipolymer is preferably thin powder body, and the reaction machine is preferably the machine with abundant pulverizing bulk polymer function for this reason, but also can use the reactant after the pulverizer pulverizing polymerization to contact with solid alkaline compound (d) afterwards in addition.
In inactivation was handled, the granularity at least 90 weight % of thick multipolymer were above below 10mm, below the preferred 4mm, more preferably below the 2mm.
Added the thick multipolymer of solid alkaline compound (d), then directly carried out mixed processing, the complete deactivation of enforcement catalyzer rubbed of fusion without cleaning to wait.Fusion mixes rubs processing, is preferably the above temperature range until 260 ℃ of the fusing point of multipolymer.If be higher than 260 ℃ then the decomposition deterioration of polymkeric substance takes place, this is undesirable.
Mixing the device of rubbing processing for fusion does not limit especially, but be to have the function of mixed melting multipolymer, preferably have a device of degassing function, specifiable is for example to have the continuously extruded mixing machine of the single shaft of at least one venting hole or multiaxis, blender etc.
Fusion mixes rubs processing and preferably carries out in the presence of antioxidant.As antioxidant, can use existing known material, for example various hindered phenol anti-oxidants etc. as the Copolyacetal resin stabilizer.Specifiable is for example 2, the 6-di-tert-butyl-4-methy phenol, triglycol-two [3-(the 3-tertiary butyl-5-methyl-4-hydroxy phenyl) propionic ester], 1,6-hexylene glycol-two-[3-(3, the 5-di-tert-butyl-hydroxy phenyl) propionic ester], four [3-(3, the 5-di-tert-butyl-hydroxy phenyl) propionic ester] methane, N, N '-hexa-methylene two (3,5-di-t-butyl-4-hydroxyl hydrocinnamamide), the 2-tertiary butyl-6-(3 '-tertiary butyl-5 '-methyl-2 '-hydroxybenzyl)-4-aminomethyl phenyl acrylate, 3,9-two [2-{ (3-tertiary butyl-4-hydroxy-5-aminomethyl phenyl) propionyloxy }-1,1 '-dimethyl ethyl]-2,4,8,10-four oxygen spiral shell [5,5]-undecanes etc.
Also have, these hindered phenol anti-oxidants, also it partly or entirely can be added in advance polymerization in main monomer (a) before the polymerization or the comonomer (b), the addition of these hindered phenol anti-oxidants does not have special mistake to limit greatly, as long as the activity for polymerizing catalyst (c) does not have detrimentally affect, promptly is an embodiment preferred.
In addition, in this step as necessary, even the known material that adds as the stablizer of various Copolyacetal resins does not have any obstruction yet.In addition, also can add the such weighting agent of glass fibre for example, crystallization promotor (nuclear agent), remover etc.
As mentioned above, add in thick multipolymer after solid alkaline compound (d), fusion mix and rub processing, being generally shaped to particle etc. becomes the goods that resin treatment is used.Particle is dried as required.When dry, for example following dry 3 hours at 140 ℃.
Embodiment
Below, describe the present invention particularly by embodiment, but the present invention is not limited.
Also have, term and assay method in embodiment and the comparative example are as follows.
% or ppm all are weight % or ppm by weight.
Melt index (MI): be illustrated in 190 ℃ of melt index (units: g/10min) that measure down.This is as estimating corresponding to the characteristic value of molecular weight.Be that MI is low more, molecular weight is high more.
Alkali rate of decomposition (amount of l fraction): pulverize copolymer pellet, its 1g is joined 100ml to be contained in 50% methanol aqueous solution of 0.5% ammonium hydroxide, in encloses container, descend heating after 45 minutes at 180 ℃, decompose the amount of the formaldehyde of stripping in the quantitative analysis liquid, use % to represent with respect to polymkeric substance.
Heating weight decrement: be illustrated in the air and heat the weight decrement of 5g copolymer pellet in the time of 45 minutes down at 230 ℃.(omitted the weight decrement in the table 1.)
Formaldehyde discharging amount: sample is filled in the cylindrical shell that keeps 200 ℃, after fusion in 5 minutes, melts is squeezed in the encloses container from cylindrical shell.Feed nitrogen in this encloses container, the soluble in water and collection with the formaldehyde that contains in the nitrogen that comes out by measuring the concentration of formaldehyde in the water, is tried to achieve the weight of the formaldehyde of emitting from melts.Remove this formaldehyde weight with the weight of melts and be formaldehyde discharging amount (ppm of unit).Embodiment 1～13 and comparative example 1～2
As polymerizing reactor, use to have two circular portion eclipsed sections, the cylinder of the subsidiary interlayer by heat (cold) medium in the outside and within it portion stir, additionally advance a plurality of blades of usefulness, at the flow reactor that 2 turning axles vertically are set.Pass through 80 ℃ warm water in the interlayer of reactor, with 2 turning axles of constant speed rotation, supply with continuously at the one end and to contain the comonomer shown in 3.5% table 1 and 70ppm mixed solution as the methylal De trioxane of chain-transfer agent, while to add the methyl-formiate solution of the heteropolyacid catalyst shown in 5% table 1 continuously with respect to the amount shown in whole monomer tables 1, is carried out copolymerization to identical place.
But the addition of polymerizing catalyst is the weight ratio (ppm) with respect to whole monomer total amounts in the table 1, closes at boron trifluoride under the situation of dibutyl ether to be meant as boron trifluoride (BF
3) value.
Then, to the resultant of reaction of discharging, add as the solid alkaline compound shown in the table 1 of catalyst deactivation agent from the reactor relief outlet, add 0.3% triglycol-two [3-(the 3-tertiary butyl-5-methyl-4-hydroxy phenyl) propionic ester] as antioxidant, 2 extrusion machines that use subsidiary venting port mix as fusion under the 5mmHg and rub and push at 220 ℃, the vacuum tightness of exhaust portion, make particle.But the addition of deactivator is meant the weight ratio (ppm) with respect to thick multipolymer in the table 1.
This particle after dry 3 hours, carries out MI mensuration under 140 ℃, the thermal degradation rate measures, heats weight decrement mensuration and the formaldehyde discharging amount is measured.The result is presented in the table 1.
In addition, for relatively, for using the cyclohexane solution that closes the dibutyl ether as 0.5% boron trifluoride of catalyzer, use is as the known triphenylphosphine of deactivator with as two (2 of hindered amine, 2,6,6-tetramethyl--4-piperidyl) situation of sebate is carried out too.
Embodiment 14～15
The heteropolyacid of specified amount shown in the dissolving table 1 and modulate polymerization catalyzed agent solution in methyl-formiate is modulated at main monomer and is and added the comonomer shown in 3.5% table 1 and the 700ppm monomer mixed solution as the methylal of chain-transfer agent in the trioxane.Converge the pipeline separately of carrying this polymerization catalyzed agent solution and monomer mixed solution, after mixing by static mixer, direct supply response device, polymerization similarly to Example 1 obtains particle.Comparative example 3
Use is as the cyclohexane solution that 0.5% boron trifluoride closes the dibutyl ether that contains of catalyzer, carry out polymerization similarly to Example 1, to be modulated into 20 weight % slurries 0.1% triethylamine aqueous solution from the resultant of reaction that relief outlet is discharged, handled 1 hour at 80 ℃ of following inactivations, after the thin slice processing, drying is 1 hour under 100 ℃.Then add 0.3% triglycol-two [3-(the 3-tertiary butyl-5-methyl isophthalic acid-hydroxy phenyl) propionic ester], carry out same extruding and evaluation with embodiment 1 as antioxidant.Comparative example 4
Use the heteropolyacid shown in the table 1 as catalyzer, carry out similarly to Example 14 after the polymerization, same with comparative example 3, carry out by wet method aftertreatment, add antioxidant, extrude and estimate.Above-mentioned each result is presented in the table 1.
Table 1
| Polymerizing catalyst | The comonomer kind | Deactivator | Extrude particulate character | ||||||
| Kind | Amount (ppm) | Kind | Amount (ppm) | MI (g/10 minute) | Alkali rate of decomposition rate of decomposition (%) | Weight decrement reduction rate (%) | HCHO discharging amount (ppm) | ||
| Embodiment 1 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????E | ????1000 | ????9.1 | ????0.52 | ????0.42 | ????39 |
| Embodiment 2 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????A | ????1000 | ????9.0 | ????0.54 | ????0.41 | ????37 |
| Embodiment 3 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????D | ????1000 | ????9.4 | ????0.55 | ????0.43 | ????38 |
| Embodiment 4 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????I | ????1000 | ????9.3 | ????0.53 | ????0.44 | ????40 |
| Embodiment 5 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????K | ????100 | ????9.6 | ????0.57 | ????0.49 | ????41 |
| Embodiment 6 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????L | ????100 | ????9.7 | ????0.58 | ????0.47 | ????40 |
| Embodiment 7 | Phospho-wolframic acid | ????4.0 | ????DOXO | ????M | ????100 | ????9.6 | ????0.56 | ????0.46 | ????42 |
| Embodiment 8 | Silicotungstic acid | ????4.0 | ????DOXO | ????E | ????1000 | ????9.3 | ????0.54 | ????0.44 | ????35 |
| Embodiment 9 | Phospho-molybdic acid | ????4.0 | ????DOXO | ????B | ????1000 | ????9.3 | ????0.53 | ????0.43 | ????32 |
| Embodiment 10 | Silicomolybdic acid | ????4.0 | ????DOXO | ????J | ????1000 | ????9.7 | ????0.52 | ????0.45 | ????35 |
| Embodiment 11 | Phospho-wolframic acid | ????4.0 | ????BDFM | ????E | ????1000 | ????9.4 | ????0.51 | ????0.43 | ????37 |
| Embodiment 12 | Phospho-wolframic acid | ????4.0 | ????DEGFM | ????A | ????1000 | ????9.2 | ????0.54 | ????0.40 | ????34 |
| Embodiment 13 | Phospho-wolframic acid | ????4.0 | ????DXN | ????B | ????1000 | ????9.1 | ????0.53 | ????0.41 | ????33 |
| Embodiment 14 | Phospho-wolframic acid | ????2.5 | ????DOXO | ????E | ????1000 | ????8.6 | ????0.48 | ????0.37 | ????29 |
| Embodiment 15 | Phospho-molybdic acid | ????2.5 | ????DOXO | ????A | ????1000 | ????8.7 | ????0.47 | ????0.38 | ????28 |
| Comparative example 1 | ??BF 3·Bu 2O | ????40 | ????DOXO | ????F | ????500 | ????14.5 | ????1.49 | ????0.66 | ????109 |
| Comparative example 2 | ??BF 3·Bu 2O | ????40 | ????DOXO | ????G | ????2000 | ????15.5 | ????1.55 | ????0.69 | ????118 |
| Comparative example 3 | ??BF 3·Bu 2O | ????40 | ????DOXO | ???????????H | ????14.7 | ????1.42 | ????0.64 | ????103 | |
| Comparative example 4 | Phospho-wolframic acid | ????2.5 | ????DOXO | ???????????H | ????13.5 | ????1.29 | ????0.55 | ????101 | |
The abbreviation of comonomer is expressed as follows material in the table 1.
DOXO:1, the 3-dioxolane
BDFM:1,4-butyleneglycol formal
DEGFM: glycol ether formal
DXN:1, the 3-diox
EO: oxyethane
Use is as the following compound or the method for deactivator.
The A:CTU guanamines
The B:CMTU guanamines
D: melamine
E: melamine resin
F: triphenylphosphine
G: two (2,2,6,6-tetramethyl--4-piperidyl) sebate
H: form the wet method cooling of 20% slurries of thick multipolymer thin slice in 0.1% triethylamine aqueous solution
I: nylon 6
J: nylon 12
K: calcium hydroxide
L: magnesium oxide
M: yellow soda ash
The invention is characterized in, by using the high heteropolyacid of polymerization activity as polymerizing catalyst (c), can obtain high polymerization yield with minute quantity, and in thick multipolymer, add the solid alkaline compound after the polymerization, only mix by fusion and rub, just can obtain the Copolyacetal goods of very high-quality simply.This with respect under the situations such as existing boron trifluoride class catalyzer, its inactivation is insufficient and inactivation also is difficult to avoid after handling owing to cause the deleterious effect of decomposition etc. from the material of catalyzer, has special effect.
If according to the present invention, compare with existing wet method, use by dry method and simplify catalyst deactivation operation and the method for extremely rationalizing of having omitted clean operation, can carry out the complete deactivation of catalyst for polymerization.Its result can not make not decomposition from catalyzer, obstacle such as rotten economically, and l fraction is few, to the Copolyacetal thermally-stabilised and excellent quality that the formaldehyde discharging amount is few.
Claims (9)
1. the manufacture method of Copolyacetal, its Yi trioxane as main monomer (a), with the cyclic ether that contains at least one carbon-carbon bond and/or cyclic formals as comonomer (b), it is characterized in that, use the heteropolyacid of following general formula (1) expression to carry out copolymerization as polymerizing catalyst (c), in resultant of reaction, add solid alkaline compound (d), fusion mixes and rubs processing, makes polymerizing catalyst (c) inactivation
H
m[M
1 x·M
2 yO
z]·nH
2O????(1)
In the formula, M
1Expression is by a kind of or two kinds of elementary composition central elements that are selected among P and the Si, M
2Expression is selected from more than one the coordination element among W, Mo and the V, X:1-10, y:6-40, z:10-100, the integer that m:1 is above, n; 0-50.
2. method according to claim 1, wherein, described comonomer (b) is selected from 1,3-dioxolane, glycol ether formal, 1,4-butyleneglycol formal, 1, at least a in 3-diox and the oxyethane.
3. method according to claim 1 and 2, wherein, the heteropolyacid of general formula (1) expression is selected from least a in phospho-molybdic acid, phospho-wolframic acid, P-Mo-Wo acid, molybdovanaphosphoric acid, P-Mo-Wo-V acid, tungstovanadophosphoric acid, silicotungstic acid, silicomolybdic acid, silicon molybdenum wolframic acid and the silicon molybdenum tungsten vanadic acid.
4. according to each described method in the claim 1～3, wherein, described solid alkaline compound (d) is selected from least a in triazine ring compound, polymeric amide and the mineral alkali of containing of amino with amino or replacement.
5. method according to claim 4, wherein, the triazine ring compound that contains of described amino with amino or replacement is selected from least a in melamine, melamine resin, CTU guanamines and the CMTU guanamines.
6. method according to claim 4, wherein, described polymeric amide is selected from least a in nylon 6, nylon 12, nylon 4/6, nylon 6/6, nylon 6/10, the nylon 6/12.
7. method according to claim 4, wherein, described mineral alkali is selected from least a in alkali metal compound or the alkaline earth metal compound.
8. according to each described method in the claim 1～7, wherein, make in advance after the solution of main monomer (a), comonomer (b) and polymerizing catalyst (c) mixes under liquid phase state, be supplied to poly-unit.
9. according to each described method in the claim 1～8, wherein, mix the catalyst deactivation of rubbing processing by fusion and in the presence of antioxidant, carry out.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001212918 | 2001-07-12 | ||
| JP2001212918A JP4610805B2 (en) | 2001-07-12 | 2001-07-12 | Process for producing polyacetal copolymer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1406995A true CN1406995A (en) | 2003-04-02 |
| CN1237086C CN1237086C (en) | 2006-01-18 |
Family
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02131504 Expired - Lifetime CN1237086C (en) | 2001-07-12 | 2002-07-09 | Polyacetal copolymer production |
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| Country | Link |
|---|---|
| JP (1) | JP4610805B2 (en) |
| CN (1) | CN1237086C (en) |
| HK (1) | HK1054756A1 (en) |
| MY (1) | MY135168A (en) |
| TW (1) | TW593398B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102079801A (en) * | 2009-09-25 | 2011-06-01 | 提克纳有限公司 | Oxymethylene polymers and process for the preparation thereof |
| WO2014083987A1 (en) * | 2012-11-27 | 2014-06-05 | ポリプラスチックス株式会社 | Production method for polyacetal copolymer |
| WO2014083983A1 (en) * | 2012-11-27 | 2014-06-05 | ポリプラスチックス株式会社 | Production method for polyacetal copolymer |
| CN101525404B (en) * | 2008-03-07 | 2015-04-29 | 宝理塑料株式会社 | Method for producing thermostable polyacetal copolymer |
| CN105143294A (en) * | 2013-04-25 | 2015-12-09 | 宝理塑料株式会社 | Method for producing polyacetal copolymer |
| US9695265B2 (en) | 2014-03-31 | 2017-07-04 | Polyplastics Co., Ltd. | Process for producing polyacetal copolymer |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5225529B2 (en) * | 2001-07-12 | 2013-07-03 | ポリプラスチックス株式会社 | Process for producing polyacetal copolymer |
| JP6282805B2 (en) | 2013-04-25 | 2018-02-21 | ポリプラスチックス株式会社 | Process for producing polyacetal copolymer |
| JP7096043B2 (en) * | 2018-03-30 | 2022-07-05 | ポリプラスチックス株式会社 | Method for producing polyacetal copolymer |
| CN111662554B (en) * | 2020-07-13 | 2022-03-11 | 万华化学集团股份有限公司 | Polyacetal composition and preparation method and application thereof |
| JP2024090366A (en) * | 2022-12-23 | 2024-07-04 | ポリプラスチックス株式会社 | Method for producing polyacetal copolymer |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3916787B2 (en) * | 1998-12-28 | 2007-05-23 | ポリプラスチックス株式会社 | Process for producing polyacetal copolymer |
| KR100306072B1 (en) * | 1999-07-09 | 2001-09-24 | 최동건 | Method of deactivating a polymerization catalyst |
-
2001
- 2001-07-12 JP JP2001212918A patent/JP4610805B2/en not_active Expired - Lifetime
-
2002
- 2002-07-01 MY MYPI20022487 patent/MY135168A/en unknown
- 2002-07-04 TW TW91114855A patent/TW593398B/en not_active IP Right Cessation
- 2002-07-09 CN CN 02131504 patent/CN1237086C/en not_active Expired - Lifetime
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101525404B (en) * | 2008-03-07 | 2015-04-29 | 宝理塑料株式会社 | Method for producing thermostable polyacetal copolymer |
| CN102079801A (en) * | 2009-09-25 | 2011-06-01 | 提克纳有限公司 | Oxymethylene polymers and process for the preparation thereof |
| WO2014083987A1 (en) * | 2012-11-27 | 2014-06-05 | ポリプラスチックス株式会社 | Production method for polyacetal copolymer |
| WO2014083983A1 (en) * | 2012-11-27 | 2014-06-05 | ポリプラスチックス株式会社 | Production method for polyacetal copolymer |
| US9657136B2 (en) | 2012-11-27 | 2017-05-23 | Polyplastics Co., Ltd. | Production method for polyacetal copolymer |
| CN105143294A (en) * | 2013-04-25 | 2015-12-09 | 宝理塑料株式会社 | Method for producing polyacetal copolymer |
| CN105143294B (en) * | 2013-04-25 | 2017-09-05 | 宝理塑料株式会社 | The manufacture method of Copolyacetal |
| US9695265B2 (en) | 2014-03-31 | 2017-07-04 | Polyplastics Co., Ltd. | Process for producing polyacetal copolymer |
| CN105916906B (en) * | 2014-03-31 | 2017-12-05 | 宝理塑料株式会社 | The manufacture method of Copolyacetal |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4610805B2 (en) | 2011-01-12 |
| MY135168A (en) | 2008-02-29 |
| CN1237086C (en) | 2006-01-18 |
| TW593398B (en) | 2004-06-21 |
| HK1054756A1 (en) | 2003-12-12 |
| JP2003026746A (en) | 2003-01-29 |
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