WO2016056810A1 - 내열성 수지의 제조방법, 내열성 수지 및 내열 abs 수지 조성물 - Google Patents
내열성 수지의 제조방법, 내열성 수지 및 내열 abs 수지 조성물 Download PDFInfo
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- C—CHEMISTRY; METALLURGY
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F212/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
- C08F212/02—Monomers containing only one unsaturated aliphatic radical
- C08F212/04—Monomers containing only one unsaturated aliphatic radical containing one ring
- C08F212/06—Hydrocarbons
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- C08F212/10—Styrene with nitriles
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F265/00—Macromolecular compounds obtained by polymerising monomers on to polymers of unsaturated monocarboxylic acids or derivatives thereof as defined in group C08F20/00
- C08F265/08—Macromolecular compounds obtained by polymerising monomers on to polymers of unsaturated monocarboxylic acids or derivatives thereof as defined in group C08F20/00 on to polymers of nitriles
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- C08F2/00—Processes of polymerisation
- C08F2/12—Polymerisation in non-solvents
- C08F2/16—Aqueous medium
- C08F2/22—Emulsion polymerisation
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- C08F2/00—Processes of polymerisation
- C08F2/12—Polymerisation in non-solvents
- C08F2/16—Aqueous medium
- C08F2/22—Emulsion polymerisation
- C08F2/24—Emulsion polymerisation with the aid of emulsifying agents
- C08F2/26—Emulsion polymerisation with the aid of emulsifying agents anionic
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- C08F2/00—Processes of polymerisation
- C08F2/38—Polymerisation using regulators, e.g. chain terminating agents, e.g. telomerisation
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- C08F2/00—Processes of polymerisation
- C08F2/44—Polymerisation in the presence of compounding ingredients, e.g. plasticisers, dyestuffs, fillers
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- C08F212/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
- C08F212/02—Monomers containing only one unsaturated aliphatic radical
- C08F212/04—Monomers containing only one unsaturated aliphatic radical containing one ring
- C08F212/06—Hydrocarbons
- C08F212/12—Monomers containing a branched unsaturated aliphatic radical or a ring substituted by an alkyl radical
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- C08F279/00—Macromolecular compounds obtained by polymerising monomers on to polymers of monomers having two or more carbon-to-carbon double bonds as defined in group C08F36/00
- C08F279/02—Macromolecular compounds obtained by polymerising monomers on to polymers of monomers having two or more carbon-to-carbon double bonds as defined in group C08F36/00 on to polymers of conjugated dienes
- C08F279/04—Vinyl aromatic monomers and nitriles as the only monomers
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- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L25/00—Compositions of, homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring; Compositions of derivatives of such polymers
- C08L25/02—Homopolymers or copolymers of hydrocarbons
- C08L25/04—Homopolymers or copolymers of styrene
- C08L25/08—Copolymers of styrene
- C08L25/12—Copolymers of styrene with unsaturated nitriles
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- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L25/00—Compositions of, homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring; Compositions of derivatives of such polymers
- C08L25/02—Homopolymers or copolymers of hydrocarbons
- C08L25/16—Homopolymers or copolymers of alkyl-substituted styrenes
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- C08L51/00—Compositions of graft polymers in which the grafted component is obtained by reactions only involving carbon-to-carbon unsaturated bonds; Compositions of derivatives of such polymers
- C08L51/06—Compositions of graft polymers in which the grafted component is obtained by reactions only involving carbon-to-carbon unsaturated bonds; Compositions of derivatives of such polymers grafted on to homopolymers or copolymers of aliphatic hydrocarbons containing only one carbon-to-carbon double bond
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F4/00—Polymerisation catalysts
- C08F4/40—Redox systems
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L2201/00—Properties
- C08L2201/08—Stabilised against heat, light or radiation or oxydation
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L2205/00—Polymer mixtures characterised by other features
- C08L2205/03—Polymer mixtures characterised by other features containing three or more polymers in a blend
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L2207/00—Properties characterising the ingredient of the composition
- C08L2207/53—Core-shell polymer
Definitions
- the present invention relates to a method for producing a heat resistant resin, a heat resistant resin and a heat resistant ABS resin composition, in particular, to prepare a heat resistant resin with a high polymerization conversion rate and a reduced polymerization coagulum under a short polymerization time and fine when agglomerated. It provides a manufacturing method that can also reduce the content, from the heat-resistant resin and heat-resistant ABS resin composition with improved heat deformation temperature and processability.
- the emulsion-polymerized heat-resistant SAN has the advantages of having a high Tg and a high molecular weight, while the polymerization takes a long time and the workability and productivity due to the high temperature and pressurization process in the flocculation / drying process is inferior.
- Patent Document 1 US4340723 A
- Patent Document 2 US5171814 A
- heat-resistant resins can be prepared with high polymerization conversion and reduced polymerization coagulum under a short polymerization time, and can also reduce fine content during aggregation.
- the technology has been confirmed and the present invention has been completed.
- an object of the present invention is to provide a method for producing a heat resistant resin having a polymerization rate and cohesiveness, and a heat resistant resin obtained therefrom and a heat resistant ABS resin composition having improved heat deformation temperature and processability.
- the glass transition temperature (Tg) is at least 140 °C, the average particle diameter of 300 to 700 Pa, the weight average under 70 to 80 parts by weight of the heat-resistant compound monomer and 30 to 20 parts by weight of the vinyl cyan compound monomer Polymerizing a heat resistant compound-vinylcyan compound-based seed having a molecular weight (Mw) of 200,000 to 300,000 g / mol; And (b) a shell surrounding the seed, wherein the glass transition temperature (Tg) is 135 to 145 ° C. under 30 to 80 parts by weight of the seed and 70 to 20 parts by weight of the heat resistant compound monomer and the vinyl cyan compound monomer, and a weight average molecular weight (Mw). It provides a method of producing a heat-resistant resin comprising ;; polymerizing a heat-resistant compound-vinyl cyan compound-based shell having a) 100,000 to 150,000 g / mol.
- the heat-resistant compound-vinylcyan compound seed and the heat-resistant compound-vinylcyan compound shell surrounding the seed have a structure having a weight average molecular weight (Mw) of 100,000 to 150,000 g / mol and a glass transition temperature (Tg). ) Provides a heat resistant SAN resin having 135 to 145 °C.
- thermoplastic ABS resin composition comprising the above-mentioned heat-resistant SAN resin, the heat deformation temperature (HDT) exceeds 100 °C, the melt index (MI) is 3.5 to 4.0.
- a heat-resistant resin is prepared from a high polymerization conversion rate and a reduced coagulum under a short polymerization time, and provides a manufacturing method that can also reduce the fine content during aggregation, and from the heat resistance It is effective to provide a heat-resistant ABS resin composition with improved resin and heat distortion temperature and workability.
- Heat-resistant resin manufacturing method according to the invention can be carried out in the following steps as a specific example:
- the method for producing a heat resistant resin according to the present invention may be carried out in another example by the following steps:
- the heat resistant compounds of step (a) and (b) may be alpha methyl styrene, for example, and in this case, there is an effect of excellent heat resistance and balance of physical properties.
- the vinyl cyan compound of step (a) and (b) may be at least one selected from the group consisting of acrylonitrile, methacrylonitrile and ethacrylonitrile, and in this case, the effect of excellent heat resistance and mechanical properties is excellent. have.
- step (a) has a technical feature to meet the lower glass transition temperature lower limit proposed in order to offset the decrease in the glass transition temperature (Tg) due to the formation of a lower molecular weight in step (b).
- the weight average molecular weight (Mw) is less than 200,000 g / mol may cause a decrease in the glass transition temperature, if it exceeds 300,000 g / mol, the molding processability of the final polymer using the prepared seed may be lowered Can be.
- step (a) if the average particle diameter is less than 300 kPa, the emulsifier is excessively used to obtain the polymer, so that the glass transition temperature of the final polymer may be lowered, and if the average particle diameter exceeds 700 kPa, the shell in the subsequent step (b) It is not expected to increase the polymerization rate during the polymerization.
- the glass transition temperature of the entire resin after the shell polymerization may be sharply lowered.
- the total time required for polymerization in steps (a) and (b) is, for example, within 4 hours, 3 to 4 hours, or 3 hours, and the polymerization conversion rates of steps (a) and (b) are each examples, It may be 98.5% or more, 99.0% or more, or 99.0 to 99.5%, and the residual monomer content is reduced within this range to have excellent heat resistance.
- the (meth) acrylic acid alkyl ester monomer and the aromatic vinyl compound monomer are contained within 2 to 5 parts by weight, or 3 to 5 parts by weight of 20 to 30 parts by weight of the vinyl cyan compound monomer. And (meth) acrylic acid alkyl ester monomers or aromatic vinyl compound monomers (except alphamethylstyrene).
- (meth) acrylic acid alkyl ester examples include (meth) acrylic acid methyl ester, (meth) acrylic acid ethyl ester, (meth) acrylic acid propyl ester, (meth) acrylic acid 2-ethylhexyl ester, (meth) acrylic acid decyl ester and (meth ) Acrylic acid lauryl ester may be one or more selected from the group consisting of, in this case there is an excellent effect of mechanical and physical properties balance.
- the aromatic vinyl compound may be at least one selected from the group consisting of styrene, paramethyl styrene, orthomethyl styrene, paraethyl styrene, and vinyl toluene, for example, in this case, the mechanical properties and the physical properties are excellent in balance.
- Step (a) is a specific example, (a-1) 70 to 80 parts by weight of the heat-resistant compound monomer, 8 to 10 parts by weight of the vinyl cyan compound monomer, (meth) acrylic acid alkyl ester monomer and aromatic vinyl compound monomer (except alphamethylstyrene) ) At least one selected from 0 to 2 parts by weight under a saturated hydrocarbon-based emulsifier of C 12 to C 18 to perform emulsion polymerization; (a-2) emulsion polymerization by continuously adding 5 to 15 parts by weight of a vinylcyan compound monomer at a point of polymerization conversion rate of 83 to 88% under a saturated hydrocarbon emulsifier of C 12 to C 18 ; And (a-3) polymerizing a batch of 2 to 8 parts by weight of the vinyl cyan compound monomer at a polymerization conversion rate of 92 to 96%.
- Step (a) is another example, (a-1) 72 to 78 parts by weight of the heat-resistant compound monomer, 8 to 10 parts by weight of the vinyl cyan compound monomer, (meth) acrylic acid alkyl ester monomer and aromatic vinyl compound monomer (alphamethylstyrene 0 to 2 parts by weight of at least one selected from C) to a saturated hydrocarbon-based emulsifier of C 12 to C 18 in a batch step of emulsion polymerization; (a-2) emulsion polymerization by continuously adding 7 to 12 parts by weight of a vinyl cyan compound monomer under a saturated hydrocarbon emulsifier of C 12 to C 18 at a polymerization conversion rate of 84 to 86%; And (a-3) polymerizing 3 to 6 parts by weight of the vinyl cyan compound monomer in a batch at 93 to 95% of the polymerization conversion rate.
- a-1 72 to 78 parts by weight of the heat-resistant compound monomer, 8 to 10 parts by weight of the vinyl cyan compound
- At least one selected from the (meth) acrylic acid alkyl ester monomer and the aromatic vinyl compound monomer (except alphamethylstyrene) may be included, for example, in an amount of 0.1 to 2 parts by weight.
- the saturated hydrocarbon-based emulsifier of C 12 to C 18 for example, an alkali salt of lauric acid, an alkali salt of stearic acid, an alkali salt of palmitic acid, and the like can be used.
- the saturated hydrocarbon-based emulsifier of C 12 to C 18 may be included as 1.4 to 2.9 parts by weight, or 2.0 to 2.9 parts by weight in step (a-1) based on 100 parts by weight of the total monomers constituting step (a).
- the total amount of the emulsifier used in the step (a-1) in step (a-2) may be included in an amount of 2.1 to 4.0 parts by weight, or 2.1 to 3.5 parts by weight, and prepared in step (a) within this range.
- the average particle diameter of the seeds, the weight average molecular weight (Mw) and the glass transition temperature (Tg) has the effect that can be adjusted appropriately.
- a mercaptan molecular weight regulator may be applied together with an initiator, if necessary.
- the mercaptan molecular weight modifier may be included in 0.1 to 0.2 parts by weight based on a total of 100 parts by weight of the total monomer constituting the step (a).
- the initiator may be used in combination with a water-soluble initiator such as potassium persulfate or a fat-soluble peroxide initiator in combination with the oxidation-reduction catalyst, it is preferable to use a fat-soluble peroxide initiator to polymerize at the initial 70 °C or less.
- the redox catalyst for example, dextrose, sodium pyrolate, ferrous sulfate, and the like may be used.
- Specific examples of the redox catalyst include dextrose 0.025 to 100 parts by weight based on 100 parts by weight of the total monomers constituting the step (a). 0.035 parts by weight, sodium pyrrolate 0.05 to 0.06 parts by weight, ferrous sulfate 0.005 to 0.0015 parts by weight.
- the step (a) may be carried out at 30 to 80 °C as an example, for example in the step (a-1) 50 to 70 °C, (a-2) and (a-3) respectively 70 to 80 °C Can be.
- the heat resistant compound monomer may be included in an amount of 5 to 60 parts by weight, or 10 to 55 parts by weight based on 100 parts by weight of the total seed and the total monomers constituting the shell.
- the vinyl cyan compound monomer may be included in an amount of 5 to 20 parts by weight, or 10 to 15 parts by weight, based on 100 parts by weight of the total monomers and the seed constituting the shell.
- step (b) may include (meth) acrylic acid alkyl ester monomers and aromatic vinyl compound monomers (alphamethyl) within 1 to 5 parts by weight, or 2 to 4 parts by weight of the vinyl cyan compound monomers. Styrene), or (meth) acrylic acid alkyl ester monomers or aromatic vinyl compound monomers (except alphamethylstyrene).
- (meth) acrylic acid alkyl ester examples include (meth) acrylic acid methyl ester, (meth) acrylic acid ethyl ester, (meth) acrylic acid propyl ester, (meth) acrylic acid 2-ethylhexyl ester, (meth) acrylic acid decyl ester and (meth ) Acrylic acid lauryl ester may be one or more selected from the group consisting of, in this case there is an excellent effect of mechanical and physical properties balance.
- the aromatic vinyl compound may be at least one selected from the group consisting of styrene, paramethyl styrene, orthomethyl styrene, paraethyl styrene, and vinyl toluene, for example, in this case, the mechanical properties and the physical properties are excellent in balance.
- Step (b) is a specific example, (b-1) 30 to 80 parts by weight of the seed, 7 to 45 parts by weight of the heat resistant compound monomer, 3 to 10 parts by weight of the vinyl cyan compound monomer and (meth) acrylic acid alkyl ester and aromatic vinyl compound 0 to 2 parts by weight of one or more selected from (excluding alphamethylstyrene), an emulsifier mixture of C 12 to C 18 saturated hydrocarbon-based emulsifiers and monomeric or polymeric emulsifiers having unsaturated double bonds, and C 6 to C 12 Carrying out a batch polymerization under a molecular weight regulator mixture of a mercaptan molecular weight regulator and a dimer molecular weight regulator; (b-2) At a 83 to 88% polymerization conversion rate, 3 to 10 parts by weight of the heat resistant compound monomer and 3 to 5 parts by weight of the vinyl cyan compound monomer are continuously added under a saturated hydrocarbon emulsifier of C 12 to C 18 to perform emul
- Step (b) is another example, (b-1) 30 to 80 parts by weight of the seed, 7 to 45 parts by weight of the heat resistant compound monomer, 3 to 10 parts by weight of the vinyl cyan compound monomer and (meth) acrylic acid alkyl ester and aromatic vinyl 0 to 2 parts by weight of at least one selected from compounds (except alphamethylstyrene), an emulsifier mixture of C 12 to C 18 saturated hydrocarbon-based emulsifiers and monomeric or polymeric emulsifiers having unsaturated double bonds, and C 6 to C 12 Carrying out a batch polymerization under a mixture of a mercaptan molecular weight regulator and a molecular weight regulator of a dimer-based molecular weight regulator; (b-2) at a polymerization conversion rate of 84 to 86%, continuously adding 3 to 10 parts by weight of the heat resistant compound monomer and 3 to 5 parts by weight of the vinyl cyan compound monomer under a saturated hydrocarbon emulsifier of C 12 to C 18 to perform
- At least one selected from the (meth) acrylic acid alkyl ester monomer and the aromatic vinyl compound monomer (except alphamethylstyrene) may be included, for example, in an amount of 0.1 to 2 parts by weight.
- the molecular weight regulator mixture of C 6 to C 12 mercaptan molecular weight regulator and dimer-based molecular weight regulator is, for example, a weight ratio of 50:50 to 90:10, or 60:40 to 90:10 As a weight ratio, it may be included in 0.2 to 0.5 parts by weight, or 0.2 to 0.4 parts by weight, based on 100 parts by weight of the total monomers and the seed constituting the shell of the step (b), polymerization conversion rate, coagulation content, The reaction time, glass transition temperature and weight average molecular weight and the like can be adjusted appropriately.
- the dimer-based molecular weight modifier refers to alphamethylstyrene dimers, such as ASMD-alphamethylstyrene, unless otherwise specified.
- the molecular weight modifier may be applied with an initiator, for example.
- the initiator may be used in combination with a water-soluble initiator such as potassium persulfate or an oil-soluble peroxide initiator and an oxidation-reduction catalyst.
- a water-soluble initiator such as potassium persulfate or an oil-soluble peroxide initiator and an oxidation-reduction catalyst.
- a fat-soluble peroxide initiator is preferable.
- the redox catalyst may include dextrose, sodium pyrolate, and ferrous sulfate, and specific examples thereof may include 0.035 parts by weight of dextrose, 0.06 parts by weight of sodium pyrolate, and 0.0015 parts by weight of ferrous sulfate. .
- the emulsifier mixture of a C 12 to C 18 saturated hydrocarbon-based emulsifier and an emulsifier having a low molecular weight unsaturated double bond is, for example, a weight ratio of 50:50 to 90:10, or 60:40 to As a weight ratio of 90:10, it may be included in 0.5 to 1.0 parts by weight, or 0.6 to 0.9 parts by weight, based on 100 parts by weight of the total monomers and the total monomers constituting the shell of the step (b).
- the emulsifier having a low molecular weight unsaturated double bond may be a monomolecular emulsifier having an unsaturated double bond and copolymerizable with a monomer.
- an anionic emulsifier or a neutral emulsifier having an allyl group, an alkenyl group, or a propenyl group can be used.
- Specific examples of the anionic emulsifier having an allyl group include sulfate salts of polyoxyethylene and allylglycidyl nonylphenyl ether, and anionic emulsifiers having the alkenyl group include alkenyl succinate, and the like.
- neutral emulsifiers examples include ether series of polyoxyethylene allylglycidyl nonylphenyl, and the like.
- Anionic emulsifiers having a propenyl group include ammonium sulfate salts of polyoxyethylene allylglycidyl nonylpropenyl phenyl ether. have.
- the saturated hydrocarbon-based emulsifier of C 12 to C 18 is 0.2 to 0.5 parts by weight, based on 100 parts by weight of the total monomers and the seed constituting the shell of the step (b), for example, Or 0.2 to 0.4 parts by weight.
- Step (b) may be performed at 30 to 80 ° C., for example, at 50 to 70 ° C. in step (b-1), and 70 to 80 ° C. at step (b-2) and (b-3), respectively. Can be.
- Coagulation of the step (b) polymerization may be, for example, 0.03% by weight or less, 0.018% by weight or less, or 0.012 to 0.018% by weight.
- the polymer may be aggregated within a temperature range normally used, and may be aggregated at 100 to 130 ° C or 100 to 120 ° C as a specific example.
- the coagulant used in the coagulation may be used, for example, acid coagulants such as sulfuric acid, phosphoric acid and hydrochloric acid, or salt coagulants such as magnesium sulfate and calcium chloride, alone or in combination, and 0.1 to 5 parts by weight based on 100 parts by weight of the total resin solids. Can be used within the range.
- acid coagulants such as sulfuric acid, phosphoric acid and hydrochloric acid
- salt coagulants such as magnesium sulfate and calcium chloride
- the method of preparing the heat resistant resin can shorten the polymerization reaction time by achieving the above-described two-step polymerization method, achieve polymerization stability, and at the same time, effective aggregation can be performed without deteriorating the physical properties of the heat resistant ABS in the polymer agglomeration process using the same. Efficient
- a heat-resistant SAN resin obtained by the above-described method has a structure of a heat-resistant compound-vinyl cyan compound seed and a heat-resistant compound-vinyl cyan compound shell surrounding the seed, the weight average molecular weight of 100,000 to 150,000 g / mol, Or 120,000 to 140,000 g / mol and a glass transition temperature of 135 to 145 ° C, or 137 to 142 ° C.
- the heat-resistant ABS resin composition comprising the heat-resistant SAN resin and ABS resin described above, the heat distortion temperature (HDT) is more than 100 °C, or 105 to 108 °C, the melt index (MI) is 3.5 to 4.0 Resin can be provided.
- HDT heat distortion temperature
- MI melt index
- the SAN resin may be included in 50 to 80 parts by weight, or 60 to 80 parts by weight, and the ABS resin may be included in 50 to 20 parts by weight or 40 to 20 parts by weight.
- the ABS resin may be, for example, a dry powder type having a rubber content of 30 to 80% by weight, or 40 to 70% by weight.
- ABS resin composition may include additives such as lubricants and heat stabilizers within the range that does not affect the physical properties, if necessary.
- a redox catalyst consisting of 0.03 parts by weight of t-butylhydroperoxide, 0.035 parts by weight of dextrose, 0.06 parts by weight of sodium pyrolate, and 0.0015 parts by weight of ferrous sulfate and polymerized for an additional 1 hour.
- a redox catalyst consisting of 0.03 parts by weight of t-butylhydroperoxide, 0.035 parts by weight of dextrose, 0.06 parts by weight of sodium pyrolate, and 0.0015 parts by weight of ferrous sulfate and polymerized for an additional 1 hour.
- the polymerization conversion rate of the final polymer was 99.5%, the average particle size was 350 ⁇ , and the glass transition temperature of the sample obtained by drying the obtained latex at 160 ° C. for 30 minutes was 142 ° C., and the weight average molecular weight was 250,000 g /. mol level.
- the polymerization conversion rate is 1.5 g of the prepared latex in a 150 °C hot air dryer after drying for 15 minutes to determine the total solids content (TSC) to calculate the weight, and calculated the conversion rate in the following formula 1,
- TSC total solids content
- the average particle diameter was measured by diluting the prepared latex 1 g in distilled water 100 g, using a light scattering measuring device (Nicomp), and recorded the number average particle diameter of the measuring device.
- step 1 preparation of S1
- 75 parts by weight of alphamethylstyrene, 8 parts by weight of acrylonitrile and 2 parts by weight of methyl methacrylate are 2.0 parts by weight of potassium laurate Except that was added and polymerized together, it was carried out in the same manner as in (a) seed polymerization step 1 (manufactured by S1). Physical properties for the latex are shown together in Table 1.
- step 1 preparation of S1
- the polymerization is carried out by adding 3.5 parts by weight of potassium lauryl acid, which is initially added in a batch, and the polymerization conversion rate is 85% after which potassium lauryl acid is continuously added in the form of an emulsion.
- an oxidation-reduction catalyst consisting of 0.02 parts by weight of t-butyl hydroperoxide, 0.035 parts by weight of dextrose, 0.06 parts by weight of sodium pyrolate and 0.0015 parts by weight of ferrous sulfate was collectively administered, and the polymerization was performed while raising the temperature to 70 ° C. for 1 hour. Was carried out. The polymerization conversion was 85% level.
- an emulsion composed of 100 parts by weight of ion-exchanged water, 10 parts by weight of alphamethylstyrene, 3 parts by weight of acrylonitrile, and 0.3 parts by weight of potassium laurate was heated to 75 ° C. for 1 hour while being continuously added.
- the polymerization conversion was at 94% level.
- the polymerization conversion rate of the obtained final polymer was 99.5% level, the weight average molecular weight was 120,000 g / mol, the latex obtained was agglomerated using 1 part by weight of CaCl 2 at 100 to 120 ° C and then dried at 160 ° C for 30 minutes The glass transition temperature was about 137 °C.
- Example 2 The same experiment as in Example 1 was repeated except that the latex S1, which was initially added, was replaced with S3, and was added in the manner shown in Table 2 below.
- Example 2 The same experiment as in Example 1 was carried out in the same manner as in Example 1, except that the mercaptan molecular weight regulator was not included, the dimer-based molecular weight regulator was used in 0.5 parts by weight, and was added in the manner shown in Table 2 below. Repeated.
- step (a-1) 75 parts by weight of alphamethylstyrene and 10 parts by weight of acrylonitrile are added without adding a seed in step (a-1), 1.5 parts by weight of Fatty soap (fatty acid emulsifier) is added, and in step (a-2), acryl
- Fatty soap fatty acid emulsifier
- step (a-2) acryl
- 1.0 part by weight of fatty acid emulsifier was added based on 10 parts by weight of ronitrile, and was added in the manner shown in Table 2.
- Example 2 The same experiment as in Example 1 was repeated except that the latex S1 was initially added to S4, and was added in the manner shown in Table 2 below.
- Coagulum (% by weight): The polymerized latex is filtered through a 200 mesh filter, and then the coagulum on the filter is dried in an oven at 80 ° C. to remove moisture. Calculated as a percentage.
- Glass transition temperature (Tg, °C) After drying the powder obtained through the aggregation for 30 minutes on an oven at 165 °C, the value measured at a temperature rising rate of 10 °C / min through a DSC instrument was recorded.
- Examples 1 to 3 subjected to the two-step polymerization according to the present invention is Comparative Example 3, which does not perform the two-step polymerization, or Comparative Example 1 using seeds (S3) having an inappropriate particle size range even if carried out. And it was confirmed that to provide a high polymerization conversion and polymerization stability and a high glass transition temperature in a short time compared to 2. In addition, in the case of Comparative Example 4 using the seed (S4) having a very small particle diameter, it was confirmed that the glass transition temperature is somewhat reduced.
- Fine (fine particle) content (% by weight): Particle diameters were measured using a standard mesh (No. 200 mesh) and expressed as percentages for the passage through 200 mesh.
- Examples 1 to 3 subjected to the two-step polymerization according to the present invention is Comparative Example 3, which does not perform the two-step polymerization, or Comparative Example 1 using the seed (S3) having an inappropriate particle size range even if performed. And it was confirmed that both the moisture content and the fine particles (fine) content compared to 2.
- Comparative Example 4 using a seed (S4) having a very small particle diameter as the emulsifier is added in excess, the cohesiveness is lowered under the same flocculant content, and thus, the water content improvement effect is insignificant, and the content of fine particles is fine. It was confirmed that the increase.
- MI melt index, g / 10 min
- HDT heat deformation temperature, ° C.
- Preparation Examples 1 to 3 prepared using Examples 1 to 3 subjected to two-step polymerization according to the present invention were prepared using Comparative Example 3, which was not subjected to two-step polymerization.
- Example 3 or two-step polymerization impact strength (IMP), melt index (MI) in a short time compared to Comparative Examples 1 and 2 prepared using Comparative Examples 1 and 2 using seeds (S3) having an inappropriate particle size range ) And the heat deflection temperature (HDT) were both improved.
- Comparative Preparation Example 4 prepared using Comparative Example 4 using a seed (S4) having a very small particle diameter it was confirmed that the impact strength and the heat deflection temperature (HDT) were lowered as the residual low molecular weight material was included in excess.
- IMP impact strength
- MI melt index
- HDT heat deflection temperature
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Abstract
Description
구분 | S1 | S2 | S3 | S4 | |
(a-1) 단계(일괄 투입) | 알파메틸스티렌(wt%)* | 75 | 75 | 75 | 75 |
아크릴로니트릴(wt%)* | 10 | 8 | 8 | 10 | |
메틸메타크릴레이트(wt%)* | - | 2 | 2 | - | |
(a-2) 단계(연속 투입) | 아크릴로니트릴(wt%)* | 10 | 10 | 10 | 10 |
(a-3) 단계(일괄 투입) | 아크릴로니트릴(wt%)* | 5 | 5 | 5 | 5 |
유화제 | (a-1) 단계내 사용량(phr:*100wt% 기준)/(a-2) 단계내 사용량(phr:*100wt% 기준) | 2.5/1.0 | 2.5/1.0 | 1.5/0.5 | 3.5/1.5 |
중합 전환율 | % | 99.5 | 99.0 | 99.0 | 99.9 |
평균 입자경 | Å | 350 | 450 | 800 | 250 |
중량평균 분자량 | g/mol | 250,000 | 250,000 | 200,000 | 250,000 |
유리전이온도 | ℃ | 142 | 140 | 140 | 140 |
구분 | 실시예 | 비교예 | ||||||
1 | 2 | 3 | 1 | 2 | 3 | 4 | ||
(b-1) 단계(일괄 투입) | 시드(wt%)* | 30(S1) | 80(S1) | 80(S2) | 30(S3) | 30(S3) | - | 30(S4) |
알파메틸스티렌(wt%)* | 45 | 7 | 7 | 45 | 45 | 75 | 45 | |
아크릴로니트릴(wt%)* | 10 | 3 | 3 | 10 | 10 | 10 | 10 | |
(b-2) 단계(연속 투입) | 알파메틸스티렌(wt%)* | 10 | 3 | 3 | 10 | 10 | 10 | 10 |
아크릴로니트릴(wt%)* | 3 | 5 | 5 | 3 | 3 | - | 3 | |
(b-3) 단계(일괄 투입) | 아크릴로니트릴(wt%)* | 2 | 2 | 2 | 2 | 2 | 5 | 2 |
멀캅탄류 분자량조절제 | Phr(*100wt% 기준) | 0.3 | 0.3 | 0.3 | 0.3 | - | 0.2 | 0.3 |
다이머계 분자량 조절제 | Phr(*100wt% 기준) | 0.2 | 0.2 | 0.2 | 0.2 | 0.5 | - | 0.2 |
중합 전환율 | % | 99.5 | 99.2 | 98.7 | 95.2 | 94.3 | 96.5 | 99.7 |
응고분 | 중량% | 0.014 | 0.012 | 0.018 | 0.320 | 0.470 | 0.270 | 0.01 |
반응시간 | Hr | 3.0 | 3.0 | 3.0 | 6.0 | 8.0 | 12.0 | 3.0 |
중량평균 분자량 | g/mol | 120,000 | 140,000 | 130,000 | 80,000 | 100,000 | 220,000 | 130,000 |
유리전이온도 | ℃ | 137 | 142 | 140 | 132 | 118 | 135 | 135 |
응집 물성 | 실시예 | 비교예 | |||||
1 | 2 | 3 | 1 | 2 | 3 | 4 | |
함수율(%) | 27 | 30 | 32 | 28 | 25 | 75 | 45 |
파인 함량(중량 %) | 10 | 18 | 15 | 5 | 2 | 32 | 20 |
내열 ABS 물성 | 제조예 | 비교제조예 | |||||
1 | 2 | 3 | 1 | 2 | 3 | 4 | |
IMP(1/4") | 17 | 18 | 17 | 14 | 15 | 18 | 16 |
MI(g/10 min) | 4.0 | 3.5 | 3.7 | 4.5 | 4.3 | 2.5 | 4.5 |
HDT(℃) | 105 | 108 | 106 | 97 | 95 | 100 | 102 |
Claims (16)
- (a) 내열성 화합물 단량체 70 내지 80 중량부 및 비닐시안 화합물 단량체 30 내지 20 중량부를 포함하며, 유리전이온도가 140 ℃ 이상이고, 평균 입자경이 300 내지 700 Å이며, 중량평균 분자량이 200,000 내지 300,000 g/mol인 내열성 화합물-비닐시안 화합물계 시드를 중합하는 단계; 및(b) 상기 시드를 감싸는 쉘로서, 시드 30 내지 80 중량부 및 내열성 화합물 단량체와 비닐시안 화합물 단량체 70 내지 20 중량부를 포함하며, 유리전이온도가 135 내지 145 ℃이고, 중량평균 분자량이 100,000 내지 150,000 g/mol인 내열성 화합물-비닐시안 화합물계 쉘을 중합하는 단계;를 포함하는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (a) 단계와 (b) 단계의 중합 총 소요시간은 4시간 이내로서, (a) 단계와 (b) 단계의 중합 전환율은 각각 98.5 % 이상인 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (a) 단계는 비닐시안 화합물 단량체 20 내지 30 중량부 중 2 내지 5 중량부의 범위 내에서 (메트)아크릴산 알킬 에스테르 단량체 및 방향족 비닐 화합물 단량체(알파메틸스티렌 제외)에서 선택된 1종 이상을 포함하는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (a) 단계는 (a-1) 내열성 화합물 단량체 70 내지 80 중량부, 비닐시안 화합물 단량체 8 내지 10 중량부, (메트)아크릴산 알킬 에스테르 단량체 및 방향족 비닐 화합물 단량체(알파메틸스티렌 제외) 중에서 선택된 1종 이상 0 내지 2 중량부를 C12 내지 C18의 포화 탄화수소계 유화제 하에 일괄 투입하여 유화 중합하는 단계;(a-2) 중합 전환율 83 내지 88 % 지점에서, 비닐시안 화합물 단량체 5 내지 15 중량부를 C12 내지 C18의 포화 탄화수소계 유화제 하에 연속 투입하여 유화 중합하는 단계; 및(a-3) 중합 전환율 92 내지 96 % 지점에서, 비닐시안 화합물 단량체 2 내지 8 중량부를 일괄 투입하여 중합하는 단계;를 포함하여 수행되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제4항에 있어서,상기 (a-1) 단계의 유화제는 상기 (a) 단계를 구성하는 전체 단량체 총 100 중량부 기준, 1.4 내지 2.9 중량부로 포함되고, (a-2) 단계의 유화제는 상기 (a-1) 단계의 유화제 사용량과의 총 합량이 2.1 내지 4.0 중량부 함량 범위 내로 포함되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (b) 단계에서, 상기 내열성 화합물 단량체는 쉘을 구성하는 시드와 전체 단량체 총 100 중량부 기준, 5 내지 60 중량부로 포함되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (b) 단계에서, 상기 비닐시안 화합물 단량체는 쉘을 구성하는 시드와 전체 단량체 총 100 중량부 기준, 5 내지 20 중량부로 포함되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제7항에 있어서,상기 (b) 단계는 비닐시안 화합물 단량체 5 내지 20 중량부 중 1 내지 5 중량부의 범위 내에서 (메트)아크릴산 알킬 에스테르 단량체 및 방향족 비닐 화합물 단량체(알파메틸스티렌 제외)에서 선택된 1종 이상을 포함하는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (b) 단계는, (b-1) 시드 30 내지 80 중량부, 내열성 화합물 단량체 7 내지 45 중량부, 비닐시안 화합물 단량체 3 내지 10 중량부 및 (메트)아크릴산 알킬 에스테르와 방향족 비닐 화합물(알파메틸스티렌 제외) 중에서 선택된 1종 이상 0 내지 2 중량부를, C12 내지 C18의 포화 탄화수소계 유화제와 불포화 이중결합을 가진 단량체형 혹은 고분자형 유화제의 유화제 혼합물, 및 C6 내지 C12의 멀캅탄류 분자량 조절제 및 다이머계 분자량 조절제의 분자량 조절제 혼합물 하에 일괄 투입하여 유화 중합하는 단계;(b-2) 중합 전환율 83 내지 88 % 지점에서, 내열성 화합물 단량체 3 내지 10 중량부, 비닐시안 화합물 단량체 3 내지 5 중량부를 C12 내지 C18의 포화 탄화수소계 유화제 하에 연속 투입하여 유화 중합하는 단계; 및(b-3) 중합 전환율 92 내지 96 % 지점에서, 비닐시안 화합물 단량체 1 내지 5 중량부를 일괄 투입하여 중합하는 단계;를 포함하여 수행되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제9항에 있어서,상기 (b-1) 단계에서, C6 내지 C12의 멀캅탄류 분자량 조절제 및 다이머계 분자량 조절제의 분자량 조절제 혼합물은 50:50 내지 90:10의 중량비로서, 상기 (b) 단계의 쉘을 구성하는 시드와 전체 단량체 총 100 중량부 기준, 0.2 내지 0.5 중량부로 포함되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (b-1) 단계에서, C12 내지 C18의 포화 탄화수소계 유화제 및 저분자량의 불포화 이중결합을 갖는 유화제의 유화제 혼합물은 50:50 내지 90:10의 중량비로서, 상기 (b) 단계의 쉘을 구성하는 시드와 전체 단량체 총 100 중량부 기준, 0.5 내지 1.0 중량부로 포함되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (b-2) 단계에서, C12 내지 C18의 포화 탄화수소계 유화제는 상기 (b) 단계의 쉘을 구성하는 시드와 전체 단량체 총 100 중량부 기준, 0.2 내지 0.5 중량부로 포함되는 것을 특징으로 하는 내열성 수지의 제조방법.
- 제1항에 있어서,상기 (b) 단계 중합의 응고분(coagulum)은 0.03 중량% 이하인 것을 특징으로 하는 내열성 수지의 제조방법.
- (a) 내열성 화합물 단량체 70 내지 80 중량부 및 비닐시안 화합물 단량체 30 내지 20 중량부를 포함하며, 유리전이온도가 140 ℃ 이상이고, 평균 입자경이 300 내지 700 Å이며, 중량평균 분자량이 200,000 내지 300,000 g/mol인 내열성 화합물-비닐시안 화합물계 시드; 및(b) 상기 시드를 감싸는 쉘로서, 시드 30 내지 80 중량부 및 내열성 화합물 단량체와 비닐시안 화합물 단량체 70 내지 20 중량부를 포함하며, 유리전이온도가 135 내지 145 ℃이고, 중량평균 분자량이 100,000 내지 150,000 g/mol인 내열성 화합물-비닐시안 화합물계 쉘;을 포함하는 것을 특징으로 하는 내열성 SAN 수지.
- 제14항에 있어서,상기 내열성 수지는 중량평균 분자량이 100,000 내지 150,000 g/mol이며, 유리전이온도가 135 내지 145 ℃인 것을 특징으로 하는 내열성 SAN 수지.
- 제14항의 내열성 SAN 수지 및 ABS 수지를 포함하고, 열변형온도(HDT)가 100 ℃ 초과이고, 용융지수(MI)가 3.5 내지 4.0인 것을 특징으로 하는 내열 ABS 수지 조성물.
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- 2015-10-02 KR KR1020150138837A patent/KR101706471B1/ko active IP Right Grant
- 2015-10-06 CN CN201580002156.6A patent/CN105705533B/zh active Active
- 2015-10-06 WO PCT/KR2015/010529 patent/WO2016056810A1/ko active Application Filing
- 2015-10-06 US US15/022,550 patent/US9845370B2/en active Active
- 2015-10-06 JP JP2016553199A patent/JP6304907B2/ja active Active
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US20160297909A1 (en) | 2016-10-13 |
KR20160041780A (ko) | 2016-04-18 |
CN105705533B (zh) | 2018-04-24 |
US9845370B2 (en) | 2017-12-19 |
JP6304907B2 (ja) | 2018-04-04 |
CN105705533A (zh) | 2016-06-22 |
KR101706471B1 (ko) | 2017-02-13 |
JP2016535165A (ja) | 2016-11-10 |
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