Foamable polystyrene production process

FIELD: polymer production.

SUBSTANCE: high molecular-weight foamable polystyrene is produced via two-step styrene polymerization, wherein, (i) in the first step, styrene is subjected to prepolymerization in presence of primary process initiator, fire-retardant - hexabromocyclododecane and its synergist dicumyl peroxide, chain growth regulator, and secondary initiator - O,O-tert-amyl-O-(2-hexyl) monoproxycarbonate, and (ii) in the second step, suspension polymerization proceeds in aqueous medium in presence of stabilizer - polyvinyl alcohol, chain growth regulator, third initiator - tert-butyl perbenzoate, and foaming agent. Invention is characterized by that, as primary process initiator, 2,5-bis(2-ethylhexanoyl-peroxy)-2,5-dimethylhexane is utilized and process is conducted at weight ratio of all three initiators 0.956:1:(1.14-2.5), respectively, until polymer with relative viscosity 2.1-2.3 is obtained.

EFFECT: enhanced process efficiency.

3 ex

 

The invention relates to petrochemistry, namely the production technology of polymeric materials, and can be used in the manufacture of expandable polystyrene used for the manufacture of foam for insulation boards, cold insulation, packaging, electronics packaging for food, etc.

A method of obtaining expandable polystyrene by multistage block-suspension polymerization, consisting of raw material preparation, terpolymerization of styrene in bulk, suspension of the prepolymer in the aqueous solution of the stabilizer - thin suspension of tricalcium phosphate, the final polymerization with the introduction of the blowing agent is isopentane, pressed pellet in the centrifuge, drying the pellets in a stream of hot air, sieving and packaging of the finished product (encyclopedia of polymers, t, s-571, M., 1977).

The disadvantage of this method is the use of polymerization initiators at the stage of terpolymerization and final polymerization with significantly different temperature settings decomposition of peroxides, which in the conditions of the reactor even under vigorous stirring leads to local overheating of the reaction mixture with getting polydisperse product on the molecular-mass distribution and the transition process in an unsupervised mode, may result in the formation is of glomerata ("goat")

The closest in technical essence and the achieved effect is a method for expandable polystyrene by multistage block-suspension polymerization, consisting of raw material preparation, terpolymerization of styrene in bulk in the presence of the initiator is benzoyl peroxide, flame retardant - hexabromocyclododecane flame retardant synergist - peroxide of Dicumyl, growth regulator circuit - dimer of alfamethylstyrene, the suspension of the prepolymer in the aqueous solution of the stabilizer is polyvinyl alcohol, the final polymerization using as an initiator of tertbutylbenzene, growth regulator circuit - dimer of alfamethylstyrene, calcium chloride, calcium carbonate, and with the introduction of the blowing agent is isopentane, pressed pellet in the centrifuge, drying the pellets in the stream hot air, sieving and packaging of the finished product (the Technology of plastics. Edited CEK, M.: Chemistry, 1976, s).

The disadvantage of the prototype is a relatively low molecular weight, expressed by the index of relative viscosity of 1.6 to 1.8 units.

Molecular weight is a value that defines the whole complex of physical and mechanical properties of the polymer, the area of its application, the processing technology and the efficiency of the recycling process it into products.

The aim of the proposed invented the I is to increase the molecular weight of the polymer unit 30000-40000 due to the replacement of classical monofunctional initiator process - benzoyl peroxide on bifunctional peroxide - 2.5 bis(2-ethylhexanoyl-peroxy)-2,5-dimethylhexane ("TRIGONOX-141") to produce expandable polystyrene index relative viscosity of 2.3 to 2.4%

This objective is achieved in that in a method of producing expandable polystyrene by multistage block-suspension polymerization, consisting of raw material preparation, terpolymerization of styrene in bulk in the presence of a polymerization initiator, a flame retardant synergist of the flame retardant and growth regulator circuit, the suspension of the prepolymer in the aqueous solution of the stabilizer is polyvinyl alcohol, the final polymerization in the presence of a polymerization initiator and growth regulator circuit with the introduction of the blowing agent is isopentane, pressed pellet in the centrifuge, drying the granules, sieving and packaging of the finished product. The process of terpolymerization and final polymerization of styrene is carried out using a three-component mixture of initiators, allowing to intensify the process while reducing the amount of initiator used in 7-8 times and the corresponding smoothing of ectothermy process. The components of the initiator mixture of different temperature parameters of decomposition that allows softly p is in excess of the temperature of the reaction mixture. For this stage terpolymerization loaded initiator of polymerization "Trigonox-141" 2,5 bis(2-ethylhexanoyl-peroxy)-2,5-dimethylhexane and additionally introduced the initiator O,O-treamill-O-(2-hexyl)-nonoperational ("Luperox-TAEK, Trigonox-131). At the final stage of polymerization is loaded initiator - tertbutylbenzene "Trigonox. Thus instead of 17 kg of benzoyl peroxide is loaded only 2.2 kg "Trigonox 141", which reduces the total consumption of the initiator on the process for the 14.5 to 14.8 kg per cycle occurring in the reactor with a volume of 10 m3.

The introduction of the proposed three-component mixture of peroxide polymerization initiators can significantly change the structure of the obtained polymer, providing a cost-effective suitability as raw materials for the whole range of foams (grade 15, 25, 35, 50), obtained from polystyrene for foaming, made a block-by suspension and foam-type "PENOPLEX"received extrusion method.

The proposed method is implemented on industrial reactors, and it is illustrated by the following examples.

Obtaining expandable polystyrene brands PSV-s

EXAMPLE 1 (analog). In a reactor with a capacity of 10 m3download demineralized water in a quantity of 2500 l, styrene in the amount of 5000 l include a mixer (40 rpm) and load the initiator on the imerissia - peroxide benzoyl - 11.5 kg (1) calculated on the anhydrous initiator, the flame retardant hexabromocyclododecane (32.2 kg in two to 16,1 kg to avoid the formation of lumps), the synergist of the flame retardant - peroxide Dicumyl (9,0 kg) and growth regulator circuit - dimer of alpha - methylstyrene - 0.5 liter Mass homogenized using a mixer for 20-30 minutes, after which the rotation speed of the agitator is reduced to 30 rpm and produce purging with nitrogen and at a residual pressure of 0.5 MPa, the reaction mass is heated to 80±2° for 1-1,5 hours. After 1.5-2 hours after the temperature specified and subsequently every 20 minutes determine the viscosity of the polymer and the conversion of monomer to achieve the degree of conversion ˜37-42% (2-2 .5 hours). If agreed conversion and viscosity of 10-15 seconds is loaded with 0.5 liters of dimer of alpha-methylstyrene, reduce speed of mixer until 26 rpm and dosed 2500-2600 l of a solution of the stabilizer is polyvinyl alcohol (PVA) concentration of 0.33 - 0.34% and the solution of calcium chloride in the solution of PVA concentration to 1.3-1.4% CaCl2in the amount of 10 kg and produce the dispersion of the mass. At this speed mixers vary to provide the necessary particle size distribution of beads in the range of 0.4-2.3 mm with a visual quality control breakdown. After loading solution of PVA with a stable breakdown of the prepolymer add for you is animania pH (less than 5.5) up to 0.5 kg of calcium carbonate. Add initiator - tertbutylbenzene in the amount of 7.9 kg (2), the reactor sealed, provide positive pressure of nitrogen to a pressure of 2.5 MPa and 15 minutes for 0.5 hours injected foaming agent is isopentane in the amount of 500 liters at a temperature of 50 plus or minus 2°and the reaction mass is heated for 30-40 minutes until the 80°C and maintained at this temperature for 5 hours to implement the suspension polymerization. The ratio of the initiators of 1:2 is equal to 1.45:1.0 in. After this time the reaction mixture is heated to 85°C for 0.5 hour and incubated for 0.5 hour, after which the temperature was raised to 115°C and maintained at this temperature for 4.5 hours. Upon completion of the polymerization, the suspension is cooled to 40°and the pulp through the sieve is pumped into a buffer tank, after which the beads are washed on a belt filter press in the centrifuge, is subjected to drying in a fluidized layer at a temperature of polymer 35-40°and with a moisture content of 0.8-1.5% of send in the silos of the finished product.

The relative viscosity is 1,5-1,6%, which corresponds (approximately) 120000-130000 units molecular weight.

The relative viscosity is determined by the ratio of the kinematic viscosities of pure solvent - benzene and 1%-aqueous solution therein of the polymer in the capillary viscometer type VPI.

EXAMPLE 2 (the prototype). Obtain foam is Osia polystyrene brand PSV-SV-NM(15. 20, TG, MD)

In a reactor with a capacity of 10 m3download demineralized water in a quantity of 2500 l, styrene in the amount of 5000 l include a mixer (40 rpm) and load the polymerization initiator is benzoyl peroxide, 16-17 kg (1) the flame retardant hexabromocyclododecane (33,2 kg in two to 16,1 kg to avoid the formation of lumps), the synergist of the flame retardant - peroxide Dicumyl (9,0 kg) and growth regulator circuit - dimer of alfamethylstyrene (0.5 l), and 50 kg of dust polystyrene marks MD and the polymerization initiator - O,O-treamill-O-(2 hexyl)-nonoperational in the amount of 2.0 kg Mass is homogenized using a mixer for 20-30 minutes, after which the rotation speed of the agitator is reduced to 30 rpm and produce purging with nitrogen and at a residual pressure of 0.5 MPa, the reaction mass is heated to 84-86°C for 1.0 to 1.5 hours. 1.5-2.0 hours after the temperature specified and subsequently every 20 minutes determine the viscosity and conversion of the prepolymer and the process lasts until the conversion of 37-42% with a viscosity of at Fordwich 9-15 sec. If we achieve these parameters terpolymerization ends, the speed of the agitator is reduced to 26 rpm, load 0.5 l dimer of alfamethylstyrene, pumped 2600-2700 l of a solution of the stabilizer is polyvinyl alcohol (PVA) with a concentration of 0.33-0.34 percent PVA and a solution of calcium chloride in the solution of PVA with a concentration of 1.3-1.4% of CaCl2in the Alceste 10 kg and produce the dispersion of the mass. Speed stirrers thus vary depending on the resulting particle size distribution in the range of 0.4-2% mm visual quality control breakdown. After loading solution of PVA with a stable breakdown adds to align pH (not less than 5.5) up to 0.5 kg of calcium carbonate. Add the initiator of the process - tertbutylbenzene in the amount of 4.7 kg (2), the reactor sealed, provide positive pressure of nitrogen to a pressure of 2.5 MPa and 15 minutes for 0.5 hours injected foaming agent is isopentane in the number of 300-450 kg at a temperature of 50-52°and the reaction mass is heated for 30-40 minutes until 83-87°C and maintained at this temperature for 5 hours for the first phase suspension polymerization. The ratio of the initiators of 1:2 is equal to 11.5:1,0. After this time the reaction mass is heated to 95°and incubated for 0.5 hour, after which the temperature was raised to 115°C and maintained at this temperature for 4.5 hours. Upon completion of the polymerization, the suspension is cooled to 40°and the pulp through the sieve is pumped into a buffer tank, after which the beads are washed on the filter, pressed in a centrifuge and dried to a moisture of 0.8,-1,5% in the dryer with a "fluidized bed", scatters (or diffused) into fractions and sent to the finished product silos

The relative viscosity is of 1.6-1.8 IU, which corresponds (approximately) 160000-170000 units molecular weight.

EXAMPLE 3. In a reactor with a capacity of 10 m3loaded 5000 l of styrene and at 40 rpm agitator load 30 kg dust polystyrene and 34 kg of a flame retardant - hexabromocyclododecane and all is homogenized for 30 minutes, Then the speed of the agitator is reduced to 30 rpm and the reactor is loaded: demineralized water in a quantity of 2500 l, the polymerization initiator is 2,5 bis (2-ethylhexanoyl-peroxy)-2,5-dimethylhexane "Trigonox-141" in the amount of 1.9-2.3 kg, the synergist of the flame retardant - dicumylperoxide - 9.6 kg, dimer of alfamethylstyrene - 0.4 l, the second initiator is a peroxide "Luperox TAEK" (or Trigonox-131") is 2.0 - 2.5 kg, and the reaction mixture is heated to 90-93°C for 1.5 to 2.0 hours.

The first attempt to determine the viscosity and conversion are selected through 1.5-2.0 hours after reaching the temperature regime and the process of terpolymerization ends with a viscosity of 10 to 14 seconds and conversion 37-43%.

If we achieve these parameters, the speed of the agitator is reduced to 26 rpm and put: 0.4 l dimer of alfamethylstyrene, 2500 l of a solution of polyvinyl alcohol of 0.33-0.34% of concentration, 9 kg of calcium chloride and 0.5 kg of calcium carbonate. The mass is homogenized and dispersed to the required granulometric composition.

The speed of the agitator is reduced to 19-20 rpm and entered the third initiator of 1.52-2.5 kg of tertbutylbenzene ("Trigonox-C")

The reactor is sealed, creating pressure nitrogen of 1.5-2.0 ATM and introduce the blowing agent is isopentane in the number of 250-350 kg

The temperature in the reactor rises to 93-97°C for 1-1,5 hours at this temperature, the process goes for 4 hours, then for 1.5 to 2.0 hours, the temperature rises up to 110-120°and at this temperature, the polymerization takes place even 3,5-5,0 hours.

Upon completion of the polymerization, the suspension is cooled to 40°C, the pulp through the sieve is pumped into a buffer tank, washed on the filter is dewatered in a centrifuge, dried in the dryer with a "fluidized bed" to a moisture content of 0.8 to 1.5%, diffuse (or diffuse) into fractions and sent to silos of finished products.

The relative viscosity of the polymer in this method, polymerization is 2.1 to 2.3%, which corresponds to 270000-290000 units molecular weight.

The proposed method is tested on an industrial scale at JSC "Angarsk polymer plant", the resulting product has received the diploma of 3 degrees at the international exhibition-fair in the city of Kemerovo in may 2005, and the diploma of 2 degrees in 2006, and also won medals at the international exhibition in Irkutsk in June 2005

A method of obtaining a high-molecular expandable polystyrene by the polymerization of styrene in two stages, the first of which are terpolymerization styrene in the presence of osnovnolozhenia process (1) of the flame retardant hexabromocyclododecane and its synergist - dicumylperoxide, growth regulator circuit, the second initiator - O,O-tert-amyl-O-(2 hexyl)-monoperoxyphthalate (2) with the subsequent suspension polymerization in the second stage in an aqueous medium in the presence of the stabilizer is polyvinyl alcohol, a growth regulator circuit, the third initiator tert-butylperbenzoate (3) and a blowing agent, characterized in that as the main initiator of the process use of 2,5-bis(2-ethylhexanoyl-peroxy)-2,5 dimethylhexane and the process is carried out at a mass ratio of the three initiators of 1:2:3 equal 0,956:1:(1,14-2,5), to obtain a polymer with a relative viscosity of 2.1 to 2.3.



 

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FIELD: chemical industry; methods of transition between the incompatible catalytic agents of the layer of the nuclei practically free from the contaminants.

SUBSTANCE: the invention is pertaining to the method of transition of the layer of the nuclei practically free from the contaminants from the first reaction of the polymerization to the second reaction of the polymerization incompatible with the first reaction of the polymerization in the gaseous-phase reactor. The invention describes the method of transition of the layer of the nuclei practically free from the contaminants from the first reaction of the polymerization with utilization of the first catalytic system for production of the first product of polymerization to the second reaction of the polymerization, in which they gain the second product of the polymerization, where the second reaction of the polymerization is incompatible with the first catalytic system for polymerization or the first product of the polymerization including the contaminants in the gaseous-phase reactor including:(a) realization of the sequential reactions of the polymerization in the gaseous-phase reactor after the first reaction of the polymerization with usage of the numerous catalytic systems, the numerous conditions in the reactor and the numerous torrents of the raw for production of the numerous products of the polymerization; (b) formation for each reaction of the polymerization of the layer of the nuclei practically free from the contaminants, which contains less than 100 particles per one million of the contaminants by means of removal of a part of the polymerization product from each reaction of the polymerization and the distillation or blowing out of the reactants and contaminants from each product of the polymerization; (c) the decontamination of the molecules of the catalytic agent grasped or contained in each polymeric product without a contact of the polymerization product with the surplus of the deactivator; (d) it is optional after the stage of the to conduct the distillation or blowing the reactants and contaminants out from each product of polymerization; (e)exercise storage of each layer of the nuclei practically non-containing contaminants separately in the storage container in the atmosphere of the dry inert gas for maintaining each layer of the nuclei practically non-containing contaminants; (f) stoppage of each sequential reaction of the polymerization; (g) removal of the contents of each sequential reaction of the polymerization from the gaseous-phase reactor so, that to prevent injection of the additional or essential quantity of the contaminants; (h) picking up the saved in the container layer of the nuclei practically free from the contaminants, which is compatible with the second reaction of the polymerization with respect to the product of polymerization or the catalytic system for the polymerization; (i) injection of the picked up practically non-containing contaminants layer of the nuclei in the gaseous-phase reactor so, that to prevent injection of the additional or essential quantities of the contaminants in the layer of the nuclei or in the reactor; (j) introduction of the second system of the raw in the gaseous-phase reactor; (k)introduction of the second catalytic system in the gaseous-phase reactor; and (l) realization of the second reaction of the polymerization. The technical result of the invention is reduction of the gaseous-phase reactor idle time.

EFFECT: the invention ensures reduction of the gaseous-phase reactor idle time.

13 cl, 7 dwg

FIELD: chemical industry; methods of transition between the incompatible catalytic agents of the layer of the nuclei practically free from the contaminants.

SUBSTANCE: the invention is pertaining to the method of transition of the layer of the nuclei practically free from the contaminants from the first reaction of the polymerization to the second reaction of the polymerization incompatible with the first reaction of the polymerization in the gaseous-phase reactor. The invention describes the method of transition of the layer of the nuclei practically free from the contaminants from the first reaction of the polymerization with utilization of the first catalytic system for production of the first product of polymerization to the second reaction of the polymerization, in which they gain the second product of the polymerization, where the second reaction of the polymerization is incompatible with the first catalytic system for polymerization or the first product of the polymerization including the contaminants in the gaseous-phase reactor including:(a) realization of the sequential reactions of the polymerization in the gaseous-phase reactor after the first reaction of the polymerization with usage of the numerous catalytic systems, the numerous conditions in the reactor and the numerous torrents of the raw for production of the numerous products of the polymerization; (b) formation for each reaction of the polymerization of the layer of the nuclei practically free from the contaminants, which contains less than 100 particles per one million of the contaminants by means of removal of a part of the polymerization product from each reaction of the polymerization and the distillation or blowing out of the reactants and contaminants from each product of the polymerization; (c) the decontamination of the molecules of the catalytic agent grasped or contained in each polymeric product without a contact of the polymerization product with the surplus of the deactivator; (d) it is optional after the stage of the to conduct the distillation or blowing the reactants and contaminants out from each product of polymerization; (e)exercise storage of each layer of the nuclei practically non-containing contaminants separately in the storage container in the atmosphere of the dry inert gas for maintaining each layer of the nuclei practically non-containing contaminants; (f) stoppage of each sequential reaction of the polymerization; (g) removal of the contents of each sequential reaction of the polymerization from the gaseous-phase reactor so, that to prevent injection of the additional or essential quantity of the contaminants; (h) picking up the saved in the container layer of the nuclei practically free from the contaminants, which is compatible with the second reaction of the polymerization with respect to the product of polymerization or the catalytic system for the polymerization; (i) injection of the picked up practically non-containing contaminants layer of the nuclei in the gaseous-phase reactor so, that to prevent injection of the additional or essential quantities of the contaminants in the layer of the nuclei or in the reactor; (j) introduction of the second system of the raw in the gaseous-phase reactor; (k)introduction of the second catalytic system in the gaseous-phase reactor; and (l) realization of the second reaction of the polymerization. The technical result of the invention is reduction of the gaseous-phase reactor idle time.

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15 cl, 2 dwg, 8 ex

FIELD: polymer materials.

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2 cl, 1 tbl, 5 ex

FIELD: rubber industry.

SUBSTANCE: invention relates to production of butadiene-styrene rubbers obtained via emulsion (co)polymerization, in particular to methods for isolation thereof out of latexes. A process for manufacturing filled butadiene-styrene rubber is described comprising butadiene-styrene copolymerization in emulsion in presence of radical initiators, stopping the process, adding oil filler and antioxidant, and degassing and isolating rubber out of latexes utilizing coagulation technique. Process is characterized by that, as filler and antioxidant, fiber-polymer-antioxidant composite is used, obtained by preliminarily mixing milled garneted fibers with hydrocarbon solution of a low-molecular weight polymer material. The latter is prepared on the basis of (i) still residue of recycled solvent (toluene) purification process in production of polybutadiene rubber and (ii) styrene modified by maleic anhydride and containing amine- or phenol-type antioxidant. Thus obtained composite is grinded and dispersed in surfactant-containing aqueous phase, after which low-boiling hydrocarbon fraction is distilled off and low-molecular weight polymer material and fibrous filler are added in amounts, respectively, 2-6 and 0.1-1.0% based on the weight of rubber.

EFFECT: reduced loss of rubber and environmental pollution at higher physicochemical characteristics of vulcanizates.

2 tbl, 11 ex

FIELD: rubber industry.

SUBSTANCE: invention relates to production of butadiene-styrene rubbers obtained via emulsion (co)polymerization, in particular to methods for isolation thereof out of latexes. A process for manufacturing filled butadiene-styrene rubber is described comprising butadiene-styrene copolymerization in emulsion in presence of radical initiators, stopping the process, adding filler and antioxidant, and degassing and isolating rubber out of latexes utilizing coagulation technique. Process is characterized by that, as filler and antioxidant, fiber-polymer-antioxidant composite is used, obtained by preliminarily mixing milled garneted fibers with hydrocarbon solution of a low-molecular weight polymer material. The latter is prepared on the basis of (i) still residue of recycled solvent (toluene) purification process in production of polybutadiene rubber and (ii) styrene modified by thermooxidation action and containing amine- or phenol-type antioxidant. Thus obtained composite is grinded and dispersed in surfactant-containing aqueous phase, after which low-boiling hydrocarbon fraction is distilled off and low-molecular weight polymer material and fibrous filler are added in amounts, respectively, 2-6 and 0.1-1.0% based on the weight of rubber.

EFFECT: reduced loss of rubber and environmental pollution at higher physicochemical characteristics of vulcanizates.

2 tbl, 11 ex

FIELD: rubber industry.

SUBSTANCE: invention relates to production of butadiene-styrene rubbers obtained via emulsion (co)polymerization, in particular to methods for isolation thereof out of latexes. A process for manufacturing filled butadiene-styrene rubber is described comprising butadiene-styrene copolymerization in emulsion in presence of radical initiators, stopping the process, adding oil filler and antioxidant, and degassing and isolating rubber out of latexes utilizing coagulation technique. Process is characterized by that, as filler and antioxidant, fiber-oil-antioxidant composite is used, obtained by preliminarily mixing milled garneted fibers with hydrocarbon solution of a low-molecular weight polymer material. The latter is prepared on the basis of still residue of styrene rectification in production of styrene from ethylbenzene, wherein styrene contains amine- or phenol-type antioxidant. Thus obtained composite is grinded and dispersed in surfactant-containing aqueous phase, after which low-boiling hydrocarbon fraction is distilled off and low-molecular weight polymer material and fibrous filler are added in amounts, respectively, 2-6 and 0.1-1.0% based on the weight of rubber.

EFFECT: reduced loss of rubber and environmental pollution at higher physicochemical characteristics of vulcanizates.

2 tbl, 11 ex

FIELD: rubber industry.

SUBSTANCE: invention relates to production of butadiene-styrene rubbers obtained via emulsion (co)polymerization, in particular to methods for isolation thereof out of latexes. A process for manufacturing filled butadiene-styrene rubber is described comprising butadiene-styrene copolymerization in emulsion in presence of radical initiators, stopping the process, adding oil filler and antioxidant, and degassing and isolating rubber out of latexes utilizing coagulation technique. Process is characterized by that, as filler and antioxidant, fiber-oil-antioxidant composite is used, obtained by preliminarily mixing milled garneted fibers with hydrocarbon solution of a low-molecular weight polymer material. The latter is prepared on the basis of still residue of styrene rectification in joint styrene/propylene oxide production, wherein styrene contains amine- or phenol-type antioxidant. Thus obtained composite is grinded and dispersed in surfactant-containing aqueous phase, after which low-boiling hydrocarbon fraction is distilled off and oil and fibrous filler are added in amounts, respectively, 2-6 and 0.1-1.0% based on the weight of rubber.

EFFECT: reduced loss of rubber and environmental pollution at higher physicochemical characteristics of vulcanizates.

2 tbl, 11 ex

FIELD: rubber industry.

SUBSTANCE: invention relates to production of butadiene-styrene rubbers obtained via emulsion (co)polymerization, in particular to methods for isolation thereof out of latexes. A process for manufacturing filled butadiene-styrene rubber is described comprising butadiene-styrene copolymerization in emulsion in presence of radical initiators, stopping the process, adding filler and antioxidant, and degassing and isolating rubber out of latexes utilizing coagulation technique. Process is characterized by that, as filler and antioxidant, fiber-polymer-antioxidant composite is used, obtained by preliminarily mixing milled garneted fibers with hydrocarbon solution of a low-molecular weight polymer material. The latter is prepared on the basis of (i) still residue of recycled solvent (toluene) purification process in production of polybutadiene rubber and (ii) styrene containing amine- or phenol-type antioxidant. Thus obtained composite is grinded and dispersed in surfactant-containing aqueous phase, after which low-boiling hydrocarbon fraction is distilled off and low-molecular weight polymer material and fibrous filler are added in amounts, respectively, 2-6 and 0.1-1.0% based on the weight of rubber.

EFFECT: reduced loss of rubber and environmental pollution at higher physicochemical characteristics of vulcanizates.

2 tbl, 11 ex

FIELD: petroleum chemistry, polymers, in particular styrene production.

SUBSTANCE: invention relates to method for production of phenol-based co-inhibitor of styrene thermopolymerization comprising acid condensation reaction of by-product-coking phenols containing mono- and dihydric phenols in mass ratio (1.3-2):1, with sulfuric acid at elevated temperature followed by catalytic oxidation of obtained phenol oligomer with hydrogen peroxide and neutralization of acid catalyst with sodium nitrite to produce modified product, wherein component ratio (mass pts) of extractive (total) by-product-coking phenols:sulfuric acid:hydrogen peroxide:sodium nitrite is 100:1.5-2.0:30-33.0:2.1-2.8. Also described is two-component composition for inhibiting of styrene thermopolymerization containing Mannich's base and co-inhibitor in mass ratio of 1:(1-2), wherein as co-inhibitor composition contains modified product of by-product-coking phenols.

EFFECT: effective inhibitor with good solubility in treated product; enhanced assortment of inhibitors.

3 cl, 2 tbl, 18 ex

FIELD: chemical technology.

SUBSTANCE: invention relates to a method for preparing a binding agent for a dry film photoresist of aqueous-alkaline development used in preparing a picture in making printed boards in radio- and electronic industry and as a component of paint and varnish covers and glues. Invention describes a single-step method for preparing a binding agent for a dry film photoresist of aqueous-alkaline development. At the first step method involves the copolymerization reaction of styrene with maleic anhydride in acetone medium in the presence of azo-bis-isobutyric acid dinitrile and hydroquinone at temperature 54-72°C for 2.5-3.0 h. At the second step method involves addition of 28.0-32.0 mas. p. p. of n-butanol to the reaction mixture and distilling off of 15.0-20.0 mas. p. p. of acetone followed by carrying out esterification of the copolymerization product at temperature 64-74° for 90-120 h. Prepared dry film photoresists of aqueous-alkaline development possess high stability (9-10 h) and enhanced galvanic-chemical resistance.

EFFECT: improved preparing method, improved and valuable properties of binding agent.

1 tbl, 6 ex

FIELD: polymer production.

SUBSTANCE: invention relates to processes of producing lacquer acrylic filming agents used in manufacture of masonry, road-line, and other paints. Process of invention is realized by two-step polymerization of butyl acrylate, methyl methacrylate, styrene, and methacrylic acid at ratio (40-5):(40-45):(10-14):(1-5) in toluene-ethyl acetate mixture, while portionwise feeding monomers/initiator mixture and repeatedly ageing reaction mixture. When conversion of monomers attains 82-85%, solution of butyl acrylate/styrene/methacrylic acid copolymer is additionally charged at ratio 42:57:1 dissolved in toluene/butanol (or ethanol) mixture or toluene/acetone mixture, or in toluene/ethyl acetate/ethanol/butanol mixture. Butyl acrylate/styrene/methacrylic acid copolymer is added in amount 1.77-4.0% based on concentration of principal substance. Toluene and ethyl acetate are used in proportion (0.1-1.0):1. In the first stage, 20-30% of butyl acrylate/methyl methacrylate/styrene/methacrylic acid mixture is added and, in the second stage, 70-90%. Thus obtained filming agent is characterized by high content of nonvolatile substances at rather low viscosity, high adhesion, good strength and film drying rate, low moisture absorption, high water and wear resistance.

EFFECT: improved performance characteristics of agent.

9 cl, 4 tbl, 7 ex

FIELD: chemical industry, chemical technology, polymers.

SUBSTANCE: invention relates to a method for preparing aqueous polymer dispersions of the multipurpose designation. Method for preparing an aqueous dispersion of styrene-acryl copolymer is carried out by preliminary emulsifying a mixture of acrylic monomers with styrene in the presence of emulsifying agent and the following aqueous-emulsion co-polymerization of the reaction mixture in the presence of initiating agent. Monomer mixture comprises additionally acrylamide, and method involves using ammonium persulfate and hydrogen peroxide as an initiating agent. Method involves the successive fractionally dosing feeding ammonium persulfate for two stages followed by addition of a mixture of polymethylsiloxane of molecular mass 55-1000 Da and iron sulfate in their mass ratio = (25-35):1 to the reaction mixture at stirring, cooling the reaction mass and its neutralization to pH = 5-6. Invention provides preparing the stable aqueous polymeric dispersion with diminished size of particles. Invention provides enhancing strength and water resistance of film prepared on its base.

EFFECT: improved preparing method.

1 tbl, 3 ex

FIELD: chemistry of polymers, chemical technology.

SUBSTANCE: invention describes a method for preparing polymers. Method involves anionic polymerization reaction of vinylaromatic monomers and coupled dienes or by their copolymerization reaction in medium of hydrocarbon solvent in the presence of lithium-organic initiating agent followed by functioning ends of polymeric chains. Method involves using monofunction amine-containing lithium-organic initiating agent as a lithium-organic initiating agent wherein active lithium is stabilized with vinyl or phenyl radical of the general formula: wherein R1 and R2 are similar or different alkyl or allyl radicals; R3 means vinyl or phenyl radical. The functioning ends of polymeric chains is carried out by treatment of "living" macromolecules with a coupling agent or by the functioning break, and (co)polymerization reaction is carried out in the presence of alkaline metal alkoxides or phenolates. Invention provides preparing polymer showing reduced hysteresis losses and high mechanical strength, and improved ecological indices.

EFFECT: improved preparing method.

2 cl, 5 tbl, 11 ex

The invention relates to a method for producing cross-linked polymers and resins

The invention relates to a method for vinylaromatic polymers may contain nitrile ethyleneamines

The invention relates to the functionalized copolymers of styrene and isoolefine

FIELD: chemistry of polymers, chemical technology.

SUBSTANCE: invention describes a method for preparing polymers. Method involves anionic polymerization reaction of vinylaromatic monomers and coupled dienes or by their copolymerization reaction in medium of hydrocarbon solvent in the presence of lithium-organic initiating agent followed by functioning ends of polymeric chains. Method involves using monofunction amine-containing lithium-organic initiating agent as a lithium-organic initiating agent wherein active lithium is stabilized with vinyl or phenyl radical of the general formula: wherein R1 and R2 are similar or different alkyl or allyl radicals; R3 means vinyl or phenyl radical. The functioning ends of polymeric chains is carried out by treatment of "living" macromolecules with a coupling agent or by the functioning break, and (co)polymerization reaction is carried out in the presence of alkaline metal alkoxides or phenolates. Invention provides preparing polymer showing reduced hysteresis losses and high mechanical strength, and improved ecological indices.

EFFECT: improved preparing method.

2 cl, 5 tbl, 11 ex

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