Packed composition containing compound subjected to exothermic decomposition |
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IPC classes for russian patent Packed composition containing compound subjected to exothermic decomposition (RU 2495052):
Method of producing graft copolymers of styrene on polydienes / 2478656
Invention relates to chemistry of high-molecular weight compounds and a method of producing graft copolymers of styrene on polydienes, which can be used in chemical industry when producing materials which combine properties of thermoelastic and thermoplastic polymers. This is achieved owing to that, in the method of producing graft copolymers of styrene on polydienes by chemical modification of polydienes, graft polymerisation of styrene on the modified polydiene in the absence of oxygen while heating and separating the graft copolymer, the polydiene used is a polymer selected from a group comprising 1,4-poly-2,3-dimethylbutadiene and 1,4-poly-2-alkkyldiene; chemical modification of the polydiene is carried out by dissolving the polydiene and a radical polymerisation initiator in an organic solvent, adding to the obtained solution 2-methyl-2-nitrosopropane in the absence of light with a wavelength longer than 500 nm, holding the mixture in the absence of oxygen and light with a wavelength longer than 500 nm for not less than 1 hour at temperature not lower than the decay temperature of the initiator, but not higher than 60°C, separating the obtained modified polymer by precipitation in an organic precipitant and drying the modified polymer, wherein before graft polymerisation, the modified polymer is dissolved in styrene or mixture thereof with at least one organic solvent which is miscible with styrene but does not precipitate polydiene and the formed graft copolymer, and oxygen is removed from the obtained solution, and graft polymerisation is carried out at temperature of 90-140°C in the presence of a radical polymerisation initiator whose half-life is not more than 30 minutes at polymerisation temperature.
Activating solution / 2470034
Invention relates to activating solutions containing a complexing agent. Described is use of the activating solution for curing unsaturated polyester (UP) resin or acrylic resin, said solution containing a complexing agent selected from a group consisting of complexing agents having a nitrogen atom and a hydroxyl group, and bipyridine, a metal salt selected from a group consisting of a transition metal, magnesium and lithium, and optionally a solvent, wherein if the complexing agent has a nitrogen atom and a hydroxyl group, the amount of the complexing agent in the activating solution is at least 5 wt % with respect to the total weight of the activating solution, the amount of the solvent is less than 50 wt % and the amount of diethylene glycol as a solvent is less than 25 wt % with respect to the total weight of the activating solution. Described is an activating solution containing a complexing agent selected from a group consisting of monoethanolamine, diethanolamine, triethanolamine, dimethylaminoethanol, and bipyridine, a metal salt selected from a group consisting of a transition metal, magnesium and lithium, and a solvent, wherein if the complexing agent has a nitrogen atom and a hydroxyl group, the amount of the complexing agent in the activating solution is at least 5 wt % with respect to the total weight of the activating solution, the amount of the solvent is less than 50 wt % and the amount of diethylene glycol as a solvent is less than 25 wt % with respect to the total weight of the activating solution.
 Systems and methods of producing polyolefins / 2461577
Method involves: determining the optimum operating temperature to obtain polyolefin in a fluidised-bed reactor system; selecting a chromium oxide-based catalyst, which is reduced with diethylaluminium ethoxide (DEA1E), on a dehydrated silicon support depending on the desired properties of the polyolefin achieved at operating temperature; feeding oxygen into the reactor system to provide the reactor system an amount of oxygen which is effective for minimisation of clogging of the fluidised-bed reactor system. The oxygen is fed at a rate which is equivalent to amounts ranging from more than 0 to less than 0.05 ppm oxygen with respect to volume rate of feeding the monomer into the reactor system. The optimum operating temperature is such that the highest temperature in the reactor system less than about 20°C lower than the melting point of polyolefin.
 Method for preparing styrene-acrylic copolymers aqueous dispersions / 2260602
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.
 The method of producing initiator compositions containing polyvinyl alcohol and surfactant / 2205840
The invention relates to a method for producing stable during storage and having a low viscosity of aqueous suspensions of organic compounds, suspensions, which can be obtained by this method and to the use of these suspensions in polymerization processes
 Intensification method of suspension polymerization of vinyl chloride / 2109755
The invention relates to the intensification of the suspension polymerization of vinyl chloride in the presence of a protective colloid and initiating system based on water and monomerization initiator
Polymerisation method / 2494111
Invention relates to a polymerisation method and particularly to a method for copolymerisation of ethylene with higher α-olefins. Described is a method for copolymerisation of ethylene and an α-olefin comonomer containing 7-10 carbon atoms in a fluidised bed gas-phase reactor. Copolymerisation takes place in the presence of a Ziegler-Natta catalyst with multiple polymerisation centres. Said method is carried out in condensed mode. The amount of said α-olefin is kept less than the amount where considerable condensation occurs in the reactor. At least one of the following conditions is also used: a) the catalyst has 1-octene absorption rate of at least 700; b) polymerisation is carried out in the presence of an activator.
Method of producing polymer beads of uniform size / 2494110
Present invention relates to a method of producing beads having a uniform particle size distribution. Described is a method of producing monodisperse cross-linked polymer beads, comprising the following steps: (a) introducing droplets having a harmonic mean size from 50 to 1500 mcm and comprising at least one monomer, at least one cross-linking agent and a free-radical polymerisation initiator into an aqueous medium through openings in a moulding column to produce an aqueous suspension of droplets having a volume fraction of droplets from 35 to 64%; wherein the droplets are not encapsulated; wherein the monomers are selected from a group comprising monoethylene unsaturated compounds and polyethylene unsaturated compounds, monoethylene unsaturated monomers are selected from a group comprising (meth)acrylic acids and esters thereof, methyl-substituted styrenes, vinyl pyridines and vinyl esters, ethers and ketones; (b) forcing the aqueous suspension of droplets to move down a pipe such that: (I) the ratio of droplet harmonic mean size to inside pipe diameter is from 0.001 to 0.035; (II) mean linear flow velocity in the pipe is from 0.5 to 2.5 ft/s (0.15 to 0.75 m/s); and (III) temperature in the pipe is maintained at least 20°C below the temperature at which the polymerisation initiator has a half-life of 1 hour; wherein the droplets are forced up the moulding column, and the redirected down into the pipe, with subsequent redirection up into a reactor; and (c) polymerising the droplets in the reactor.
 Method of cleaning distribution of tray in reactor system with fluidised bed / 2493904
Invention relates to cleaning of distribution tray in polymerisation reactor system with fluidised bed. One of proposed versions comprises: first mode wherein cleaning is performed at approximately normal base magnitude of reduced rate of gas in polymerisation reactor system with fluidised bed. Said system comprises reactor vessel, circulation circuit and distribution tray arranged in said vessel nearby its inlet. In second mode, gas reduced rate is increased to magnitudes exceeding said base magnitude in aforesaid first mode to the level sufficient for increasing circulating gas temperature at inlet to temperatures higher than circulating gas mean temperature at inlet in aforesaid first mode and to the level sufficient for displacement of dirt from distribution tray holes.
 Polyethylene compositions / 2493182
Composition contains a high-molecular weight polyethylene component and a low-molecular weight polyethylene component, and has density of 0.940 g/cm3 or higher and melt strength of 18 cN or higher. The ratio of the weight-average molecular weight of the high-molecular weight component to the weight-average molecular weight of the low-molecular weight component in the composition is greater than 15:1 and less than 28:1, the high- and low-molecular weight polyethylene components being formed by polymerisation in one reactor. The composition is classified as PE 100 material and has the appropriate balance of properties. A tube made from the composition, subjected to an internal strength test, has extrapolated stress of 10 MPa or higher, when the internal strength curve of the tube is extrapolated to 50 or 100 years according to ISO 9080:2003(E).
Method of producing polymers / 2493176
Apparatus includes a reaction vessel and a degassing vessel. In the method, each of the first and second processes includes the following steps: (a) bringing a main olefin and a comonomer into contact with a catalyst in gas-phase polymerisation conditions in a reaction vessel to obtain a first polymer or a second polymer, respectively, wherein said first and second methods employ the same main olefin, the difference between the two methods being at least one of the following factors: (1) the comonomer used and (2) the reaction temperature at which the polymer is obtained, and (b) subsequently bringing the first or second polymer, respectively, into contact with a blowout gas in a degassing vessel. The transition method involves changing the flow rate of the blowout gas in the degassing vessel from a first value X1, which is used when degassing the first polymer, to a second value X2, which is used when degassing the second polymer. The second value is determined relative the flow rate Xi and temperature Ti used at earlier steps of producing the polymer during transitional polymerisation using the same comonomer as in the second process, and reaction temperature T2 in the second process. The method is characterised by that, (a) if T2 increases relative Ti, X2 is at least 1% lower than Xi when T2 is raised every 1°C compared to Ti, (b) if T2 drops relative Ti, X2 is at least 1% higher than Xi when T2 is decreased every 1°C compared to Ti, (c) if T2 is equal to Ti, X2 is equal to or greater than Xi, preferably equal to Xi.
 Catalyst components for polymerisation of olefins / 2493175
Invention relates to polymerisation of CH2=CHR olefins, where R is hydrogen or a C1-C12hydrocarbon group, and to catalysts therefor. A pre-polymerised catalyst component contains a solid component containing Mg, Ti, a halogen and an electron donor (ID), selected from alkyl esters of aromatic dicarboxylic acids. The molar ratio ID/Mg ranges from 0.025 to 0.065 and the molar ratio Mg/Ti is greater than 13. Said pre-polymerised catalyst component contains up to 50 g of an ethylene prepolymer per g of said solid catalyst component.
 Method for synthesis of functionalised poly(1,3-alkadienes) and use thereof in producing impact-resistant vinyl aromatic polymers / 2493174
Invention relates to a method for synthesis of functionalised poly(1,3-alkadienes) and use thereof in producing impact-resistant vinyl aromatic polymers. Described is a method for synthesis of functionalised poly(1,3-alkadienes), which involves anionic polymerisation of at least one 1,3-alkadiene monomer with 4-8 carbon atoms in the presence of an organolithium compound and a non-polar solvent with a low boiling point and carrying out a step for chain termination of the 1,3-alkadiene-based polymer at the end of polymerisation by adding a bromoalkane to the polymerisation mixture, where the alkane contains 1-12 carbon atoms, after which a product containing a stable nitroxyl radical, characterised by presence of a -NO• group, soluble in said non-polar solvent, is added. The invention also describes functionalised poly(1,3-alkadienes), obtained using said method. Described is a method of producing vinyl aromatic (co)polymers that are grafted on unsaturated poly(1,3-alkadiene) in a controlled manner, involving: a) dissolving said functionalised poly(1,3-alkadiene) in a liquid phase consisting of a mixture of vinyl aromatic monomers and a polymerisation solvent in a weight ratio ranging from 60/40 to 100/0, preferably from 60/40 to 90/10; b) adding at least one radical initiator to the mixture containing the functionalised poly(1,3-alkadiene) in a solution, and polymerising the obtained mixture at a temperature equal to higher than 120°C; c) extracting the vinyl aromatic (co) polymer obtained at the end of polymerisation, and removing volatile components therefrom in a vacuum in order to extract the solvent and unreacted monomers, and d) recycling the mixture of solvent and monomers obtained when removing volatile components to step (a). Described also is an impact-resistant vinyl aromatic (co)polymer, which contains a continuous phase essentially consisting of a matrix containing at least 50 wt % vinyl aromatic monomer, and a dispersion phase essentially consisting of said functionalised elastomer in amount of 1-25 wt % relative total weight, wherein elastomer particles have a "core/cladding" morphology, and average diameter thereof ranges from 0.1 mcm to 1 mcm.
Method to produce polyacrylamide hydrogel / 2493173
Method is realised by polymerisation of an aqueous solution containing 7-15 wt % of acrylamide and 0.5-1.5 wt % of N,N'-methylenebisacrylamide, in presence of polymerisation initiator, besides, the polymerisation initiator is a mixture of 4,4'-azobis(4-cyanopentane acid) and ammonium salt of 4-8-dithiobenzoate of 4-cyanopentane acid with their content in the aqueous solution as 0.03-0.07 wt % and 0.07-0.35 wt %, accordingly, and polymerisation is performed at temperature of 70-80°C and pH 3.0-4.0.
 Polymerisation of isoolefin with polymorphogenates regulated with respect to polydispersity / 2491299
Invention relates to method of polymerisation of monomers with obtaining isoolefin polymers and copolymers, polymerisation system for polymerisation of such monomers, catalytic system for carbocationic polymerisation of isoolefins, isoolefin polymer or copolymer, obtained by said method and with application of said catalytic system. Method of polymerisation of monomers with obtaining isoolefin polymers and copolymers includes polymerisation of one or more monomers in polymerisation medium, including one or more monomers, diluents and catalytic system. Diluent includes one or more halogenated hydrocarbons. Catalytic system includes one or more Lewis acids and multiple modifiers, which include one or more initiators and one or more polymorphogenates, which contain molecular oxygen or organic oxygenate. If polymorphogenate represents initiator, catalytic system includes second initiator. Regulation of concentration of said one or more polymorphogenates in said polymerisation medium is performed by regulated distribution of molecular mass (PMM) of isoolefin polymers and copolymers, constituting more than 2.0. Polymerisation medium is supplied in form of one or more raw material flows into reactor for polymerisation. Mixture of polymer and diluents is removed from reactor. Diluent is separated from mixture in order to separate polymer. Separated diluent is returned into one or more raw material flows, supplied into reactor. One or more polymorphogenates are added into at least one or more raw material flows.
Polymerisation of isoolefin with polymorphogenates regulated with respect to polydispersity / 2491299
Invention relates to method of polymerisation of monomers with obtaining isoolefin polymers and copolymers, polymerisation system for polymerisation of such monomers, catalytic system for carbocationic polymerisation of isoolefins, isoolefin polymer or copolymer, obtained by said method and with application of said catalytic system. Method of polymerisation of monomers with obtaining isoolefin polymers and copolymers includes polymerisation of one or more monomers in polymerisation medium, including one or more monomers, diluents and catalytic system. Diluent includes one or more halogenated hydrocarbons. Catalytic system includes one or more Lewis acids and multiple modifiers, which include one or more initiators and one or more polymorphogenates, which contain molecular oxygen or organic oxygenate. If polymorphogenate represents initiator, catalytic system includes second initiator. Regulation of concentration of said one or more polymorphogenates in said polymerisation medium is performed by regulated distribution of molecular mass (PMM) of isoolefin polymers and copolymers, constituting more than 2.0. Polymerisation medium is supplied in form of one or more raw material flows into reactor for polymerisation. Mixture of polymer and diluents is removed from reactor. Diluent is separated from mixture in order to separate polymer. Separated diluent is returned into one or more raw material flows, supplied into reactor. One or more polymorphogenates are added into at least one or more raw material flows.
Polymer composition hardener / 2410373
Present invention relates to hardeners for unsaturated polyester resins, as well as some other compounds containing double bonds. The hardener is a composition which contains 100 pts. wt benzoyl peroxide, 40-177 pts. wt phthalic ester, 0.6-1.3 pts. wt polyoxyalkylated alkylphenols, 13-97 pts. wt polyoxyalkylated di- or triatomic alcohols with average molecular weight 1000-6000, 1.6-6.0 pts. wt mixture of sodium salts of alkylarylsulphonic acid and 33-43 pts. wt water.
 High-concentration stable and safe diacyl peroxide and peroxy dicarbonate emulsions with low chemical oxygen demand level / 2303043
Aqueous emulsion contains (i) 52.5 to 75% by weight of one or several peroxides (diacyl peroxides and peroxy dicarbonates); (ii) 0.001 to 2.5% by weight of hydrolyzed (hydrolysis degree 45-80%) polyvinylacetate, and optionally a stabilizing amount of nonionic surfactants with hydrophilic-lipophilic balance value above 10 and selected from alkylene oxide block copolymers, ethoxylated fatty alcohols, and ethoxylated fatty acids; and (iii) antifreeze. Emulsion is characterized by low chemical oxygen demand and is safe and stable on storage being useful as free radical source in vinyl chloride polymerization process.
 The method of obtaining multicomponent peroxide polymerization initiator / 2087469
The invention relates to a process for the synthesis of the initiators of polymerization
 The process control method of obtaining cumene ethylbenzene liquid-phase oxidation of ethylbenzene with oxygen / 2046125
The invention relates to a method of managing processes more gidroperekisi ethylbenzene (GPEB) liquid-phase oxidation of ethylbenzene with oxygen, carried out in a cascade of reactors, and can be used in the chemical industry
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FIELD: chemistry. SUBSTANCE: invention relates to a packed composition, a method of storing and/or transporting a mixture containing a compound which is subjected to exothermic decomposition, a method of producing a polymer and a method of modifying a (co)polymer. The packed composition contains a compound which is subjected to exothermic decomposition, and additionally one or more organic diluents, said mixture being packed in a container with a volume of at least 250 litres, which is fitted with a gas outlet opening and is made from thermoplastic material having Vicat softening point measured by a standard ASTM D1525-00 method not higher than (a) the deviation of the temperature of the compound subjected to exothermic decomposition, which is defined as self-acceleration decomposition temperature (SADT) of plus 40°C, which is measured using UN NA test, if the mixture does not contain any diluents, or (b) boiling point of at least 50 wt % of the total weight of the diluent, if the mixture contains an organic diluent. EFFECT: preventing explosive rupture of the container. 14 cl, 4 ex
The invention relates to (i) a packaged composition comprising a compound susceptible to exothermic decomposition, (ii) storage and/or transportation of specified composition and (iii) the methods of preparation and modification of polymers using named Packed composition. Connections subject to exothermic decomposition, such as organic peroxides can decompose at a temperature above a certain critical value, with the formation of gas and heat. Now the heat contributes to the further disintegration. Storage and transport of these compounds is particularly difficult, because the containers with gases of decomposition during transport or storage can cause powerful explosions ripping containers containing peroxides. Recognizing this problem, the international laws and standards on safety regulate the transportation or storage of these compounds. The larger the container, the less the ratio of surface to volume, and the more difficult the heat exchange with the environment in the event of thermal decomposition. Therefore, the storage and transportation of peroxides and other compounds, susceptible to exothermic decomposition, becomes more dangerous by increasing the volume of the container. To increase the security of transportation and x is anemia, organic peroxides are usually stored and transported in containers containing peroxides, dilute one or two types of liquids, for example, in the form of a suspension, emulsion or solution. Aqueous emulsion or suspension peroxides are usually considered safe mixtures, because peroxide dispersed in the aqueous phase, which also takes the heat of decomposing peroxide molecules, for example, by convection and/or evaporation. Peroxide mixtures containing organic solvents, but it is recognized far more dangerous. Containers for storing and/or transporting large amounts of anhydrous peroxide mixtures are typically made from steel, which can withstand the pressure caused by the explosion. Conventional plastic containers were found to be unfit for such mixtures because of their easy destruction. Unexpectedly, it was found that plastic containers large volume can be used for safe storage and transportation of anhydrous peroxide mixtures, provided that the container has an opening for release of gases and is made of thermoplastic with heat Vika is not above the boiling point of the diluent or in the absence of diluent, emergency raise the temperature of the organic peroxide. It is established that in such containers, if the temperature inside the con is anera increases due to exothermic decomposition, (part of) the walls of the container may soften and lose strength before the accumulation of gases will become dangerously high. This softening will lead to the destruction of the container and/or to the rupture of one or more walls of the container so gently releasing the gas and/or liquid without fragmentation or explosive destruction of the container. Thus, this invention relates to a packaged composition comprising a compound susceptible to exothermic decomposition, and optionally one or more organic solvents, with the specified composition packaged in a container with a volume of at least 250 liters, equipped with a discharge gas and is made of thermoplastic material with heat Vik's not above (a) emergency temperature increase connections subject to exothermic decomposition, in the absence of a diluent, or (b) boiling point not less than 50 wt.% the total weight of the diluent, if the mixture contains an organic diluent. Thus, this invention covers two main options. In the first main embodiment, the composition comprises at least one connection subject to exothermic decomposition, and does not contain a diluent. That is: without organic diluent, but also without water diluent, where "without rabbanites is defined as less than 1 wt.%, preferably less than 0.5 wt.%, diluent. In this embodiment of the invention, it is essential that the heat Vika In thermoplastic material is not higher than the emergency temperature increase connections subject to exothermic decomposition. Emergency temperature rise is defined as the temperature of the self-accelerating Decomposition (SADT) plus 40°C. the SADT is the lowest temperature value, which may be samostirayuscheysya the collapse of the Packed substance, and it is measured according to UN test H.4. In practice, emergency increase starts at a temperature of 40°C higher than the SADT. Therefore, in this specification, the temperature of the emergency increase is defined as the SADT+40°C. The heat Vika In a preferred thermoplastic material at not less than 0°C, more preferably at least 10°C., even more preferably at least 20°C., and most preferably at least 30°C below the alarm temperature increase connections subject to exothermic decomposition. In the second main embodiment, the mixture contains an organic solvent. In this embodiment, the heat Vika In a thermoplastic material does not exceed the boiling point at least 50 wt.% the total weight of the diluent. When using pure diluent, the temperature of Kipen what I define as the boiling point of this solvent at normal pressure. If the diluent comprises a mixture of liquid components having a boiling range at normal pressure, the boiling point is defined as the lower limit of the range of the boiling point of this mixture at normal pressure. If the diluent consists of an azeotropic mixture of liquid components, the boiling point is defined as the boiling point of the azeotrope at normal pressure. If the mixture of liquid components, comprising the diluent, has its own boiling points or boiling ranges at normal pressure, the mixture has more than one point of boiling. In this case, at least 50 wt.%, preferably at least 60 wt.%, more preferably at least 70 wt.%, even more preferably at least 80 wt.%, and most preferably at least 90 wt.% the total weight of diluent present in the mixture must be at least equal to the boiling point, but preferably higher than the heat Vika In a thermoplastic material. The temperature difference between the heat resistance of a thermoplastic material and the boiling point of the diluent in the case of a mixture of diluents with more than one boiling point: the lowest boiling point higher than the heat resistance is not less than 0°C, preferably at least 5°C, more preferably 10-400°C, and most preferably 50-300°C. Heat is donosti on Vik's measured in accordance with ASTM D1525-00. Preferably, the average thickness of the container walls is in the range of 0.5 to 5.0 mm, more preferably 0.5 to 3.5 mm, and most preferably 0.5 to 2.5 mm, Such relatively thin walls contribute relatively rapid softening of the walls, when the temperature of the mixture becomes higher than the softening temperature. The burst pressure of the container is preferably between 0.5 and 4.0 bar, more preferably between 0.5 and 3.0 bar, and most preferably between 0.5 and 2.0 bar. The burst pressure is determined by filling a container with water and increase the pressure of water until, when the container will explode. Examples of thermoplastic materials, which - depending on the boiling point of the diluent and emergency increasing junction temperature, exposed to exothermic decomposition may be suitable for the manufacture of the container, are High-Density Polyethylene (HDPE; heat Vika In approximately 70°C); Polypropylene (PP; heat Vika In: about 90°C); Polyvinyl chloride (PVC; resistance by vetch At approximately 85°C); Low Density Polyethylene (LDPE; heat Vika At approximately 55°C); Linear Low Density Polyethylene (LLDPE; heat Vika In approximately 75°C); Stimulational (SAN; heat Vika In: approximately 100°C); Acrylonitrilebutadienestyrene (ABS; those whom lottonet on Vick In: approximately 100°C); Polymethylmethacrylate (PMMA; heat Vika In: approximately 100°C); Polystyrene (PS; heat Vika In approximately 95°C); Acrylonitrilebutadiene (ASA; heat Vika In approximately 95°C); Thermoplastic starch (TLC; heat Vika In approximately 85°C); Acetylsalicylate (ABC; heat Vika In approximately 65°C); Acetylcellulose (AC; heat Vika In approximately 70°C); Polybutadiene (PB; heat Vika In: approximately 85°C). thermoplastic material may also consist of co - or terpolymer of two or more of the above-mentioned thermoplastic materials. The preferred thermoplastic material is HDPE. Examples of organic solvents, which, depending on thermoplastic material may be suitable for use in the mixture, are aliphatic hydrocarbons, aromatic hydrocarbons and oxygenated hydrocarbons, such as ethers, epoxides and esters. Examples of preferred organic solvents are isododecane (boiling range: 175-195°C), neftaraka (usually boil above 200°C), n-paraffin oil (usually boiling above 110°C)odorless white spirit (usually boiling above 110°C), isoparaffin oils (usually boiling above 110°C), light oil (usually boil above 200°C), toluene (normal boiling point: 110°C), ativan the ol (boiling point: 136°C), xylene (boiling range: 138-144°C), isopropylbenzene (range boiling point: 152-154°C), diisopropylbenzene (boiling range: 203-210°C), petrol (boiling range: 175-325°C), diesel fuel, phthalates (generally boil above 230°C) and adipate (generally boil above 230°C), esters with a boiling point above 110°C, epoxides, for example, epoxydecane soybean oil (boiling above 200°C), alcohols with a boiling point above 110°C, glycols (usually boil above 110°C) and ketones or aldehydes with a boiling point above 110°C. the Diluent may also be a mixture of any two or more of the above-mentioned compounds. The most preferred organic diluents are isododecane and Neftemash. The organic diluent or dissolve the connection is subject to exothermic decomposition (in case the connection is solid), or dilutes the named connection with the formation of a homogeneous liquid (in case the connection is fluid). Alternatively, an organic diluent and a liquid connection subject to exothermic decomposition, form, together with the water used as an additional diluent emulsion. The diluent is also known as the phlegmatizer. Suitable combination of thermoplastic material and an organic diluent - HDPE, isododecane and HDPE and Neftemash. Examples is soedinenii, susceptible to exothermic decomposition, are organic peroxides and azoinitiator. Examples of azoinitiators are 2,2'-Azodi(isobutyronitrile), 2,2'-Azodi(2-methylbutyronitrile) and 1,1'-azobis(1-cyclohexylethyl). The connection is subject to exothermic decomposition, preferably is an organic peroxide. Any organic peroxide may be used in the second Main Variant that is in mixtures containing an organic diluent - including hydroperoxides, cloperastine, peroxyacids, dialkylamide, trioxepane, paroxetine, peroxocarbonate, diazepamonline, PEROXYDICARBONATE, peroxyketal, cyclic cloperastine, mixed peroxides (containing two different peroxide part in one molecule), and mixtures of two or more of these peroxides. Despite the fact that the organic peroxide may be oligomeric or polymeric nature, it is preferable to contain one, two or three of peroxide due to the molecule. Examples of peroxides that can be packaged compositions, according to the second Basic Version are: - (di)peroxidase, such as 1,1,4,4-TETRAMETHYLBUTYL-1,4-di(peroxy-2-methylpropanoate), tert-butylperoxybenzoate, treatmentpreventionmost, 1,1,3,3-tetramethylbutylphenol, 1,1-dimethyl-3-hydrox the butyl-1-peroxyneodecanoate, semiproletariat, tert-butylperoxybenzoate, tert-anilinoquinazoline, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxyneoheptanoate, 1,1-dimethyl-3-hydroxybutyl-1-peroxyneoheptanoate, tertbutyloxycarbonyl, tert-anilinomethylene, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxydisulfate, 1,1-dimethyl-3-hydroxybutyl-1-proximitybased, semiproletariat, tert-butylperoxide, tert-AMYLPEROXY, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxypivalate, 1,1-dimethyl-3-hydroxybutyl-1-peroxypivalate, tert-butyl peroxy-2-ethylhexanoate, traceminerals-2-ethylhexanoate, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxy-2-ethylhexanoate, 1,1-dimethyl-3-hydroxybutyl-1-peroxy-2-ethylhexanoate, tert-butyl peroxybenzoate, tert-AMYLPEROXY, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxybenzoate, 1,1-dimethyl-3-hydroxybutyl-1-peroxybenzoate, tert-BUTYLPEROXY-3,3,5-trimethylhexanoate, tert-AMYLPEROXY-3,3,5-trimethylhexanoate, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxy-3,3,5-trimethylhexanoate, 1,1-dimethyl-3-hydroxybutyl-1-peroxy-3,3,5-trimethylhexanoate, tert-butyl peroxyacetate, tert-AMYLPEROXY, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxyacetate, 1,1-dimethyl-3-hydroxybutyl-1-peroxyacetate, tert-butylperoxybenzoate, tert-anilinoquinazolines, 1,1,3,3-TETRAMETHYLBUTYL-1-peroxyisobutyrate, 1,1-dimethyl-3-hydroxybutyl-1-peroxyisobutyrate and 1,4-di-(tert-butylperoxide)cyclohe the San, - dialkylamide, such as di-tert-butylperoxide, di-tert-AMYLPEROXY, tert-butyl-treatmentrelated, di(tert-butylperoxyisopropyl)benzene, 2,5-dimethyl-2,5-di(tertBUTYLPEROXY)hexane, tert-butylcumylperoxide, 2,5-dimethyl-2,5-di(tert-BUTYLPEROXY)hexyne-3, dicumylperoxide and tert-butyl-3-isopropylaniline, - diazepamonline, such as diisobutylamine, di(3,5,5-trimethylhexanoyl)peroxide, dilauroylperoxide, dictyospermi, dodecanedioic, Dibenzoyl peroxide, di(4-methylbenzoyl)peroxide and di(2,4-dichlorobenzoyl)peroxide - PEROXYDICARBONATE, such as di(-methoxybutyl)peroxocarbonate, diisopropylperoxydicarbonate, di-sec-butylperoxybenzoate, di(4-tert-butylcyclohexyl)PEROXYDICARBONATE, di(2-ethylhexyl)PEROXYDICARBONATE, dicetylperoxydicarbonate, di(2-ethylhexyl)PEROXYDICARBONATE, dicetylperoxydicarbonate and dimyristylperoxydicarbonate, - peroxycarbonates, such as tert-butyl peroxy isopropyl carbonate, tert-BUTYLPEROXY-2-ethylhexylcarbonate, tert-AMYLPEROXY-2-ethylhexylcarbonate and tert-butylperoxybenzoate, - hydroperoxides, such as isopropylidenedioxy, 1,1,3,3-tetramethylbutylamine, cumylhydroperoxide and tert-AMYLPEROXY, - peroxyketals, such as 1,1-di(tert-BUTYLPEROXY)-3,3,5-trimethylcyclohexane, 1,1-di(tert-AMI the peroxy)-3,3,5-trimethylcyclohexane, 1,1-di(tert-anilinomethylene, 1,1-di(tert-BUTYLPEROXY)cyclohexane, 2,2-di(tert-BUTYLPEROXY)butane, 2,2-di(tert-AMYLPEROXY)butane, butyl-4,4-di(tert-BUTYLPEROXY)valerate and 2,2'-bis(4,4-di-(tertBUTYLPEROXY)propane), cyclic peroxides, such as 3,6,9-triethyl-3,6,9-trimethyl-1,4,7-triperoxonane and 3,3,5,7,7-pentamethyl-1,2,4-trioxepane, - cloperastine, such as methylethylketone, 2,4-pentanedionate, methylisobutylketone, cyclohexanedione, acetylacetonate and di(1-hydroxycyclohexyl)peroxide. Examples of peroxides that can be packaged compositions, according to the first Basic Variant, that is, in mixtures that do not contain a diluent, are di-tert-AMYLPEROXY, tert-butylcumylperoxide and di-tert-butylperoxide. Packed composition according to the present invention preferably contains a compound susceptible to exothermic decomposition, in the range from 10 to 100 wt.%, more preferably 10-95 wt.%, even more preferably 20-80 wt.% and most preferably 30-70 wt.%. The organic solvent is preferably contained in an amount of from 0 to 90 wt.%, more preferably 5-90 wt.%, even more preferably 20-80 wt.% and most preferably 30-70 wt.%. If necessary, the composition may also include other stood at the gates - suspendresume or emulsifying agents, for example, polyvinyl alcohol. It should be noted that the composition may also contain water in addition to organic diluent and a compound susceptible to exothermic decomposition - forming, thus, emulsion - but the mixture is preferably anhydrous. The container has a volume of at least 250 liters, preferably not less than 600 liters, more preferably not less than 800 liters, and most preferably not less than 1000 litres. The volume of the container is preferably not more than 20,000 litres, more preferably not more than 10,000 litres. The container must have an outlet for the gases generated inside the container. The desired size of the hole (scope issue) depends on, for example, the volume of the container and the type and concentration of the compound exposed to exothermic decomposition, which is in the container. This outlet may be in the form of a membrane, breather, valve pressure relief or in any other form, which facilitates the exit of gases from the container. In a preferred embodiment, the container is constructed as described in WO 2008/020000; that is: it has an output hole, the mouth of the outlet and the vent cover plate for closing the outlet, the plate having ventilation is twistie and having on its surface an edge, the edge surface of which is provided with fasteners for connection with a corresponding fastening device on the outer surface of the neck, where the discharge outlet is closed gas-permeable filter, wherein the gas-permeable filter is a plate, mounted between the mounting devices of the neck and edges. This sheet may, for example, be a thin film of plastic material. The thickness of the sheet may be, for example, about 5 micrometers and about 0.5 mm, for example between about 10 micrometers and about 0.1 mm in order to make the gas-permeable sheet, it can be perforated. The diameter of pores may, for example, be between about 10 micrometers and about 2 mm, for example between about 0.1 mm and about 1.5 mm The vent cover may be, for example, screw-on cap. In this case, the above-mentioned fasteners can be represented in the form of an external screw, screwed to the outer surface of the neck of the outlet, and an internal screw, screwed to the edge of the vent cover. If necessary, the exhaust vent hole in the cover is provided with a removable cap. In this case, the outlet opening may be covered by the neck, closely adjacent to the outer edge of the removable cap, where mutual is current side of the neckline and edges are shaped for education detachable collapsing connection. Such profiling may include cooperating projections and grooves, which are widely used in the field of technology collapsing connection. This allows you to choose the size of the slamming connection so that it will be disclosed at a certain pre-pressure, for example, at a pressure in the range 0.1-0.5 bar or above, by selecting a material with suitable elasticity and optimization of the sizes of the projections and grooves. The vent cover may, for example, have a diameter of 10-30 cm, for example, about 15 cm Removable cap may, for example, have a diameter of about 5-12 cm, for example, about 7 see, However, other dimensions for the ventilation cover and/or a removable cap, if any, may also be optionally applied. Further, the invention relates to a method for producing a polymer by radical polymerization method using an organic peroxide as a source of free radicals. This method includes the transportation of Packed peroxide compositions in accordance with the invention for curing unit and the introduction of peroxide composition in a polymerization process. Examples of such polymerization processes are processes for obtaining polyvinyl chloride, copolymers of vinyl chloride, (co)polymers, poly(meth)acrylate, etc. Preferably SPO is about is (with)polymerization process styrene suspension or (co)polymerization process of ethylene pressure. The comonomers that can be used in (from)polymerization the process of ethylene high pressure, are usually used comonomers include alkenes such as propene, (cyclo)hexene and (cyclo)octene and vinyl acetate. The comonomers that can be used in (from)polymerization process styrene suspension are usually used comonomers and include divinylbenzene. The amount of peroxide used in these conventional (co)polymerization processes will vary depending on the polymerization temperature, the capacity to remove the heat of polymerization, view(AMI) used(s) of monomer(s) and supplied pressure. Typically used from 0.001 to 25 mass% peroxide on the total weight of the monomers. Preferably used is from 0.001 to 15 wt.% the peroxide. The invention also relates to a method for the modification of (co)polymer as in the processes of cross-combination, vaccinations and controlled collapse, such as the formation of polypropylene other of molecular weight and molecular weight distribution - transportation of Packed peroxide compositions in accordance with the invention for curing unit and the introduction of peroxide compositions in the process. EXAMPLES Example 1 Medium container (STC) of 1000 liters, an average wall thickness of about 2 mm, razran the m a pressure of about 1.3 bar, equipped with a safety bleed hole with a diameter of 5.3 cm, made of HDPE (heat Vika In approximately 70°C) and placed in a metal casing, filled with 900 liters of 40 wt.% tert-butylperoxybenzoate (TBPB) isododecane. To create a self-accelerating decomposition used low heating rate (i.e 0,12°C/min). The study was performed in a total pressure tank in an atmosphere of nitrogen. After about 4 hours and 45' after the start, JCC began to bulge at the top. After the temperature reached 55°C, increased pressure in the SVC and caused the gradual opening of the cap covering the discharge opening, at about 0.1 bar overpressure. Double-layer plastic sheet beneath him cracked at 0.4 bar gauge pressure. After that, the temperature inside the container is increased rapidly to about 180°C; was created a lot of smoke and steam. The product was burned at a rate of approximately 6.2 mm/min It showed that due to the high temperature side walls and the upper part of the JCC were softened/melted and compressed in the bottom; no breaks were observed. The metal case after testing remains intact; he was only slightly bowed up at the top. Example 2 Was repeated in Example 1, except that the JCC was filled with 50 wt.% di(3,5,5-trimethylhexanoyl)peroxide (DMHP) in isododecane the E. The packaged composition was heated with a rate of 0.14°C/min after About 4 h 46 pole beginning, JCC began to slightly protrude in the upper part. After the temperature inside the container reached 76°C, increased pressure in the SVC and caused the gradual opening of the cap covering the discharge opening, at about 0.1 bar overpressure. Double-layer plastic sheet beneath him cracked at 0.4 bar gauge pressure. The temperature increased rapidly to about 188°C; was created a lot of smoke and steam. The product was burned at a rate of approximately 41 mm/min It showed that due to the high temperature side walls and the upper part of the JCC were softened/melted and compressed in the bottom; no breaks were observed. The metal case after testing remains intact; he was only slightly bowed up at the top. Example 3 Was repeated in Example 1, except that the heating rate amounted to 0.10°C/min and peroxide mixture circulated by the centrifugal pump. This test was to simulate the worst case prostacare homogeneous decomposition. After the start, the temperature was gradually increased and after about 11 hours STK started a little bulge at the top. After the temperature of the mixture reached 70°C, increased pressure in the SVC and caused the gradual opening of the cap at about 0.1 bar is izbytocnogo pressure. Double-layer plastic sheet beneath him cracked at 0.2 bar overpressure. Through the hole for about 1 minute and watched the powerful flow of liquids and gases; turned off the pump and heaters. Observed a further increase in the pressure and JCC dispersed (bottom left) when R=0,93 bar overpressure. Uniform deviation led to a rapid rise in temperature up to a maximum of 180°C; was created a lot of smoke and steam. It showed that due to the high temperature side walls and the upper part of the JCC were softened/melted and compressed in the bottom; no breaks were observed. The metal case after testing remains intact, although it was slightly bowed up at the top and on the side walls. Example 4 Was repeated Example 3 with 50 wt.% di(3,5,5-trimethylhexanoyl)peroxide (DMGP) isododecane. Used a heating rate of 0.23°C/min In the experiment, the temperature rose gradually, after about 3.5 hours have increased pressure and JCC began to be blown up. Gradually opened the cap at about 0.1 bar overpressure; the pump is turned off and the heat exchangers cooled with cold water. Double-layer plastic sheet is cracked at 0.2 bar overpressure and through the outlet of the observed flow. Pressure has increased and JCC dispersed in the upper part when P=,84 bar overpressure. The cover was torn down and a uniform deviation led to a rapid rise in temperature to about 120°C. It showed that due to the high temperature side walls and the upper part of the JCC were melted to a certain extend; no gaps, caused by the explosion, were not observed. The metal case after testing remains intact, although it was slightly bowed up at the top and on the side walls. From the above experiments, we can conclude that the data is Packed compositions meet the criteria of the UN. Even under worst-case conditions for uniform thermal variances investigated the most dangerous mixture (TBR) was not observed explosive destruction of the inner container and/or metal case. 1. Packed a composition comprising a compound subject to exothermic decomposition, and additional one or more organic solvents, while the mixture is Packed in a container of not less than 250 litres, equipped with a discharge gas and is made of thermoplastic material having a heat Vika, measured by standard method ASTM D1525-00, not above 2. Packaged composition according to claim 1 in which the compound is exposed to exothermic decomposition, is an organic peroxide. 3. Packaged composition according to claim 1 or 2, containing an organic solvent, in which at least 50 wt.% the total weight of the diluent has a boiling point at least 5°C higher heat resistance thermoplastic material. 4. Packaged composition according to claim 1 or 2, which contains the organic solvent in which the organic diluent is selected from the group consisting of isododecane and Neftemash. 5. Packaged composition according to claim 1 or 2, in which the mixture is an emulsion containing the compound susceptible to exothermic decomposition, one or more organic solvents and water as an additional diluent. 6. Packaged composition according to claim 1 or 2, in which thermoplastic material is High Density Polyethylene (HDPE). 7. Packaged composition according to claim 3, in which thermoplastic material is High Density Polyethylene (HDPE). 8. Packed composition according to any one of claims 1, 2 or 7, in which the walls of the container have an average thickness in the range of 0.5-5 mm p> 9. Packed composition according to any one of claims 1, 2 or 7, in which the container has a burst pressure in the range of 0.5-2 bar.10. Packaged composition according to claim 3, in which the container has a burst pressure in the range of 0.5-2 bar. 11. Packed composition according to any one of claims 1, 2, 7, or 10, in which the container has an outlet opening, the mouth of the outlet and the vent cover plate for closing the outlet, the plate having a vent opening and having on its surface an edge, the edge surface of which is provided with fasteners for connection with a corresponding fastening device on the outer surface of the neck, where the discharge outlet is closed gas-permeable filter, wherein the gas-permeable filter is a plate, mounted between the mounting devices of the neck and edges. 12. The method of storage and/or transportation of the mixture containing the compound susceptible to exothermic decomposition, and additional one or more organic solvents, with the specified composition packaged in a container with a volume of at least 250 liters, equipped with a discharge gas and is made of thermoplastic material having a heat Vika measured In a standard way ASTMD1525-00 not above 13. A method of obtaining a polymer by radical polymerization method using an organic peroxide as a source of free radicals, including transport of the Packed peroxide composition corresponding to point 2, to the curing unit and the introduction of peroxide composition in a polymerization process. 14. Modification of the copolymer transportation of Packed peroxide composition according to claim 2 to a polymerization unit and the introduction of peroxide compositions in the process.
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