• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    1520440 Emulsion polymerization; scale prevention MONTEDISON SpA 9 Dec 1975 [10 Dec 1974] 50403/75 Heading C3P Monoethylenically unsaturated monomers are continuously polymerized in aqueous emulsion by feeding the monomer emulsions through a succession of separate polymerization zones under superatmospheric pressure generated or contributed to by hydrostatic pressure, the zones being arranged at successively increasing heights, and reagent steam being conveyed from the lowest to the highest zone. Use of superatmospheric pressure inhibits foaming of the emulsion and formation of polymer scale. Suitable apparatus is shown in the figure, where (1) is a "seeding pot", and (2) is the polymerization pot, (3) is a "finishing pot", (4) is equipped with a watercoil for cooling the dispersion, and (5) is the vessel wherein the preliminary emulsion is formed; polymerization is performed in pots (1), (2) and (3).
    公开号:SU828971A3
    申请号:SU752197546
    申请日:1975-12-09
    公开日:1981-05-07
    发明作者:Дъачилле Массимо；Буччи Марио
    申请人:Монтэдисон С.П.А. (Фирма)；
    IPC主号:
    专利说明:

    rotation of foaming and swelling of the reaction mass in the Polymerization and i-ia coring process of internal parts of the polymerization apparatus.
    This goal is achieved by the fact that, in the study of snooping polyviiylacetate, the emulsion of continuous water emulsion polymer polymerization of vniil acetate or its monomerization with other vinyl; monomers in one or several successively connected reactors in the distillation of radical initiators, emulsifiers and other polymerization additives Process Carried out In a cascade of vertically arranged reactors in the flow of the initial reaction mixture into the lower reactor and movements in the process of polymerization from the bottom up.
    The purpose of the invention is also achieved by the fact that in the well-known installation of the optional method of obtaining an emulsion consisting of sequentially connecting pipelines for the emulsifier, a prepolymer and a polymerizer of autoclave type, an iolizer of the column type, with internal chambers (and the tubing pipes, and the piping pipes for the tubing pipes, and the tubing pipes, and the tubing pipes, and the tubing pipes, and the tubing pipes, and the tubing pipes, and the tubing pipes, and the tubing pipes, and the tubing pipes, and the piping pipes, and the piping for the tubing of the piping pipes and the piping for the piping pipes. with nozzles for Evod and output of the reaction mixture, and their implanters are located in the Vertical view of the cascade, and the input for the reaction mixture is located in poorly for the pre-polymerization unit, and for the withdrawal of the reaction mixture - in the Kriika colimerizer of coloi.
    The invention is illustrated with a drawing.
    The installation consists of three lolymer Ezativy eleiteits, two of which are standard thiaa reactors equipped with sourcals and shrubs, and for circulating thermostatic fluid (initial reactor 1 and iolimer 1-zacioine reactor 2), while the third is a tubular reservoir partitions with internal partitions (reactor 3}. The apparatus 4 is a tubular type and is equipped with a water cooler and serves to cool the dioiercia. Pumps 5 are used to feed the polymer to the Reactor 1, feed the monomer or monomers to the reactor 2I of the inoculating solution (if necessary) to the third reactor.
    Each reactor is equipped with a TCP detector and pressure gauge.
    The reactor 6 is equipped with a meplc. And a level indicator j-i, and, inter alia, for preparing emulsions, which are then placed into the reactor /.
    According to the invention, niponic, cationic and ineko can be applied: Inogenic emulsifiers - surface active agents (surfactants).
    The first group includes the following | PA: B: alkali metal or ammonium salts, or a-mines, or long-term fatty acids, for example sodium oleate, potassium stearate, diethanolaminlaurate; metal sulfate sulfates, derivatives of high molecular weight aliphatic and alkylaromatic hydrocarbons, and alkyl naphthalic sulfonic ACIDS salts; Alkrgl metal complex esters of dicarboxylic acids, for example sodium doptyl succinic sulfonic acid, sodium dodecylbenzenesulfonate, sodium lauryl sulfate.
    The following surfactants belong to the second group: alkyl ammonium salts, containing; and
    from 12 to 18 carbon atoms in the alkyl radicals, for example chlorides and acetates; quaternary ammonium salts, for example cetyltrimethylbromide bromide.
    ; To the third group belong the following surfactants: add products of aliphatic alcohols or their fatty acids and ethylene oxide.
    The concentration of these surfactants can vary from 0.1 to 5%, preferably 0.5-2.5%,
    but from the total variance,
    Together with these emulsifiers, protective ones may be used, such as ivolvinyl alcohol containing up to 10% acetyl gels, soluble starch, methylcellulose, hydroxyatc; l cellulose, sodium carboxymethyl cellulose and algae salts: natal or polyacrylate tiaa. | Conceitration of such positive agents should be from 1 to 10%, but preferably from 1 to 3%, relative to the total amount of dispersion.
    The polymerization is carried out using Calpium initiators, for example, potassium yersulfate, ammonium nersulfate, hydrogen peroxide, dibenzoyl peroxide, sodium nonrekis, diazosoediaii; they are used in an amount of from 0.01 to 10% relative to the total amount of the dispersion.
    Alkali metal bicarbonates, sodium acetate, borax, and acidic phosphates of n-metal metals can be used as the buffer compounds used.
    The method allows continuous production of water dpsiers of polymers and copolymers having distinctive morphological characteristics, such as soup, otvenenio zanpzhenny diametr particles, good mechanical stability, good stability Prp long cycles, average viscosity (2000-5000 s) and content solids in the range from 4-0 to 60%.
    Example 1. The aqueous phase fed to reactor 1 is prepared with reregeneration in tank 6 of the following components to obtain a stable, milky white foremuloin, kg: Water 24,401 Al areola SCL 83% (sodium dodeethl benzene sulfonate) 0,102 Natrosol 250 HP, 96% vym (zn) vniily acetate 20,126 kg. For delivery to the final reactor 3, a solution of the following composition is prepared, kg: Sodium persulfate 0, (} 12 Water 0.250 The various reactors, including the refrigerator, are disconnected by overlapping the corresponding valves. The initial reactor is made of stainless steel with a capacity of 11 liters They are combined with a reflux condenser and then filled with porous emulsion. At a rate of 100 or less, the temperature of the water circulating in the scrub is adjusted to 70-80 ° C, and after refluxing begins to reflux, polymerization brings to the end what the iolnoe indicates stopping boiling with reversible cooler. A 11 l stainless steel submeasurement reactor, with a capacity of 11 liters, is connected to a reflux condenser and then filled with the following composition, kg: Water5.355 Alarsol SCL0.021 Natrosol 250 HP0.055 Emulsion O0.108 Vinyl sulfonate sodium 25%, water in water, ipacTBOpe0,100 potassium persulphate 0.021 sodium acetate 0.035 vinyl acetate5.305 Starting from this, polyvinyl acetate dispersion is obtained with stirring at a rate of 100 and heated to boiling point with a reversible cooler up to SCOPE. The reflux condenser used at the beginning of the process is disconnected, then the initial reactor, the full-reactor, the final reactor and the cooler are interconnected, the last two devices being pre-filled with dispersion of polyvinyl acetate prepared in advance and containing about 50% dry Substance. With the help of the pump, the emulsion is not. continuously fed into the reactor 1, continuing to mix at a speed of 100 rpm: min; In this case, the pre-polymerization product is peremiigi in the reactor 2 at the same speed with which it is fed foreellesley. The polymerisation reactor 2, at a stirring rate of 100, is then filled with a pump pump with a ratio of 3.813 kg for every 1.006 kg of vinyl acstat contained in the prepolymerisation product, and the input; cm from the reactor /. The final reactor 5, made of stainless steel and a tank of 11 A, is continuously filled with a pump with a solution of potassium persulfate in the amount of 0.050 kg for every 10 kg of dispersion coming from reactor 2 in order to destroy the last traces of the monomer. In the supply equilibrium state, the following: reactor 1: 6.187 kg / h foremulsion; reactor 2: & 7 + of the prepolymerization product coming from the reactor /, 3.813 kg h of viii acetate; reactor 5: 0.0501 potassium ireulfate solution + 10.0 kg. h of polymer dispersion coming from reactor 2. The total production is referred to) and to the total volume of all three polymerization tanks (33 l) is 0.305 g / d / /. The temperature in various reactors is supported by the following: reactor / 75 ± 2 С, reactor 2 - 85 ± 2 ° С, reactor 5-90 ± 2 ° С. P1z of the nuclear reactor 3, the dispersion is fed into the refrigeration unit 4, from where it is poured into storage tanks or directly released into production. A stable dispersion containing 50% dry matter and not more than 5% residual monomer is obtained in the same way. Such dispersions have high chemical and mechanical stability; After a few hours of operation, the sizes of the asters reached an equilibrium value corresponding to an average diameter of 1.0-1.5 microns. Example 2. If the process of iodine is carried out using an aeration, the emulsion supplied to the reactor / is prepared in a tank of five mixes of the following comionens, kg: Water21.734 Alarsol SCL0.112 Natrosol 250 HP0.280 Emulsion O0.562 Sodium vinyl sulfate 25% in an aqueous solution of 0.518 potassium persulphate; 0.082 sodium acetate 0.090 vinyl acetate5.498
    The entire cycle, with the exception of the primary reactor /, is filled with a ready disierse, which has the same characteristics as the dispersion required to obtain,
    11 kg of formulae, irrigoodlein, as described above, are fed to the reactor (with the help of pump) —and the heating iris is polymerized, ng1I., And mixed with a speed of 100 rpm. After the polymerization of the said charge, the initial reactor is connected to the polymerization reactor, heated to 85 ° C, and the ring-type reactors heated to 90 ° C.
    In the equilibrium iodachi stage the following:
    reactor /: 14,250 foremulsil;
    reactor 2: 14.250 kg / h of the prepolymerization product coming from reactor 1, –f 10.750 kg / h of vinyl acetate;
    reactor 3: 25.0 kg1 h of dispersion of a lolimer, which lobates from reactor 2.
    Total capacity was 0.758 / cg / l / h.
    - Example 2 differs from Example 1 in that the amount of catalyst is reduced due to the elimination of its addition to the reactor 5; the process is conducted at e-4 aggl; The resultant dispersion thus contains about 56% dry matter.
    For Solers, obtained in such a way, it is similar to the one that was found in Larimer 1, however, it is reflected by decreasing the particle diameter (1 micron), higher viscosity and the rest of the monomer 1 is not higher than 0.3%.
    Even more convincing results regarding the efficiency of the installation and the conditions of its operation were obtained when it was used for several days. Neither foaming nor mass learning of polymerization was observed, taking into account the time of lolmerisacin, the amount of acid in various reactors was permissible.
    PRI m-e p 3. Ready t -the following mixtures and solutions:
    Mixture number 1 (kg):
    Water29,460
    Nat. Salt 180 L 96%
    (hydroxyethyl cellulose) 0.410
    Alarsol SCL0,230
    Ryoklen NF 10 (polyoxyethylated ioylphenol) 0.399
    Sodium acetate 0,350
    | Vnylsulfonate | sodium 25% in aqueous solution0, 476
    Croton acid (modifying somol-mer) 0.195
    Mixture (No. 2 (kg):
    Vinyl Acetate26,123
    Butylmaleate 11,628
    8 (kg):
    Rastvo-p lgo 1
    Water9,706
    Calla persulphate 0,300
    In the nerve reactor, the following aqueous phases are prepared by foremulgirovia: Mixture K "123,398
    Solution N ° 126,950
    Vipylacetate0.720
    Rodor-force anti-mousse 42-6 (anti-foam silicone oil) 0.015
    The initial reactor is charged with a water phase, -prepared, as described above, and the polymerisation is carried out while stirring, providing heat to the temperature of the ki-pei with reverse fridge due to the circulator in the jacket at 75-80 ° C iridesi to the dephlegmator reactor and its isolation from the remaining reservoirs installed earlier.
    At the end of the ilerization, the reflux condenser is disconnected, the reactor is connected to the reactor 2, 3 and cooler 4, the nredvarltello polarized copolymer dispersion. lostuiayunley from the previous previous continuous operation).
    The process is carried out under the standing conditions and the L-use of the following not loading:
    reactor /: 2.330 kg 1 h for emulsified water phase;
    reactor 2: 2.330 kg1h of the product of fori-polymerization, lostula from the reactor /, + 2.424 kg1ch of mixture No. 2;
    reactor 3: 4,754 copolymer of disperse coming from reactor 2, + 0.250 kg / h of solution M 1 (3% potassium persulphate).
    Temperature: i-Supported within the following limits: Rea-Kt-op / - 75 + 2 ° C, -Reka-Ktor 2-85 ± 2 ° C, Re-Ktor 3 -90 ± 2 ° C.
    The throughput is 0.152 kg / l.
    This gives a stable suspension containing about 52% dry matter, with an average particle diameter ranging from 1.0 to 1.5 microns.
    Pr-n drying these disiryssy get light, transparent, elastic and waterproof-and-e strings.
    As follows from the examples given, the preposition — a method and an installation for it to be carried out makes it possible to prevent the spreading of and reaction to the reaction mass and, thereby, to prevent core formation.
    Formula and 3 about b ete n and
    1. The way-for-getting a full-ethyl acetate emulsion of a continuous water-emulsion-free polymer of vinyl acetate or copolymerization of ith with other vinyl
    权利要求:
    Claims (2)
    [1]
    1. A method of producing a polyvinyl acetate emulsion by continuous aqueous emulsion polymerization of vinyl acetate or by copolymerizing it with other vinyl monomers in several reactors in series in the presence of radical initiators, emulsifiers and other polymerization additives, characterized in that, in order to prevent foaming and swelling of the reaction mass in the process polymerization and crust formation on the internal parts of the polymerization unit, the process is carried out in a cascade vertically aspo- decomposition reactor 10 at a feed of the feed to the reactor bottom and its movement during the polymerization from the bottom up.
    [2]
    2. Installation for implementing a method for producing a polyvinyl acetate emulsion, consisting of series-connected pipelines of a formulator, prepolymerizer and an autoclave type polymerizer, a column type 20 polymerizer with internal partitions, and a tubular type apparatus with an internal cooler having fittings for input and output of the reaction mixture, characterized in that, in order to prevent foaming and swelling of the reaction mass during polymerization and to prevent crusting on the inside They detail the polymerization plant, polymerizers arranged in a vertical cascade connection for the input of the reaction mixture is located in the bottom of the prepolymerizer, and to output the reaction mixture - in the lid of the column type polymerizer.
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    同族专利:
    公开号 | 公开日
    NL183586C|1988-12-01|
    FR2294190A1|1976-07-09|
    DE2555142A1|1976-06-24|
    NL7514220A|1976-06-14|
    US4022744A|1977-05-10|
    DE2555142C2|1988-05-05|
    IT1026928B|1978-10-20|
    GB1520440A|1978-08-09|
    JPS5947681B2|1984-11-21|
    FR2294190B1|1978-05-12|
    JPS5183684A|1976-07-22|
    NL183586B|1988-07-01|
    BE836417A|1976-06-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2587562A|1948-11-22|1952-02-26|Shawinigan Resins Corp|Continuous emulsion polymerization process for vinyl acetate|
    US2936303A|1958-04-25|1960-05-10|Phillips Petroleum Co|Olefin polymerization|
    GB1018667A|1962-10-19|1966-01-26|Villax Ivan|Production of oxytetracycline|
    NL297462A|1963-09-04|
    NL126771C|1965-02-01|US4559374A|1984-09-19|1985-12-17|The Goodyear Tire & Rubber Company|Continuous emulsion polymerization process for preparation of flame-retardant latex|
    GB8725131D0|1987-10-27|1987-12-02|Unilever Plc|Emulsion polymerisation|
    DE10035587A1|2000-07-21|2002-02-07|Wacker Polymer Systems Gmbh|Process for the production of protective colloid-stabilized polymers by means of continuous emulsion polymerization|
    AU785016B2|2001-06-14|2006-08-24|Rohm And Haas Company|Semi-continuous bimodal emulsion polymerization|
    DE102007038332A1|2007-08-14|2009-02-19|Wacker Chemie Ag|Continuous polymerization process|
    EP2108662A1|2008-04-10|2009-10-14|Hexion Specialty Chemicals Research Belgium S.A.|Process of copolymerization in emulsion of 1-Alkenes and vinyl esters with high conversion|
    DE102011005388A1|2011-03-10|2012-09-13|Wacker Chemie Ag|Process for the preparation of polymers by emulsion or suspension polymerization|
    EP3307792B1|2016-06-29|2018-10-24|Wacker Chemie AG|Method for producing vinyl acetate-ethylene copolymers by means of emulsion polymerization|
    FR3097541A1|2019-06-20|2020-12-25|Nge Fondations|Lifting clamp for concrete reinforcement or similar|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT3036374A|IT1026928B|1974-12-10|1974-12-10|CONTINUOUS POLYMERIZATION PROCESS IN EMULSION|
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