NO774497L - PROCEDURE FOR PREPARING POLYVINYL CHLORIDE POLYMERS - Google Patents
PROCEDURE FOR PREPARING POLYVINYL CHLORIDE POLYMERSInfo
- Publication number
- NO774497L NO774497L NO774497A NO774497A NO774497L NO 774497 L NO774497 L NO 774497L NO 774497 A NO774497 A NO 774497A NO 774497 A NO774497 A NO 774497A NO 774497 L NO774497 L NO 774497L
- Authority
- NO
- Norway
- Prior art keywords
- polymerization
- vinyl chloride
- pressure
- emulsion
- chloride polymers
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 22
- 229920000642 polymer Polymers 0.000 title claims description 11
- 229920000915 polyvinyl chloride Polymers 0.000 title description 3
- 239000004800 polyvinyl chloride Substances 0.000 title description 3
- 238000006116 polymerization reaction Methods 0.000 claims description 30
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims description 20
- 239000000178 monomer Substances 0.000 claims description 13
- 239000003054 catalyst Substances 0.000 claims description 8
- 239000003995 emulsifying agent Substances 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 238000007720 emulsion polymerization reaction Methods 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 239000000084 colloidal system Substances 0.000 claims description 2
- 230000001681 protective effect Effects 0.000 claims description 2
- 239000000839 emulsion Substances 0.000 description 16
- 239000000243 solution Substances 0.000 description 7
- USHAGKDGDHPEEY-UHFFFAOYSA-L potassium persulfate Chemical compound [K+].[K+].[O-]S(=O)(=O)OOS([O-])(=O)=O USHAGKDGDHPEEY-UHFFFAOYSA-L 0.000 description 5
- 235000019394 potassium persulphate Nutrition 0.000 description 4
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 229920001577 copolymer Polymers 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- VZCYOOQTPOCHFL-OWOJBTEDSA-N Fumaric acid Chemical compound OC(=O)\C=C\C(O)=O VZCYOOQTPOCHFL-OWOJBTEDSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical class [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000004816 latex Substances 0.000 description 2
- 229920000126 latex Polymers 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 235000010265 sodium sulphite Nutrition 0.000 description 2
- CIHOLLKRGTVIJN-UHFFFAOYSA-N tert‐butyl hydroperoxide Chemical compound CC(C)(C)OO CIHOLLKRGTVIJN-UHFFFAOYSA-N 0.000 description 2
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 2
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 2
- IQBLWPLYPNOTJC-FPLPWBNLSA-N (z)-4-(2-ethylhexoxy)-4-oxobut-2-enoic acid Chemical compound CCCCC(CC)COC(=O)\C=C/C(O)=O IQBLWPLYPNOTJC-FPLPWBNLSA-N 0.000 description 1
- JAHNSTQSQJOJLO-UHFFFAOYSA-N 2-(3-fluorophenyl)-1h-imidazole Chemical compound FC1=CC=CC(C=2NC=CN=2)=C1 JAHNSTQSQJOJLO-UHFFFAOYSA-N 0.000 description 1
- OEPOKWHJYJXUGD-UHFFFAOYSA-N 2-(3-phenylmethoxyphenyl)-1,3-thiazole-4-carbaldehyde Chemical compound O=CC1=CSC(C=2C=C(OCC=3C=CC=CC=3)C=CC=2)=N1 OEPOKWHJYJXUGD-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical class [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 239000004908 Emulsion polymer Substances 0.000 description 1
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical group C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 1
- OFOBLEOULBTSOW-UHFFFAOYSA-N Propanedioic acid Natural products OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 125000005210 alkyl ammonium group Chemical group 0.000 description 1
- 150000008055 alkyl aryl sulfonates Chemical class 0.000 description 1
- 150000008051 alkyl sulfates Chemical class 0.000 description 1
- 229940045714 alkyl sulfonate alkylating agent Drugs 0.000 description 1
- 150000008052 alkyl sulfonates Chemical class 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007334 copolymerization reaction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 150000005690 diesters Chemical class 0.000 description 1
- LDCRTTXIJACKKU-ONEGZZNKSA-N dimethyl fumarate Chemical compound COC(=O)\C=C\C(=O)OC LDCRTTXIJACKKU-ONEGZZNKSA-N 0.000 description 1
- LDCRTTXIJACKKU-ARJAWSKDSA-N dimethyl maleate Chemical compound COC(=O)\C=C/C(=O)OC LDCRTTXIJACKKU-ARJAWSKDSA-N 0.000 description 1
- GRWZHXKQBITJKP-UHFFFAOYSA-L dithionite(2-) Chemical compound [O-]S(=O)S([O-])=O GRWZHXKQBITJKP-UHFFFAOYSA-L 0.000 description 1
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- GLVVKKSPKXTQRB-UHFFFAOYSA-N ethenyl dodecanoate Chemical compound CCCCCCCCCCCC(=O)OC=C GLVVKKSPKXTQRB-UHFFFAOYSA-N 0.000 description 1
- GFJVXXWOPWLRNU-UHFFFAOYSA-N ethenyl formate Chemical compound C=COC=O GFJVXXWOPWLRNU-UHFFFAOYSA-N 0.000 description 1
- 150000002191 fatty alcohols Chemical group 0.000 description 1
- 239000001530 fumaric acid Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910052742 iron Chemical class 0.000 description 1
- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 239000011976 maleic acid Substances 0.000 description 1
- 125000005395 methacrylic acid group Chemical group 0.000 description 1
- LVHBHZANLOWSRM-UHFFFAOYSA-N methylenebutanedioic acid Natural products OC(=O)CC(=C)C(O)=O LVHBHZANLOWSRM-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 125000000864 peroxy group Chemical group O(O*)* 0.000 description 1
- JRKICGRDRMAZLK-UHFFFAOYSA-L persulfate group Chemical group S(=O)(=O)([O-])OOS(=O)(=O)[O-] JRKICGRDRMAZLK-UHFFFAOYSA-L 0.000 description 1
- -1 polyethylene sulfates Polymers 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- XWGJFPHUCFXLBL-UHFFFAOYSA-M rongalite Chemical compound [Na+].OCS([O-])=O XWGJFPHUCFXLBL-UHFFFAOYSA-M 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- BTURAGWYSMTVOW-UHFFFAOYSA-M sodium dodecanoate Chemical compound [Na+].CCCCCCCCCCCC([O-])=O BTURAGWYSMTVOW-UHFFFAOYSA-M 0.000 description 1
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 1
- 229940082004 sodium laurate Drugs 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- DHCDFWKWKRSZHF-UHFFFAOYSA-L thiosulfate(2-) Chemical compound [O-]S([S-])(=O)=O DHCDFWKWKRSZHF-UHFFFAOYSA-L 0.000 description 1
- KOZCZZVUFDCZGG-UHFFFAOYSA-N vinyl benzoate Chemical compound C=COC(=O)C1=CC=CC=C1 KOZCZZVUFDCZGG-UHFFFAOYSA-N 0.000 description 1
- 229920001567 vinyl ester resin Polymers 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- 229940124024 weight reducing agent Drugs 0.000 description 1
- 239000013585 weight reducing agent Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F14/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F14/02—Monomers containing chlorine
- C08F14/04—Monomers containing two carbon atoms
- C08F14/06—Vinyl chloride
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Polymerisation Methods In General (AREA)
Description
Fremgangsmåte ved fremstilling av polyvinylkloridpolymerer. Process for the production of polyvinyl chloride polymers.
Ved opparbeidelse av pol^merdispersjoner, f.eks. ved fjernelse av restmonomeren, kan aksepterbare avgassingstider bare opprett-holdes når dispersjonene utsettes for temperaturer og skjærkrefter som øker risikoen for termisk hhv. mekanisk beskadigelse. Dette fører fremfor alt for emulsjonspolymerer til fare for koagulering som vil vanskeliggjøre en videre bearbeidelse av polymeren. When preparing polymer dispersions, e.g. when removing the residual monomer, acceptable degassing times can only be maintained when the dispersions are exposed to temperatures and shear forces that increase the risk of thermal or mechanical damage. Above all, for emulsion polymers, this leads to the risk of coagulation, which will make further processing of the polymer difficult.
Det tas derfor ved op<p>finnelsen sikte på å tilveiebringe en fremgangsmåte som fører til en vinylkloridpolymeremulsjon som.til-fredsstiller de økede krav til termisk stabilitet og skjærstabilitet. The invention therefore aims to provide a method which leads to a vinyl chloride polymer emulsion which satisfies the increased requirements for thermal stability and shear stability.
Oppfinnelsen angår således en fremgangsmåte ved fremstilling av vinylkloridpolymerer med minst 80 vekt% innpolymerisert vinylklorid, ved emulsjonspolymerisasjon under selvinnstillende monomertrykk og ved temperaturer mellom -20 og 80°C, fortrinnsvis 25-70°C, The invention thus relates to a method for the production of vinyl chloride polymers with at least 80% by weight polymerized vinyl chloride, by emulsion polymerization under self-adjusting monomer pressure and at temperatures between -20 and 80°C, preferably 25-70°C,
i nærvær av beskyttelseskolloider og/eller emulgeringsmidler, radikaldannende katalysatorer og eventuelt reguleringsmidler, og fremgangsmåten er særpreget ved at polymerisasjonen avbrytes efter tilsetning av monomerene efter et trykkfall av 1-3 bar i forhold til det selvinnstillende polymerisasjonstrykk. in the presence of protective colloids and/or emulsifiers, radical-forming catalysts and possibly regulators, and the method is characterized by the fact that the polymerization is interrupted after addition of the monomers after a pressure drop of 1-3 bar in relation to the self-adjusting polymerization pressure.
Ved den foreliggende fremgangsmåte er det blitt mulig vedWith the present method, it has become possible by
en liten forandring av de vanlige polymerisasjonsbetingelser gunstig å innvirke på polymeremulsjonens skjærkraft- og termiske stabilitet.. a small change in the usual polymerization conditions to favorably affect the polymer emulsion's shear force and thermal stability..
Dessuten forbrukes ved den foreliggende fremgangsmåte en vesentlig mindre katalysatormengde enn ved de hittil vanlige fremgangsmåter, hvor en efterpolymerisasjon foretas inntil et større trykkfall og under tilførsel av ytterligere katalysator. Den In addition, the present method consumes a substantially smaller amount of catalyst than in the hitherto usual methods, where a post-polymerization is carried out until a greater pressure drop and during the supply of additional catalyst. It
lille katalysatortilførsel kommer også produktkvaliteten til gode. Dessuten påvirkes polymerisasjonssyklusene gunstig da både den tidlige avslutning av efterpolymerisasjonsprosessen og produktets økede stabilitet overfor skjærkrefter bevirker en påskyndelse av a small catalyst supply also benefits the product quality. Moreover, the polymerization cycles are favorably affected as both the early termination of the post-polymerization process and the product's increased stability against shear forces cause an acceleration of
produksjonssyklusene.the production cycles.
Den foreliggende fremgangsmåte er spesielt godt egnet for emulsjonspolymerisasjon av vinylklorid. Dersom den foreliggende fremgangsmåte anvendes for fremstilling av vinylkloridpolymerer med minst 80 vekt% vinylklorid i kopolymerer, kan alle monomerer som er kopolymeriserbare med vinylklorid, tilføres. Imidlertid er slike monomerer som kan kopolymeriseres med vinylklorid fore-trukne som bare inneholder en polymeriserbar carbondobbeltbinding. Som eksempler på slike monomerer kan nevnes vinylidenklorid, vinyl-estere av carboxylsyrer, som vinylformiat, vinylacetat, vinyllaurat, vinylbénzoat og vinylversatat, acirylestere og methacrylestere, som methylacrylat og methylmethacrylat, og dessuten de umettede di-carboxylsyrer, som maleinsyre, fumarsyre, itaconsyre, og mono- og diesterne av disse syrer, som maleinsyredimethylester, -diethylester og -di-n-butylester, maleinsyremono-(2-ethylhexyl)-ester, fumarsyredimethylester, -diethylester, -di-n-butylester, -di-(2-ethylhexyl)-ester og -di-laurylester. Selvfølgelig kan også kopolymerer av flere enn to monomerer fremstilles ved den foreliggende fremgangsmåte. The present method is particularly well suited for emulsion polymerization of vinyl chloride. If the present method is used for the production of vinyl chloride polymers with at least 80% by weight of vinyl chloride in copolymers, all monomers that are copolymerizable with vinyl chloride can be added. However, such monomers which can be copolymerized with vinyl chloride are preferred which contain only one polymerizable carbon double bond. Examples of such monomers include vinylidene chloride, vinyl esters of carboxylic acids, such as vinyl formate, vinyl acetate, vinyl laurate, vinyl benzoate and vinyl versatate, acyryl esters and methacrylic esters, such as methyl acrylate and methyl methacrylate, and also the unsaturated di-carboxylic acids, such as maleic acid, fumaric acid, itaconic acid, and the mono- and diesters of these acids, such as maleic acid dimethyl ester, -diethyl ester and -di-n-butyl ester, maleic acid mono-(2-ethylhexyl)-ester, fumaric acid dimethyl ester, -diethyl ester, -di-n-butyl ester, -di-(2- ethylhexyl)-ester and -di-lauryl ester. Of course, copolymers of more than two monomers can also be produced by the present method.
Alle forbindelser som ved polymerisasjon og kopolymerisasjon av vinylklorid i vandig emulsjon er blitt anvendt som katalysatorer, kan også anvendes for utførelse av den foreliggende fremgangsmåte. For utførelsen av den foreliggende fremgangsmåte foretrekkes også for det meste vannop<p>løselige, radikalgivende materialer, spesielt peroxyforbindelser, som hydrogenperoxyd, persulfater, perborater og tert.butylhydroperoxyd. Peroxydene tilføres som. regel oppløst i vann og i en mengde av 0,005-0,1 vekt% i overensstemmelse med behovet, eventuelt under samtidig anvendelse av 0,005-0,1 vekt% reduksjonsmiddel, som thiosulfat, rongalitt, dithionitt, sulfitt og eventuelt 5-20 ppm salter av kobber og jern. All compounds that have been used as catalysts in the polymerization and copolymerization of vinyl chloride in an aqueous emulsion can also be used for carrying out the present method. For carrying out the present method, mostly water-soluble, radical-generating materials are also preferred, especially peroxy compounds, such as hydrogen peroxide, persulphates, perborates and tert-butyl hydroperoxide. The peroxides are supplied as usually dissolved in water and in an amount of 0.005-0.1% by weight in accordance with the need, possibly with the simultaneous use of 0.005-0.1% by weight reducing agent, such as thiosulphate, rongalite, dithionite, sulphite and possibly 5-20 ppm salts of copper and iron.
Som emulgeringsmidler kan alle vanlig anvendte anioniske, kationiske og ikke-ioniske emulgeringsmidler anvendes, som f.eks. fettsåper og salter derav, alkylsulfonater, alkylsulfater, poly-ethylensulfater, alkylarylsulfonater, sulforavsyreester, del-fos-forsyreester, alkylammoniumsalter eller også alkylfenoler med 5-30 molekylenheter ethylenoxyd, og dessuten fettalkoholer. Emulger-ingsmidlene anvendes i en mengde av 0,1-5 vekt%, basert på monomer-vekten. * ;De polymerisasjonstemperaturer som skal anvendes, ligger innen de grenser som er vanlige ved emulsjonspolymerisasjon av vinylklorid. Som regel er polymerisasjonstem<p>eraturene mellom -20 og 80°C, og fortrinnsvis anvendes temperaturer mellom 30 og 70°C, idet polymerisasjonen som regel forløper ved en i det vesentlige konstant temperatur. Under<p>olymerisasjonsreaksjonen bør emul-sjonens pH ligge mellom 4 og 10, og den kan eventuelt holdes innen dette område ved anvendelse av en pufferblanding. ;Polymerisasjonen utføres vanligvis under et trykk som til-svarer det selvinnstillende vinylkloridtrykk.. Avhengig av poly-merisas j onstemperaturen er dette 5-15 bar. Det skal i den for-bindelse vises til at den særpregede forholdsregel ifølge oppfinnelsen som går ut på å avslutte polymerisasjonen efter et trykkfall mellom 1 og 3 bar, skal forstås derhen at ved et lavt selvinnstillende trykk avsluttes polymerisasjonen efter et trykkfall, innen den nedre del av det ovenfor angitte område, mens polymerisasjonen ved et høyt selvinnstillende trykk avsluttes innen den øvre del av det ovenfor angitte område. Vannavkjølte autoklaver som er forsynt med omrøringsinnretninger anvendes vanligvis som reaksjonsbeholdere. Dessuten kan autoklavene være utstyrt med tilbakeløpskondensatorer for å øke kjølekapasiteten. ;Polymerisasjonsprosessen forløper på den måte som ellers;er vanlig for polymerisering. • Efter at f.eks. vann, monomerer, emulgeringsmiddel og eventuelt kimlatex er blitt tilført og oppvarmet til polymerisasjonstem<p>eraturen, settes polymerisasjon igang ved tilsetning av katalysator, og ytterligere monomermengder eftertilsettes. Efter at monomertilsetningen er ferdig og efter et begynnende trykkfall, stanses katalysatortilsetningen, og det uomsatte vinylklorid destilleres av. Dette finner vanligvis sted efter 0,1-1 time. Når emulsjonen siktes, fås tydelig en mindre grovgodsmengde enn ved de vanlige prosesser. Emulsjonen viser en vesentlige forbedret stabilitet mot koagulering ved tømming av autoklaven og videretransport ved hjelp av en fortrengningspumpe. ;Polyvinylkloridet hhv. vinylkloridkopolymerene fremstilt;ved den foreliggende fremgangsmåte kan bearbeides videre ved de vanlige metoder, som utfelling, forstøvningstørking eller valse-tørking. , ;Ved den foreliggende fremgangsmåte fås polymeremulsjoner;som er langt bedre istand til å tåle belastningene ved den videre bearbeidelse av polymeremulsjonene enn hva som hittil har vært mulig ved anvendelse av de kjente fremgangsmåter. ;Eksempel 1 (Sammenli<g>ningseksempel);10 000 1 vann, 4000 kg vinylklorid, 60 kg natriumlaurat og 2,5 kg natriumsulfitt tilføres til en 25 m 3 autoklav forsynt med et røreverk og med oppvarmings- og avkjølingsinnretninger. Efter at autoklaven som er trykkfast stengt er blitt oppvarmet til 43°C (tilsvarende et innvendig trykk av 6,5 bar), settes polymerisasjonen igang ved kontinuerlig tilførsel av en vandig 1%-ig oppløsning av kaliumperoxydisulfat. Tilsetningenshastigheten for oppløsningen reguleres slik at temperaturen i autoklaven holdes i det vesentlige konstant. Fra polymerisasjonen er blitt igangsatt eftertilsettes samtidig ytterligere 5000 kg vinylklorid jevnt i løpet av 7 timer. ;Ca. 8 timer efter at polymerisasjonsreaksjonen har begynt, faller trykket i autoklaven. Efter et trykkfall til 3 bar ca. 2 timer efter at trykkfallet har begynt, avbrytes tilførselen av kaliumperoxydisulfatoppløsningen,og det uomsatte vinylklorid destilleres av og emulsjonen avgasses ved forhøyet temperatur ;(ca. 90°C). Emulsjonen blir derefter siktet og tilført for;videre opparbeidelse. En rest på ca. 250 kg fås på sikten, og denne rest består av kuleformige, hårde, små deler. Den siktede emulsjon har en rosa farvetone. ;Eksempel 2 ( Ifølge oppfinnelsen);Samme fremgangsmåte som i eksempel 1 benyttes, men polymerisasjonen avbrytes imidlertid allerede når polymerisasjonstrykket er blitt på 5 bar (ca. 30 minutter efter at trykkfallet har begynt),. Derefter viderebehandles emulsjonen som beskrevet i eksempel 1. ;En siktrest på ca. 50 kg grovgods fraskilles, og emulsjonen er ren hvit. ;Eksempel 3 ( Sammenligningseksempel);10 000 1 vann, 4500 kg vinylklorid, 400 kg kimlatex med 40% tørrstoffinnhold og 2,5 kg natriumsulfitt tilføres til en 25 m<3>autoklav forsynt med et røreverk og med oppvarmings- og avkjølings- innretninger. Efter at autoklaven som er trykkfast stengt er blitt*-oppvarmet til 65°C (tilsvarende et innvendig trykk av 10,5 bar), settes polymerisasjonen igang ved kontinuerlig tilførsel av en vandig 1%-ig oppløsning av kaliumperoxydisulfat. Tilførsels-hastigheten for oppløsningen reguleres slik at temperaturen i autoklaven i det vesentlige holdes konstant. Fra polymerisasjonen har begynt tilsettes samtidig 50 kg natriumdodecylbenzensulfonat i form av en 20%-ig vandig oppløsning og ytterligere efterdosert 5000 kg vinylklorid jevnt i løpet av .4 timer. As emulsifiers, all commonly used anionic, cationic and non-ionic emulsifiers can be used, such as e.g. fatty soaps and their salts, alkylsulfonates, alkyl sulfates, polyethylene sulfates, alkylarylsulfonates, sulforaic acid esters, del-phosphoric acid esters, alkylammonium salts or also alkylphenols with 5-30 molecular units of ethylene oxide, and also fatty alcohols. The emulsifiers are used in an amount of 0.1-5% by weight, based on the monomer weight. * ;The polymerization temperatures to be used are within the limits that are common for emulsion polymerization of vinyl chloride. As a rule, the polymerization temperatures are between -20 and 80°C, and temperatures between 30 and 70°C are preferably used, as the polymerization usually proceeds at an essentially constant temperature. During the polymerization reaction, the pH of the emulsion should lie between 4 and 10, and it can possibly be kept within this range by using a buffer mixture. The polymerization is usually carried out under a pressure corresponding to the self-adjusting vinyl chloride pressure. Depending on the polymerization temperature, this is 5-15 bar. In this connection, it should be pointed out that the distinctive precaution according to the invention, which is to terminate the polymerization after a pressure drop between 1 and 3 bar, is to be understood as meaning that at a low self-adjusting pressure, the polymerization is terminated after a pressure drop, within the lower part of the above-mentioned range, while the polymerization at a high self-adjusting pressure ends within the upper part of the above-mentioned range. Water-cooled autoclaves equipped with stirring devices are usually used as reaction vessels. In addition, the autoclaves can be equipped with reflux condensers to increase the cooling capacity. The polymerization process proceeds in the manner that is otherwise usual for polymerization. • After e.g. water, monomers, emulsifier and possibly seed latex have been added and heated to the polymerization temperature, polymerization is started by adding a catalyst, and further amounts of monomer are subsequently added. After the monomer addition is finished and after an initial pressure drop, the catalyst addition is stopped, and the unreacted vinyl chloride is distilled off. This usually takes place after 0.1-1 hour. When the emulsion is sieved, a smaller amount of coarse material is clearly obtained than with the usual processes. The emulsion shows a significantly improved stability against coagulation when emptying the autoclave and further transport using a displacement pump. Polyvinyl chloride or The vinyl chloride copolymers produced by the present method can be further processed by the usual methods, such as precipitation, spray drying or roller drying. , ;With the present method, polymer emulsions are obtained which are far better able to withstand the loads during the further processing of the polymer emulsions than what has hitherto been possible using the known methods. ;Example 1 (Comparative Example); 10,000 1 of water, 4000 kg of vinyl chloride, 60 kg of sodium laurate and 2.5 kg of sodium sulphite are fed to a 25 m 3 autoclave equipped with an agitator and with heating and cooling devices. After the pressure-tight closed autoclave has been heated to 43°C (corresponding to an internal pressure of 6.5 bar), the polymerization is started by continuous supply of an aqueous 1% solution of potassium peroxydisulfate. The rate of addition of the solution is regulated so that the temperature in the autoclave is kept essentially constant. From the time the polymerization has been initiated, a further 5,000 kg of vinyl chloride is added at the same time evenly over the course of 7 hours. ;About. 8 hours after the polymerization reaction has started, the pressure in the autoclave drops. After a pressure drop to 3 bar approx. 2 hours after the pressure drop has begun, the supply of the potassium peroxydisulfate solution is interrupted, and the unreacted vinyl chloride is distilled off and the emulsion is degassed at an elevated temperature; (approx. 90°C). The emulsion is then sieved and added for further processing. A remainder of approx. 250 kg is obtained on the sieve, and this residue consists of spherical, hard, small parts. The sieved emulsion has a pink tint. ;Example 2 (According to the invention);The same method as in example 1 is used, but the polymerization is already interrupted when the polymerization pressure has reached 5 bar (approx. 30 minutes after the pressure drop has begun). The emulsion is then further processed as described in example 1. A sieve residue of approx. 50 kg of coarse material is separated, and the emulsion is pure white. ;Example 3 (Comparative example);10,000 1 water, 4500 kg of vinyl chloride, 400 kg of germ latex with a 40% solids content and 2.5 kg of sodium sulphite are fed to a 25 m<3>autoclave equipped with an agitator and with heating and cooling devices . After the pressure-tight autoclave has been* heated to 65°C (corresponding to an internal pressure of 10.5 bar), the polymerization is started by continuous supply of an aqueous 1% solution of potassium peroxydisulfate. The supply rate for the solution is regulated so that the temperature in the autoclave is essentially kept constant. From the time the polymerization has begun, 50 kg of sodium dodecylbenzenesulfonate in the form of a 20% aqueous solution and a further post-dosed 5000 kg of vinyl chloride are added at the same time over the course of .4 hours.
Ca. 5 1/2 time efter at polymerisasjonsreaksjonen har begynt, faller trykket i autoklaven. Efter at trykket har falt til 5 bar ca. 2 1/2 time efter at trykket har begynt å falle, avbrytes til-førselen av kaliumperoxydisulfatoppløsningen, og det uomsatte vinylklorid destilleres av. Emulsjonen utsettes derefter for en fjernelse av restgass ved forhøyet temperatur (ca.90°C) og siktes og tilføres for videre o<pp>arbeidelse. Ca. 150 kg grove deler fås som siktrest. Når emulsjonen transporteres ved hjelp av en roterende fortrengningspumpe, dannes ytterligere koagulat på grunn av at emulsjonen har en lav stabilitet overfor skjærkrefter, og koagulatet må fraskilles og fører dessuten til beskadigelse av pumpens rotor. About. 5 1/2 hours after the polymerization reaction has begun, the pressure in the autoclave drops. After the pressure has dropped to 5 bar approx. 2 1/2 hours after the pressure has begun to fall, the supply of the potassium peroxydisulfate solution is interrupted, and the unreacted vinyl chloride is distilled off. The emulsion is then subjected to a removal of residual gas at an elevated temperature (approx. 90°C) and sieved and supplied for further processing. About. 150 kg of coarse parts are available as sieve residue. When the emulsion is transported by means of a rotary displacement pump, additional coagulate is formed due to the fact that the emulsion has a low stability to shear forces, and the coagulate must be separated and also leads to damage to the pump's rotor.
Eksempel 4 ( Ifølge oppfinnelsen)Example 4 (According to the invention)
Samme fremgangsmåte som i eksempel 3 benyttes, men tilførselen av kaliumperoxydisulfatoppløsningen avbrytes imidlertid allerede når det innvendige trykk i autoklaven har nådd 8,5 bar. Derefter benyttes samme fremgangsmåte som beskrevet i eksempel 3. 50 kg grove deler fås som siktrest, og ved transport ved hjelp av fortrengningspumpen dannes intet ytterligere koagulat. The same method as in example 3 is used, but the supply of the potassium peroxydisulphate solution is interrupted already when the internal pressure in the autoclave has reached 8.5 bar. The same procedure as described in example 3 is then used. 50 kg of coarse parts are obtained as sieve residue, and no further coagulate is formed during transport using the displacement pump.
Claims (1)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19762659535 DE2659535A1 (en) | 1976-12-30 | 1976-12-30 | PROCESS FOR THE PRODUCTION OF POLYVINYL CHLORIDE POLYMERISATES |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO774497L true NO774497L (en) | 1978-07-03 |
Family
ID=5997021
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO774497A NO774497L (en) | 1976-12-30 | 1977-12-29 | PROCEDURE FOR PREPARING POLYVINYL CHLORIDE POLYMERS |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS5384090A (en) |
| BE (1) | BE862411A (en) |
| DE (1) | DE2659535A1 (en) |
| FR (1) | FR2376162A1 (en) |
| IT (1) | IT1092242B (en) |
| NL (1) | NL7712698A (en) |
| NO (1) | NO774497L (en) |
| SE (1) | SE7714917L (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL46851C (en) * | 1935-09-28 | |||
| US2689242A (en) * | 1951-03-20 | 1954-09-14 | Monsanto Chemicals | ph control in the emulsion polymerization of vinyl chloride |
-
1976
- 1976-12-30 DE DE19762659535 patent/DE2659535A1/en active Pending
-
1977
- 1977-11-17 NL NL7712698A patent/NL7712698A/en not_active Application Discontinuation
- 1977-12-19 IT IT52261/77A patent/IT1092242B/en active
- 1977-12-28 JP JP15864377A patent/JPS5384090A/en active Pending
- 1977-12-28 BE BE183915A patent/BE862411A/en unknown
- 1977-12-29 SE SE7714917A patent/SE7714917L/en unknown
- 1977-12-29 FR FR7739618A patent/FR2376162A1/en not_active Withdrawn
- 1977-12-29 NO NO774497A patent/NO774497L/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| FR2376162A1 (en) | 1978-07-28 |
| SE7714917L (en) | 1978-07-01 |
| DE2659535A1 (en) | 1978-07-06 |
| JPS5384090A (en) | 1978-07-25 |
| NL7712698A (en) | 1978-07-04 |
| IT1092242B (en) | 1985-07-06 |
| BE862411A (en) | 1978-06-28 |
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