CA2346993A1 - Redox polymerization process - Google Patents
Redox polymerization process Download PDFInfo
- Publication number
- CA2346993A1 CA2346993A1 CA002346993A CA2346993A CA2346993A1 CA 2346993 A1 CA2346993 A1 CA 2346993A1 CA 002346993 A CA002346993 A CA 002346993A CA 2346993 A CA2346993 A CA 2346993A CA 2346993 A1 CA2346993 A1 CA 2346993A1
- Authority
- CA
- Canada
- Prior art keywords
- tert
- butyl
- temperature
- polymerization
- process according
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
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
- C08F2/00—Processes of polymerisation
- C08F2/12—Polymerisation in non-solvents
- C08F2/16—Aqueous medium
- C08F2/22—Emulsion polymerisation
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polymerisation Methods In General (AREA)
- Polymerization Catalysts (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Paints Or Removers (AREA)
- Adhesives Or Adhesive Processes (AREA)
Abstract
A process for emulsion polymerization comprising the steps of reacting together a polymerization initiator, a reductor, and a polymerizable species, with the proviso that the polymerization initiator is not a hydroperoxide, characterized in that the polymerization initiator and the reductor are reacted together to provide a free radical moiety of the initiator, whereupon this free radical moiety initiates polymerization of the polymerizable species, this step being carried out at an initial cold start temperature, whereafter the temperature is increased to follow a temperature profile to a final preselected polymerization temperature.
Description
REDOX POLYMERIZATION PROCESS
The present invention relates to a process for emulsion polymerization, to the polymers obtainable by such a process, and to their uses.
The production of water based resins, for example by means of emulsion polymerization techniques, is carried out thermally with inorganic persulfates. A
problem with thermal polymerization is the process time, which leads to a less than desirable reactor output.
io An object of the present invention is to provide an alternative polymerization process which aims to improve the process time.
The first aspect of the present invention provides a process according to claim 1.
Since the polymerizatian process according to the present invention provides a free radical initiator moiety by means of a redox reaction instead of by thermal decomposition, the polymerization can be carried out with a so-called "cold start", which involves the process time being reduced and the reactor output per unit 2 o time being increased.
A redox polymerization is known for tertiary butyl hydroperoxide "Trigonox A-W70". The inventors have shown, however, that a redox polymerization utilizing other organic peroxides provides unexpectedly good results.
The inventors have shown that polymerization can start at a lower initial temperature, which means that because of the longer "heating-up" time necessary in thermal polymerization, the polymerization time can be reduced utilizing the process of the current invention.
The inventors have furthermore demonstrated that the process according to the present invention enables a polymer with a very low residual monomer level to be GONFiRMATION COPY
The present invention relates to a process for emulsion polymerization, to the polymers obtainable by such a process, and to their uses.
The production of water based resins, for example by means of emulsion polymerization techniques, is carried out thermally with inorganic persulfates. A
problem with thermal polymerization is the process time, which leads to a less than desirable reactor output.
io An object of the present invention is to provide an alternative polymerization process which aims to improve the process time.
The first aspect of the present invention provides a process according to claim 1.
Since the polymerizatian process according to the present invention provides a free radical initiator moiety by means of a redox reaction instead of by thermal decomposition, the polymerization can be carried out with a so-called "cold start", which involves the process time being reduced and the reactor output per unit 2 o time being increased.
A redox polymerization is known for tertiary butyl hydroperoxide "Trigonox A-W70". The inventors have shown, however, that a redox polymerization utilizing other organic peroxides provides unexpectedly good results.
The inventors have shown that polymerization can start at a lower initial temperature, which means that because of the longer "heating-up" time necessary in thermal polymerization, the polymerization time can be reduced utilizing the process of the current invention.
The inventors have furthermore demonstrated that the process according to the present invention enables a polymer with a very low residual monomer level to be GONFiRMATION COPY
obtained, whilst, with respect to thermal polymerization, the amount of initiator used can be reduced.
Good results have been achieved under the conditions as defined in claims 2-6.
The polymerization initiator is most preferably a substantially non-water soluble initiator, such as defined in claim 7 or 8, since these non-water soluble initiators yield an unexpectedly high efficiency in polymerization.
to This higher efficiency results in shorter polymerization times and in polymer resins with improved properties. The higher efficiency of the organic peroxides is expressed by the low level of residual monomers and by the low molecular weights (Mw/Mn) of the polymers formed.
i5 Furthermore, the conductivity of the resins initiated with the organic peroxide/redox system is lower than for corresponding resins that were initiated by persulfates.
The reductor of the redox system preferably is chosen from the following group:
Zo sodium formaldehyde sulfoxyiate (SFS), sodium bisulfate, Ascorbic acid (vitamin C), aldehydes, for example glutaraldehyde, sodium metabisulfite, sodium dithionate, and sugars, wherein the reductor most preferably is sodium formaldehyde sulfoxide.
a5 The polymerizable species preferably is chosen from the following group:
acrylonitrile, acrylic acid, methyl acrylate, ethyl acrylate, butyl acrylate, ethylhexyl acrylate, methoxyethyl acrylate, dimethyl aminoacrylate, methacrylic acid, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacryfate, 2-ethylhexyl methacrylate, lauryl methacrylate, stearic 3o methacrylate, dimethyl aminomethacrylate, aliyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxypropyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl methacrylate, acrylamide, methacrylamide, glycidyl acrylate, vinyl ester of versatic acid, styrene, para-methyl styrene, vinyl acetate, alpha-methyl styrene, wherein the polymerizable species most preferably comprises vinyl acetate s and/or the vinyl ester of versatic acid.
Further preferred process conditions are detailed in claims 11-15.
The polymerization is carried out in a conventional emulsion, for example in a to mixture of anionic and non-ionic surfactants such as Witconate (sodium alpha-olefin sulfonate) and Syntopon (ethoxylated nonylphenol); however, other emulsifiers or mixtures are also possible.
This emulsifier solution preferably is a mixture of nonionic and anionic emulsifiers 15 and most preferably is selected from the group consisting essentially of:
long-chain aliphatic carboxylates (ionic) - alkylbenzene sulfonates (ionic) - alkyl sulphates (ionic) - dialkylsulphosuccinate (ionic) so - ethoxylated alcohols (nonionic) - ethoxylated alkyl phenols (nonionic) - ethoxylated amine or amides (nonionic).
A second aspect of the present invention provides a polymer obtainable as according to this process.
The invention will now be further elucidated by way of the following examples.
Examples 1-6 are comparative examples and Examples 7-12 are examples according to the present invention using a redox system. Examples 3, 4, 6, 8-3o were subjected to a temperature profile increasing from an initial temperature to a final temperature, i.e. subjected to a so-called "cold-start", and Example 7 was carried out at constant temperature.
ProcedurP,sf~r~naration s The polymerization in all the examples was carried out in a 0.25 L glass reactor with a stirrer under nitrogen. A seed was prepared first by adding 10% of the reactive components at polymerization temperature.
The preparation of the seed was carried out as follows;
io The reactor was filled with buffered (NaAc/HAc) emulsifier solution (Witconate/Syntopon), prepared with oxygen-free deionized water. At the polymerization temperature 10% of the pre-emulsion containing soaps (Witconate and Syntopon), monomers, and, in the case of the redox system according to the present invention, also reductor and catalyst, were added. In addition the solution i5 or pre-emulsion of the initiator was added to achieve control over the accurate dosing of the initiator.
After a polymerization time of 30 minutes the remaining monomers, pre-emulsion, and initiator solution were dosed in 2.5 hours. In Examples 3, 4, 6, 8-12 the ao temperature was increased to the final temperature in the same period, following a temperature profile. The final temperature was maintained for 1 hour.
The composition of the buffered soap solution used was as follows:
NaAC.3aq 0.25 g (sodium acetate) as HAc 0.11 g (acetic acid) H20 30.3 g Witconate 0.38 g (soap) Syntopon 0.38 g (soap) Thermal system The temperature was kept at 70°C during the polymerization. The composition of the used pre-emulsion was:
Witconate 1.28 g Syntopon 1.28 g H20 34.43 g Vac (vinyl acetate) 52.5 g (monomer) VEOVA (vinyl ester of versatic acid) 22.5 g (monomer) The initiator solution was composed of 4.18 mmoles ammoniumlsodium or potassium persulfate in 25 g H20. The total process time including the time needed for heating up the reactor contents to 70°C before polymerization amounted to 5.5 hours.
to Exam I~es 2, 5, 7 The temperature was kept at 70°C (Examples 2, 5) and 20°C
(Example 7), respectively. The composition of the used pre-emulsions was as follows:
Witconate 1.28 g Syntopon 1.28 g H20 34.43 g Peroxide 1.04-4.18 mmoles as mentioned in the examples Vac (vinyl acetate) 52.5 g (monomer) VEOVA (vinyl ester of 22.5 g (monomer) versatic acid) i5 The reductor SFS (sodium formaldehyde sulfoxyde: 0.65 g) and the catalyst (FeS04 16.7 mg) were dissolved in 25 g H20.
The total process time was 4 hours.
Good results have been achieved under the conditions as defined in claims 2-6.
The polymerization initiator is most preferably a substantially non-water soluble initiator, such as defined in claim 7 or 8, since these non-water soluble initiators yield an unexpectedly high efficiency in polymerization.
to This higher efficiency results in shorter polymerization times and in polymer resins with improved properties. The higher efficiency of the organic peroxides is expressed by the low level of residual monomers and by the low molecular weights (Mw/Mn) of the polymers formed.
i5 Furthermore, the conductivity of the resins initiated with the organic peroxide/redox system is lower than for corresponding resins that were initiated by persulfates.
The reductor of the redox system preferably is chosen from the following group:
Zo sodium formaldehyde sulfoxyiate (SFS), sodium bisulfate, Ascorbic acid (vitamin C), aldehydes, for example glutaraldehyde, sodium metabisulfite, sodium dithionate, and sugars, wherein the reductor most preferably is sodium formaldehyde sulfoxide.
a5 The polymerizable species preferably is chosen from the following group:
acrylonitrile, acrylic acid, methyl acrylate, ethyl acrylate, butyl acrylate, ethylhexyl acrylate, methoxyethyl acrylate, dimethyl aminoacrylate, methacrylic acid, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacryfate, 2-ethylhexyl methacrylate, lauryl methacrylate, stearic 3o methacrylate, dimethyl aminomethacrylate, aliyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxypropyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl methacrylate, acrylamide, methacrylamide, glycidyl acrylate, vinyl ester of versatic acid, styrene, para-methyl styrene, vinyl acetate, alpha-methyl styrene, wherein the polymerizable species most preferably comprises vinyl acetate s and/or the vinyl ester of versatic acid.
Further preferred process conditions are detailed in claims 11-15.
The polymerization is carried out in a conventional emulsion, for example in a to mixture of anionic and non-ionic surfactants such as Witconate (sodium alpha-olefin sulfonate) and Syntopon (ethoxylated nonylphenol); however, other emulsifiers or mixtures are also possible.
This emulsifier solution preferably is a mixture of nonionic and anionic emulsifiers 15 and most preferably is selected from the group consisting essentially of:
long-chain aliphatic carboxylates (ionic) - alkylbenzene sulfonates (ionic) - alkyl sulphates (ionic) - dialkylsulphosuccinate (ionic) so - ethoxylated alcohols (nonionic) - ethoxylated alkyl phenols (nonionic) - ethoxylated amine or amides (nonionic).
A second aspect of the present invention provides a polymer obtainable as according to this process.
The invention will now be further elucidated by way of the following examples.
Examples 1-6 are comparative examples and Examples 7-12 are examples according to the present invention using a redox system. Examples 3, 4, 6, 8-3o were subjected to a temperature profile increasing from an initial temperature to a final temperature, i.e. subjected to a so-called "cold-start", and Example 7 was carried out at constant temperature.
ProcedurP,sf~r~naration s The polymerization in all the examples was carried out in a 0.25 L glass reactor with a stirrer under nitrogen. A seed was prepared first by adding 10% of the reactive components at polymerization temperature.
The preparation of the seed was carried out as follows;
io The reactor was filled with buffered (NaAc/HAc) emulsifier solution (Witconate/Syntopon), prepared with oxygen-free deionized water. At the polymerization temperature 10% of the pre-emulsion containing soaps (Witconate and Syntopon), monomers, and, in the case of the redox system according to the present invention, also reductor and catalyst, were added. In addition the solution i5 or pre-emulsion of the initiator was added to achieve control over the accurate dosing of the initiator.
After a polymerization time of 30 minutes the remaining monomers, pre-emulsion, and initiator solution were dosed in 2.5 hours. In Examples 3, 4, 6, 8-12 the ao temperature was increased to the final temperature in the same period, following a temperature profile. The final temperature was maintained for 1 hour.
The composition of the buffered soap solution used was as follows:
NaAC.3aq 0.25 g (sodium acetate) as HAc 0.11 g (acetic acid) H20 30.3 g Witconate 0.38 g (soap) Syntopon 0.38 g (soap) Thermal system The temperature was kept at 70°C during the polymerization. The composition of the used pre-emulsion was:
Witconate 1.28 g Syntopon 1.28 g H20 34.43 g Vac (vinyl acetate) 52.5 g (monomer) VEOVA (vinyl ester of versatic acid) 22.5 g (monomer) The initiator solution was composed of 4.18 mmoles ammoniumlsodium or potassium persulfate in 25 g H20. The total process time including the time needed for heating up the reactor contents to 70°C before polymerization amounted to 5.5 hours.
to Exam I~es 2, 5, 7 The temperature was kept at 70°C (Examples 2, 5) and 20°C
(Example 7), respectively. The composition of the used pre-emulsions was as follows:
Witconate 1.28 g Syntopon 1.28 g H20 34.43 g Peroxide 1.04-4.18 mmoles as mentioned in the examples Vac (vinyl acetate) 52.5 g (monomer) VEOVA (vinyl ester of 22.5 g (monomer) versatic acid) i5 The reductor SFS (sodium formaldehyde sulfoxyde: 0.65 g) and the catalyst (FeS04 16.7 mg) were dissolved in 25 g H20.
The total process time was 4 hours.
Exam leo s 3. 44 6, 8-12 The polymerization temperature was kept at 20°C for the first 30 minutes to prepare a seed. The temperature was then increased by 20°C/hour to 70°C
following a temperature profile.
It is noted that other starting temperatures and temperature programmes can be used, either for initiating polymerization or for initiating and completing polymerization.
io In all the examples the residual monomers were determined by gas chromatography (GC). The molecular weight of the prepared polymers was determined by gel permeation chromatography (GPC) with polystyrene for calibration. The conversion/solids content was determined by standard procedure. The viscosity was determined using a Brookfield digital viscometer.
is The results are shown in Table 1.
F_xamples 13-24 ao Procedure of pre ap ration The polymerization in all examples was carried out in a 0.25 L glass reactor with a stirrer under nitrogen. A seed was prepared first by adding 10% of the reactive components at polymerization temperature.
is The preparation of the seed was carried out as follows:
The reactor was filled with the emulsifier solution (sodium lauryl sulfate in water) prepared with oxygen-free deionized water. ~ At the starting polymerization temperature 10% of the pre-emulsion containing soap, monomers, and in the case of the redox system, also reductor and catalyst, were added. In addition the 3 o solution or pre-emulsion of the initiator was added to achieve control over the accurate dosing of the initiator.
After a polymerization time of 30 minutes the remaining monomers, pre-emulsion, and initiator solution were dosed in 2.5 hours. The temperature was increased to s the final temperature in the same period, following a temperature profile.
The final temperature was maintained for 1 hour.
The composition of the soap solution was as follows:
0.10 g sodium lauryl sulfate (emulsifier) l0 25.0 ml deionized water Pre-emulsion:
1.60 g sodium lauryl sulfate 30 ml deionized water is 70 g monomer mixture (butylacrylate I styrene I methacrylic acid = 6/4/0.1) including the initiator (1.04 meq), if not water-soluble.
The reductor SFS (sodium formaldehyde sulfoxylate 0.16 g) and the catalyst (Fe"S04 2.8 mg) were dissolved in 10 ml water.
ao The molar ratio oxidator: reductor: Fe = 1: 1: 0.01 The results are shown in Tables 2 and 3.
ON ~ 0 O r M n O- p N
O pf 0 N D d t ~ iC O ~
e-01O ' d' OO !
1 C' N r r ~ T r r rr r r' U Mc0M ~ ~! ~ e- N NCo~ -c C I
! n47~ LnM M M M N~ e-M
Of~.~f'07O) ~ a~0N MOa,~ O
O ~ ' , 0 InM C V e d o o o o o 3 ~o,~ ~ ~ ao,~ ~ p O
t0sth i~N fC r r N~
o ~M ~ N O N ~ - MN O O
N M O O
N O ~ O O O O
N O
o ~O O O O ~ ~ O Oq U
C 0 t~M~ ~ ~ONO~
~~7N ~ O - O OO O
O
OO O O O O O O OO O
N
N
O ~ ~ O Q OO O Q
X ~ ~ X ~ X ~ NN d H O ~ '~O v- O W -'_L ~-~ U ~ - UU U
p O0 0 p c U n.~ U r- U n.~~ ~ ~
Vo n ~ o n o n ~n n n ~i i h I ~ f~ i N ;
N N
N N NN N N
~ NN N <-N N N N r~c70 Cat :D ' ' V ~tN V V ~ ~ N
C7d N N N N
N
N
~ ~~ d I T . ~X ~ X
p D X
X
j, j, O OO O O
> > o, a~a~a~a~a~
m m ~ a aa a a ~ ~ ~ ~ ~~ ~ ~
~ a~ m 'f' ~
'D ~ ~ ~ 7O 7 7 ...'D m ~X ..r X , O O ~ ~w r O O ~
w w ~
00a0CD00O ~ ~ C1~G~d OO O O ~ O ~ . ~ ~r O - - ~
~
O
p r O
m ~~ ~ ~ Q~ Q~ L U UU U Ut_ NT
NN N N X . . X XX X X
Y Y > X X I-1-1-~-I--7 ~
- I-YY: I- F a~
s s a E
p X O r N
L1J r(VM ~ lf7(O !~.00Os-m-r 0o w ~o r MM M tnr <O
Ll NN ~t etet M
M~ ~~ OMD
OO CO 00~
O
O
OO O OO
O
OO O O~
O
OO M s!'r ~
rO M r ~" U!l7M M
O
~ r OO O OO
O
OO O OO
O
OO M Ntn O
3. NN r COO
lf) ppr r ~N
O
~tYN N1 ~D
d' N G1 MM tD
l0 C ~ ~ Nr N ~
>
O O rO O CC
O CO
O
..
~0 ~
d COM 'D 'O'C7 d O ~ ~.' OO C CC
- ~ O
e ..
td 00N N ~f71.n tn ~ OM N (V(O
O
_ ~ Mv ~~ v.-CO
C -U
N !L
'Q ~ ~ ~fr '~ d~V
:v rN r rr ~ CV
C UU U UU
U
~ QQ Q QQ
Q
zz ~z ~Z
-v ~
~ ~N ~ ~S~V r~~
N
~' >> > >> V
uJ > ~
E- o ~
.
a a~
ca -v N O ~ r..X
~ ~ UN ~~ II
II
_ Y x X~ ~ 'C3 H
F f-.
G C
r O N~ etM
d N Nr ~ CC
et P. Lnf~..N tn O r Oe~'00M
O tt7st~1~.cM1n O O O O O
O O OO O O
COOo ~Tp O CG
~ ~
G ~ CO~O V N
M P
r r. r et O O
O O OO O O
O O OO GOd' M O f~r~O i~.
M ~ MQ1tD~O
N
~ ~ (OIwt7~ N
H
m ~ O ~ ~
O t N Zf0 'C7 m t 0 r ~-r-C C
r C O
l0 d -o~ o-ti v ~
N
c c oc O c a o C
mo - Opr MO O M~ C
O ~ M 00COf~M
N u ' (n X ~ ~tst~ st~tt5 t a U
X
.-, c6 p C = ~ U ~L
O .r R,,Ø, H lL C 0 0 00 0 0V p m 'O ~ :=. r CVrhlr ~-C6 N 0 ~ O
~
~ ~
l N ' p ~
i O
U
O
X p H Q Q QQ Q Q~ j, -~
O
V G m ~ ~ ~~ ~ ~~ X .,7 L
o ~, ~ a a aa a a~, ~ .~ ~ _ ~ Q
' H L U O m m mm Lnm_ ~ ~ ~ (~ ~, ~_ N -fl O ~ ~ ~' O' ~ ~-' O
V
W H- ~ cnf~f~c~InfO
LY
a. N 7. ~
~ 'a ~ ~ ' _ .~ O
_ O O ~ U ~ II II
~
M O ~ t,.. c c U
x II ~ X
II
O o ~ V N N ~- O
T II II ~
~ U N .-~
O Y x ~ ~ ~ ~ X X X ca v ~
F I C C (n H I- I- J
- F
-m o . WO 00/22003 PCT/EP99/07769 Results As reference the emulsion copolymerization of vinylacetate and VeoVa with potassium persulfate at 70°C was used (thermal conditions).
The results show low residual monomer levels for the non-water soluble organic peroxides (peroxyesters) under redox conditions. As the efficiency of the non-water-soluble peroxyesters such as Trigonox C was much higher than that of the water-soluble persulfates and hydroperoxides, the levels of addition to could be lowered to 20-40% of the original milli-equivalents of initiator used.
Due to lower amounts of initiator and reductor, a higher value for pH and lower values for the conductivity were obtained. The prepared polymer had molecular weights (Mw/Mn) comparable with those of the reference copolymer of VeoVaNAc.
The peroxyesters such as Trigonox 21 gave a high conversion of monomers at ambient temperature.
The invention is not limited to the above description; rather, the requested ao rights are determined by the following claims.
following a temperature profile.
It is noted that other starting temperatures and temperature programmes can be used, either for initiating polymerization or for initiating and completing polymerization.
io In all the examples the residual monomers were determined by gas chromatography (GC). The molecular weight of the prepared polymers was determined by gel permeation chromatography (GPC) with polystyrene for calibration. The conversion/solids content was determined by standard procedure. The viscosity was determined using a Brookfield digital viscometer.
is The results are shown in Table 1.
F_xamples 13-24 ao Procedure of pre ap ration The polymerization in all examples was carried out in a 0.25 L glass reactor with a stirrer under nitrogen. A seed was prepared first by adding 10% of the reactive components at polymerization temperature.
is The preparation of the seed was carried out as follows:
The reactor was filled with the emulsifier solution (sodium lauryl sulfate in water) prepared with oxygen-free deionized water. ~ At the starting polymerization temperature 10% of the pre-emulsion containing soap, monomers, and in the case of the redox system, also reductor and catalyst, were added. In addition the 3 o solution or pre-emulsion of the initiator was added to achieve control over the accurate dosing of the initiator.
After a polymerization time of 30 minutes the remaining monomers, pre-emulsion, and initiator solution were dosed in 2.5 hours. The temperature was increased to s the final temperature in the same period, following a temperature profile.
The final temperature was maintained for 1 hour.
The composition of the soap solution was as follows:
0.10 g sodium lauryl sulfate (emulsifier) l0 25.0 ml deionized water Pre-emulsion:
1.60 g sodium lauryl sulfate 30 ml deionized water is 70 g monomer mixture (butylacrylate I styrene I methacrylic acid = 6/4/0.1) including the initiator (1.04 meq), if not water-soluble.
The reductor SFS (sodium formaldehyde sulfoxylate 0.16 g) and the catalyst (Fe"S04 2.8 mg) were dissolved in 10 ml water.
ao The molar ratio oxidator: reductor: Fe = 1: 1: 0.01 The results are shown in Tables 2 and 3.
ON ~ 0 O r M n O- p N
O pf 0 N D d t ~ iC O ~
e-01O ' d' OO !
1 C' N r r ~ T r r rr r r' U Mc0M ~ ~! ~ e- N NCo~ -c C I
! n47~ LnM M M M N~ e-M
Of~.~f'07O) ~ a~0N MOa,~ O
O ~ ' , 0 InM C V e d o o o o o 3 ~o,~ ~ ~ ao,~ ~ p O
t0sth i~N fC r r N~
o ~M ~ N O N ~ - MN O O
N M O O
N O ~ O O O O
N O
o ~O O O O ~ ~ O Oq U
C 0 t~M~ ~ ~ONO~
~~7N ~ O - O OO O
O
OO O O O O O O OO O
N
N
O ~ ~ O Q OO O Q
X ~ ~ X ~ X ~ NN d H O ~ '~O v- O W -'_L ~-~ U ~ - UU U
p O0 0 p c U n.~ U r- U n.~~ ~ ~
Vo n ~ o n o n ~n n n ~i i h I ~ f~ i N ;
N N
N N NN N N
~ NN N <-N N N N r~c70 Cat :D ' ' V ~tN V V ~ ~ N
C7d N N N N
N
N
~ ~~ d I T . ~X ~ X
p D X
X
j, j, O OO O O
> > o, a~a~a~a~a~
m m ~ a aa a a ~ ~ ~ ~ ~~ ~ ~
~ a~ m 'f' ~
'D ~ ~ ~ 7O 7 7 ...'D m ~X ..r X , O O ~ ~w r O O ~
w w ~
00a0CD00O ~ ~ C1~G~d OO O O ~ O ~ . ~ ~r O - - ~
~
O
p r O
m ~~ ~ ~ Q~ Q~ L U UU U Ut_ NT
NN N N X . . X XX X X
Y Y > X X I-1-1-~-I--7 ~
- I-YY: I- F a~
s s a E
p X O r N
L1J r(VM ~ lf7(O !~.00Os-m-r 0o w ~o r MM M tnr <O
Ll NN ~t etet M
M~ ~~ OMD
OO CO 00~
O
O
OO O OO
O
OO O O~
O
OO M s!'r ~
rO M r ~" U!l7M M
O
~ r OO O OO
O
OO O OO
O
OO M Ntn O
3. NN r COO
lf) ppr r ~N
O
~tYN N1 ~D
d' N G1 MM tD
l0 C ~ ~ Nr N ~
>
O O rO O CC
O CO
O
..
~0 ~
d COM 'D 'O'C7 d O ~ ~.' OO C CC
- ~ O
e ..
td 00N N ~f71.n tn ~ OM N (V(O
O
_ ~ Mv ~~ v.-CO
C -U
N !L
'Q ~ ~ ~fr '~ d~V
:v rN r rr ~ CV
C UU U UU
U
~ QQ Q QQ
Q
zz ~z ~Z
-v ~
~ ~N ~ ~S~V r~~
N
~' >> > >> V
uJ > ~
E- o ~
.
a a~
ca -v N O ~ r..X
~ ~ UN ~~ II
II
_ Y x X~ ~ 'C3 H
F f-.
G C
r O N~ etM
d N Nr ~ CC
et P. Lnf~..N tn O r Oe~'00M
O tt7st~1~.cM1n O O O O O
O O OO O O
COOo ~Tp O CG
~ ~
G ~ CO~O V N
M P
r r. r et O O
O O OO O O
O O OO GOd' M O f~r~O i~.
M ~ MQ1tD~O
N
~ ~ (OIwt7~ N
H
m ~ O ~ ~
O t N Zf0 'C7 m t 0 r ~-r-C C
r C O
l0 d -o~ o-ti v ~
N
c c oc O c a o C
mo - Opr MO O M~ C
O ~ M 00COf~M
N u ' (n X ~ ~tst~ st~tt5 t a U
X
.-, c6 p C = ~ U ~L
O .r R,,Ø, H lL C 0 0 00 0 0V p m 'O ~ :=. r CVrhlr ~-C6 N 0 ~ O
~
~ ~
l N ' p ~
i O
U
O
X p H Q Q QQ Q Q~ j, -~
O
V G m ~ ~ ~~ ~ ~~ X .,7 L
o ~, ~ a a aa a a~, ~ .~ ~ _ ~ Q
' H L U O m m mm Lnm_ ~ ~ ~ (~ ~, ~_ N -fl O ~ ~ ~' O' ~ ~-' O
V
W H- ~ cnf~f~c~InfO
LY
a. N 7. ~
~ 'a ~ ~ ' _ .~ O
_ O O ~ U ~ II II
~
M O ~ t,.. c c U
x II ~ X
II
O o ~ V N N ~- O
T II II ~
~ U N .-~
O Y x ~ ~ ~ ~ X X X ca v ~
F I C C (n H I- I- J
- F
-m o . WO 00/22003 PCT/EP99/07769 Results As reference the emulsion copolymerization of vinylacetate and VeoVa with potassium persulfate at 70°C was used (thermal conditions).
The results show low residual monomer levels for the non-water soluble organic peroxides (peroxyesters) under redox conditions. As the efficiency of the non-water-soluble peroxyesters such as Trigonox C was much higher than that of the water-soluble persulfates and hydroperoxides, the levels of addition to could be lowered to 20-40% of the original milli-equivalents of initiator used.
Due to lower amounts of initiator and reductor, a higher value for pH and lower values for the conductivity were obtained. The prepared polymer had molecular weights (Mw/Mn) comparable with those of the reference copolymer of VeoVaNAc.
The peroxyesters such as Trigonox 21 gave a high conversion of monomers at ambient temperature.
The invention is not limited to the above description; rather, the requested ao rights are determined by the following claims.
Claims (16)
1. A Process for emulsion polymerization comprising the steps:
- of reacting together a polymerization initiator, a reductor, and a polymerizable species, with the proviso that the polymerization initiator is not a hydroperoxide, wherein the polymerization initiator and the reductor are reacted together to provide a free radical moiety of the initiator, characterized in that the free radical moiety initiates polymerization of the polymerizable species, this step being carried out at an initial cold start temperature, whereafter the temperature is actively increased by means of an external heat supply source so that the polymerization follows an increasing temperature profile to a final preselected polymerization temperature, this final temperature being higher than the cold start temperature, wherein the polymerization initiators are selected from the group consisting essentially of aliphatic and aromatic peroxy esters and peroxy carbonates.
12a
- of reacting together a polymerization initiator, a reductor, and a polymerizable species, with the proviso that the polymerization initiator is not a hydroperoxide, wherein the polymerization initiator and the reductor are reacted together to provide a free radical moiety of the initiator, characterized in that the free radical moiety initiates polymerization of the polymerizable species, this step being carried out at an initial cold start temperature, whereafter the temperature is actively increased by means of an external heat supply source so that the polymerization follows an increasing temperature profile to a final preselected polymerization temperature, this final temperature being higher than the cold start temperature, wherein the polymerization initiators are selected from the group consisting essentially of aliphatic and aromatic peroxy esters and peroxy carbonates.
12a
2. Process according to claim 1 carried out at an initial temperature of up to 70°C, for example carried out at an initial temperature of up to 50°C and preferably of up to 35°C.
3. Process according to claim 1 or 2 carried out at an initial temperature lying in the range of +10° to 35°C, preferably in the range of 15° to 25°C.
4. Process according to any one of the preceding claims wherein the initial temperature is maintained for a predetermined length of time, for example up to 2 hours, preferably up to 1 hour, most preferably up to half an hour.
5. Process according to any one of the preceding claims wherein the temperature is increased subsequent to the initial temperature maintenance period to follow a temperature profile to a final polymerization temperature, preferably up to a final polymerization temperature of at the most 90°C, and wherein the final polymerization temperature preferably lies in the range of 50-80°C and most preferably is 70°C or less.
6. Process according to claim 5 wherein the initial temperature is increased incrementally per pre-selected time period, preferably by about 20°C
per hour.
per hour.
7. Process according to claim 6 wherein the initiator is selected from the group consisting essentially of: diisobutanoyl peroxide, cumyl peroxyneodecanoate, 2,4,4-trimethylpentyl-2-peroxyneodecanoate, tert-amyl peroxyneodecanoate, bis(4-tert-butylcyclohexyl)peroxydicarbonate, bis(-ethylhexyl)peroxydicarbonate, tert-butyl peroxyneodecanoate, dibutyl peroxydicarbonate, dicetyl peroxydicarbonate, dimyristyl peroxy-dicarbonate, tert-amyl peroxypivalate, tert-butyl peroxypivalate, bis(3,5,5-trimethylhexanoyl) peroxide, dilauroyl peroxide, didecanoyl peroxide, 2,5"-bis(2-ethylhexanoylperoxy)-2,5-dimethylhexane, tert-amyl peroxy-2-ethylhexanoate, dibenzoyl peroxide, tert-butyl peroxy-2-ethylhexanoate, tert-butyl peroxydiethylacetate, 1,4-bis(tert-butylperoxycarbo)cyclohexane, tert-butyl peroxyisobutanoate, 1,1-bis(tert-butylperoxy)-3,3,5-trimethylcyclohexane, 1,1-bis(tert-butylperoxy)cyclohexane, tert-butyl peroxy-3,5-trimethylhexanoate, 2,2-bis(tert-butylperoxy)butane, tert-butylperoxy isopropyl carbonate, tert-butylperoxy 2-ethylhexyl carbonate, tert-butyl peroxyacetate, tert-butyl peroxybenzoate, di-tert-amyl peroxide, dicumyl peroxide, bis(tert-butylperoxyisopropyl)benzene, 2,5-bis(tert-butylperoxy)-2,5-dimethylhexane, tert-butyl cumyl peroxide, 2,5-bis(tert-butylperoxy)-2,5-dimethyl-3-hexyne, and di-tert-butyl peroxide.
8. Process according to claim 7 wherein the initiator is substantially non water-soluble and is selected from the group consisting essentially of:
- alifatic and aramatic peroxyesters, preferably tert-butyl peroxy-2-ethylhexanoate (Trigonox 21), tert-amyl peroxy-2-ethylhexanoate, tert-butyl peroxybenzoate (Trigonox C), tert-amyl peroxybenzoate, tert-butyl peroxyacetate, tert-butyl peroxy-3,5-trimethylhexanoate, tert-butyl peroxyisobutanoate, tert-butyl peroxydiethylacetate, tert-butyl peroxypivalate;
- peroxycarbonates, preferably tert-butyl peroxyisopropyl carbonate (Trigonox BPIC), and tert-butyl peroxy-2-ethyl hexyl carbonate Trigonox 117).
- alifatic and aramatic peroxyesters, preferably tert-butyl peroxy-2-ethylhexanoate (Trigonox 21), tert-amyl peroxy-2-ethylhexanoate, tert-butyl peroxybenzoate (Trigonox C), tert-amyl peroxybenzoate, tert-butyl peroxyacetate, tert-butyl peroxy-3,5-trimethylhexanoate, tert-butyl peroxyisobutanoate, tert-butyl peroxydiethylacetate, tert-butyl peroxypivalate;
- peroxycarbonates, preferably tert-butyl peroxyisopropyl carbonate (Trigonox BPIC), and tert-butyl peroxy-2-ethyl hexyl carbonate Trigonox 117).
9. Process according to any one of the preceding claims wherein the reductor is chosen from the group consisting essentially of: sodium formaldehyde sulfoxylate (SFS), sodium bisulfate, Ascorbic acid (vitamin C), aldehydes, for example glutaraldehyde, sodium metabisulfite, sodium dithionate, and sugars.
10. Process according to any one of the preceding claims wherein the polymerizable species is selected from the group consisting essentially of:
acrylonitrile, acrylic acid, methyl acrylate, ethyl acrylate, butyl acrylate, ethylhexyl acrylate, methoxyethyl acrylate, dimethyl aminoacrylate, methacrylic acid, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, 2-ethylhexyl methacrylate, lauryl methacrylate, stearic methacrylate, dimethyl aminomethacrylate, allyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxypropyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl methacrylate, acrylamide, methacrylamide, glycidyl acrylate, vinyl ester of versatic acid, styrene, para-methyl styrene, vinyl acetate, alpha-methyl styrene.
acrylonitrile, acrylic acid, methyl acrylate, ethyl acrylate, butyl acrylate, ethylhexyl acrylate, methoxyethyl acrylate, dimethyl aminoacrylate, methacrylic acid, methyl methacrylate, ethyl methacrylate, butyl methacrylate, isobutyl methacrylate, 2-ethylhexyl methacrylate, lauryl methacrylate, stearic methacrylate, dimethyl aminomethacrylate, allyl methacrylate, 2-hydroxyethyl acrylate, 2-hydroxypropyl acrylate, 2-hydroxyethyl methacrylate, 2-hydroxypropyl methacrylate, acrylamide, methacrylamide, glycidyl acrylate, vinyl ester of versatic acid, styrene, para-methyl styrene, vinyl acetate, alpha-methyl styrene.
11. Process according to any one of the preceding claims carried out in the presence of a catalyst, said catalyst preferably being a water soluble salt derived from a transition metal, and most preferably being selected from the group consisting essentially of Fe2+, Co3+, Cu+, and Ce3+.
12. Process according to any one of the preceding claims wherein the initiator and the reductor are provided in the following ratios 10:1 to 1:5, preferably 4:1 to 1:2.
13. Process according to any one of the preceding claims wherein the ratio of catalyst: oxidator is about 0-0.1 on a molar basis.
14. A polymer obtainable according to the process of any one of the preceding claims.
15. Polymer according to claim 14 having one or more of the following characteristics:
- a conductivity lower than about 5, - a low residual monomer level, - a particle size of less than about 220 nm, preferably less than 200 nm.
- a conductivity lower than about 5, - a low residual monomer level, - a particle size of less than about 220 nm, preferably less than 200 nm.
16. Use of a polymer according to claims 14 and/or 15 in coatings and/or adhesives.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP98203407.6 | 1998-10-12 | ||
EP98203407 | 1998-10-12 | ||
PCT/EP1999/007769 WO2000022003A1 (en) | 1998-10-12 | 1999-10-11 | Redox polymerization process |
Publications (1)
Publication Number | Publication Date |
---|---|
CA2346993A1 true CA2346993A1 (en) | 2000-04-20 |
Family
ID=8234202
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CA002346993A Abandoned CA2346993A1 (en) | 1998-10-12 | 1999-10-11 | Redox polymerization process |
Country Status (11)
Country | Link |
---|---|
EP (1) | EP1129113A1 (en) |
JP (1) | JP2002527540A (en) |
KR (1) | KR20010083906A (en) |
CN (1) | CN1326470A (en) |
AU (1) | AU6472199A (en) |
CA (1) | CA2346993A1 (en) |
NO (1) | NO20011865L (en) |
PL (1) | PL347253A1 (en) |
TR (1) | TR200101810T2 (en) |
WO (1) | WO2000022003A1 (en) |
ZA (1) | ZA200103009B (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8993667B2 (en) | 2013-03-15 | 2015-03-31 | Rohm And Haas Company | Redox polymers for improved dirt and water resistance for elastomeric wall and roof coatings |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10241481B4 (en) | 2002-09-07 | 2006-07-06 | Celanese Emulsions Gmbh | A process for preparing aqueous polymer dispersions having very low residual monomer contents and their use |
DE10335958A1 (en) | 2003-08-04 | 2005-02-24 | Basf Ag | Aqueous polymer dispersion, useful as a binding agent in adhesives, is prepared by radical aqueous emulsion polymerization of at least one ethylenically unsaturated monomer at two temperatures |
CN103443130B (en) * | 2006-07-18 | 2016-01-20 | 赛拉尼斯国际公司 | Emulsion polymerisation process |
JP5517459B2 (en) * | 2009-01-15 | 2014-06-11 | 日東電工株式会社 | Method for producing pressure-sensitive adhesive composition |
CN106661136A (en) * | 2014-04-09 | 2017-05-10 | 塞拉尼斯销售德国有限公司 | Process for the emulsion polymerization of free-radically polymerizable, ethylenically unsaturated monomers |
CN109653848B (en) * | 2018-12-27 | 2020-09-22 | 天津大学 | Method for adsorbing nitrogen oxides and/or hydrocarbon compounds during cold start of motor vehicle |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3022281A (en) * | 1958-11-24 | 1962-02-20 | Goodyear Tire & Rubber | Polymerization process with a peroxydicarbonate initiator formed in situ |
GB1558835A (en) * | 1976-01-01 | 1980-01-09 | Japan Synthetic Rubber Co Ltd | Process for preparing polymers having high molecular weight |
-
1999
- 1999-10-11 AU AU64721/99A patent/AU6472199A/en not_active Abandoned
- 1999-10-11 KR KR1020017004597A patent/KR20010083906A/en not_active Application Discontinuation
- 1999-10-11 CA CA002346993A patent/CA2346993A1/en not_active Abandoned
- 1999-10-11 WO PCT/EP1999/007769 patent/WO2000022003A1/en not_active Application Discontinuation
- 1999-10-11 PL PL99347253A patent/PL347253A1/en not_active Application Discontinuation
- 1999-10-11 TR TR2001/01810T patent/TR200101810T2/en unknown
- 1999-10-11 EP EP99952574A patent/EP1129113A1/en not_active Withdrawn
- 1999-10-11 CN CN99813273A patent/CN1326470A/en active Pending
- 1999-10-11 JP JP2000575905A patent/JP2002527540A/en active Pending
-
2001
- 2001-04-11 NO NO20011865A patent/NO20011865L/en not_active Application Discontinuation
- 2001-04-11 ZA ZA200103009A patent/ZA200103009B/en unknown
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8993667B2 (en) | 2013-03-15 | 2015-03-31 | Rohm And Haas Company | Redox polymers for improved dirt and water resistance for elastomeric wall and roof coatings |
Also Published As
Publication number | Publication date |
---|---|
ZA200103009B (en) | 2002-07-11 |
WO2000022003A1 (en) | 2000-04-20 |
KR20010083906A (en) | 2001-09-03 |
PL347253A1 (en) | 2002-03-25 |
CN1326470A (en) | 2001-12-12 |
AU6472199A (en) | 2000-05-01 |
EP1129113A1 (en) | 2001-09-05 |
JP2002527540A (en) | 2002-08-27 |
TR200101810T2 (en) | 2001-11-21 |
NO20011865L (en) | 2001-06-11 |
NO20011865D0 (en) | 2001-04-11 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6306982B1 (en) | Process for the production of general purpose PSA's | |
US5399621A (en) | Process for the preparation of a graft copolymer latex of core/shell dispersion particles having improved phase binding between core and shell | |
US20090306302A1 (en) | Process of free-radical polymerization in aqueous disperasion for the preparation of polymers | |
CA2346993A1 (en) | Redox polymerization process | |
US5374686A (en) | Process for segmented copolymers | |
WO2006039860A1 (en) | A preparation method of small particle sized polybutadiene latex used for the production of abs | |
KR100569219B1 (en) | Method of reducing the content of residual monomers in emulsion polymers | |
JP3149487B2 (en) | Method for producing methacrylic resin particles | |
JP3212471B2 (en) | Vinyl chloride resin | |
JPS60158210A (en) | High stability aqueous dispersion and manufacture | |
CA1318433C (en) | Pressure sensitive adhesive compositions | |
US4342676A (en) | Method for producing latices of copolymers of butyl acrylate and 1-methacrylate-1-tert-butyl peroxy ethane | |
EP0729493A1 (en) | Aqueous dispersion of vinyl polymers | |
JPH072954A (en) | Production of graft copolymer | |
CA2094354A1 (en) | Segmented copolymers | |
JPH0627200B2 (en) | Methacrylic resin molding material | |
JP3262700B2 (en) | Vinyl chloride resin | |
JP2803277B2 (en) | Method for producing styrenic resin | |
US4833223A (en) | High molecular weight polystyrene and method | |
CN117210173A (en) | Water-based pressure-sensitive adhesive and preparation method and application thereof | |
KR100431453B1 (en) | Method for preparing polyvinyl resin having superior high impact property | |
WO2022112190A1 (en) | Process of producing polymer dispersions | |
JPH1060059A (en) | Production of vinyl chloride-based graft copolymer | |
JP2000198900A (en) | Vinyl chloride-based graft copolymer | |
JPH1087762A (en) | Vinyl chloride-based graft copolymer and its production |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
FZDE | Dead |