The present invention relates to a process wherein one or more initiators are used to polymerize a mixture containing one or more monomers of which one is vinyl chloride monomer (VCM).
As is known to a person skilled in the art, such a process can be performed in many different ways. It is generally desired to shorten the total polymerization time. This can be achieved by shortening the period of constant pressure in the polymerization reactor, or by reducing the time required to complete the polymerization reaction after the pressure in the reactor starts to drop. An example of a process where the time of pressure drop is reduced is US 5,908,905
, wherein a process is described which is completed at a higher temperature than a preset temperature for the polymerization. However, such a temperature increase may result in discolouration of the polymer. Above all, it has the disadvantage of influencing the molecular weight of the polymers formed.
 US 5,739,222
describes another process, wherein when the internal pressure of the reactor declines, further monomer is fed to the reactor. This procedure will significantly affect the physical properties of the polymer particles.
 US 4,015,065
describes a process wherein a polymerization initiator is added at the pressure drop to the polymer formed, while subjecting the polymer to radio frequency dielectric heating. With this process, the aim is to remove or partially remove the abundantly present vinyl halide monomer from the vinyl halide polymer. The use of radio frequency dielectric heating is less desired, since it is energy intensive and affects the properties, such as thermal stability and colour, of the polymer produced.
It is an object of the present invention to provide an improved process which overcomes the disadvantages of the prior art processes. More specifically, it is intended to provide a process wherein the overall polymerization time is reduced by a reduction of the pressure drop time.
The process of the present invention is a process as described in claim 1.
During VCM polymerizations, the pressure initially is proportional to the temperature of the reaction mixture. This is because the pressure in the polymerization reactor is predominantly determined by the vapour pressure of the VCM in the polymerization mixture. Towards the end of the polymerization reaction, the VCM is depleted. At a certain moment no liquid VCM phase is present any longer and the pressure in the reactor starts to drop below the pressure otherwise observed at that temperature. After and/or during the pressure drop there still is VCM present in the gas phase, but typically more and _ more is being adsorbed in the water and polymer phase of the reaction mixture. At that time the polymerization rate conventionally decreases and the cooling capacity of the reactor is not optimally used.
The inventors have now identified these problems and found that the available cooling capacity of the reactor can be used more efficiently if the polymerization rate is enhanced by the addition of one or more initiators after the initial pressure drop and/or during the pressure drop. Preferably, the initiator is added at or after the moment at which the pressure drops in the reactor. It is less preferred to add said initiator before that moment, as it may lead to an undesirable runaway reaction, which is generally accompanied by an undesirable and dangerous increase in pressure. Apart from more efficient use of the cooling capacity, the total polymerization time is reduced due to a higher pressure drop rate, thereby shortening the period in which the pressure of the reactor is dropping. Also, the reactor space-time yield is improved.
The initiators can be any kind of organic peroxide suitable for use in the polymerization process, such as peroxydicarbonates and acetyl-cyclohexylsulfonyl-peroxide. Hence, the additional initiator can be the same as or different from the initiator(s) used in the polymerization before the pressure drop. The additional initiators are organic peroxides having a half-life of from 0.0001 to 1 hour at the polymerization temperature. Even more preferred are peroxides having a half-life ranging from 0.0001 to 0.5 hour at the polymerization temperature. Most preferred are extremely fast peroxides having a half-life of from 0.0001 to 0.05 hour at the polymerization temperature.
Preferred examples of organic peroxides used in the process of the invention are 1,1,3,3-tetramethylbutylperoxy methoxy acetate, tert.-butylperoxy methoxy acetate, tert.-amylperoxy methoxy acetate, tert.-butylperoxy ethoxy acetate, diisobutanoyl peroxide (Trigonox® 187), hexanoyl pivaloyl peroxide, 2-ethyl-butanoyl-isononanoyl peroxide, isobutanoyl-lauroyl peroxide, isobutanoyl-isononanoyl peroxide, bis(tert-butylperoxy) oxalate, cyclododecyl-tert. butylperoxy oxalate, 2,2-bis-2-ethylhexanoylperoxy-4-methylpentane, 2,2-bis-2-ethylbutanoylperoxy-4-methylpentane,2,2-bis(2,2-dimethyl-propanoylperoxy)-4-methylpentane,1-(2-ethylhexanoylperoxy)-1,3-dimethylbutyl-1-peroxypivalate (Trigonox® 267) or 2,4,4-trimethylpentyl-2-peroxyneodecanoate (Trigonox® 423), tert-amyl peroxyneodecanoate (Trigonox® 123), tert-butyl peroxyneodecanoate (Trigonox® 23), benzene (m,p)di(2-isopropyl-2-peroxyneodecanoate), 2-methyl-4-hydrox-ypentane-2-peroxyneodecanoate, α-cumyl peroxyneodecanoate (Trigonox® 99), and peroxydicarbonates such as di-sec-butylperoxydicarbonate (Trigonox® SBP), di(4-tert-butylcyclohexyl) peroxydicarbonate (Perkadox® 16) and di(2-ethylhexyl) peroxydicarbonate (Trigonox® EHP).
Other organic peroxides having a half-life ranging from 0.0001 to 1 hour at the polymerization temperature can also be used. Whether a peroxide is suitable and has the required half-life can be determined by conventional thermal decomposition studies in monochlorobenzene, as is well-known in the art (see for instance the brochure "Initiators for high polymers" with code 10013921001 available from Akzo Nobel).
The initiator according to the invention can be a redox initiation system. In such a case the reducing agent, the oxidizing agent, or both can be dosed in accordance with the invention. For such redox systems, the half-life of the redox system is the half-life as measured when all components of the system are present. However, in view of the fact that redox systems typically contain heavy metals and/or undesired reducing agents, the initiators of the present invention preferably are not such redox initiation systems.
The amount of initiator (or initiators) to be used in a process according to the invention after the start of the pressure drop and/or during the pressure drop is within the range conventionally used in polymerization processes. Typically, this range has a lower limit of 0.001 % by weight (% w/w) of additional initiator and more preferably of 0.005% w/w, and an upper limit of 0.3% w/w of additional initiator, preferably of 0.2% w/w; most preferably, 0.05% w/w, based on the weight of VCM monomer, is used.
The additional initiator is added to the reactor in the pure form or, preferably, in the form of a dilute solution or dispersion (such as a suspension or emulsion). One or more suitable solvents can be used to dilute the initiator. Preferably, such solvents are easily removed during the steps where the polymer is worked up after the polymerization process, such as alcohols, or they are of such a nature that it is acceptable to leave them as a residue in the final polymer, as in the case of solvents that are desired plasticizers for the final resin. Furthermore, it can be advantageous, but is not necessarily required, that such solvents do not adversely affect the thermal stability of the initiator dissolved therein, as can be verified by analyzing the half-life temperature of the initiator in said solvent. An example of such a solvent is isododecane. If an initiator dispersion is added, then the dispersion can be of either the initiator itself or of a solution of the initiator, preferably in said suitable solvents. Preferably, the dispersion is an aqueous dispersion. Preferably, the initiator is added in a concentration of at least 0.1% w/w, more preferably 0.5% w/w, and most preferably 2% w/w, and at most 75% w/w, more preferably at most 60% w/w, even more preferably at most 50% w/w, more preferably still 25% w/w, and most preferably 15% w/w. The more dilute initiator solutions or dispersions ensure rapid mixing of the initiator and the polymerization mixture, which leads to a more efficient use of the initiator, which is important for the fast initiators that are used.
The addition after the start of the pressure drop and/or during the pressure drop is the addition of fast initiators having a half-life of 0.0001-1 hour at the polymerization temperature, as a relatively small residual amount of the initiator will remain in the polymer formed. In order to reduce the residual amount even more, it is preferred to add extremely fast peroxides having a half-life of less than 0.05 hour at the polymerization temperature. However, a slower initiator can also be employed. In that case it can be preferred to add a scavenger which is able to neutralize or destroy the residual initiator in any subsequent step to such an extent that the residual amount of the initiator in the polymer is acceptable. It is also contemplated to add a scavenger when fast and/or extremely fast peroxides are used.
During the first part of the polymerization reaction any conventional initiating system can be used. Herein, the initiator can be added intermittently or continuously to the polymerization mixture at the polymerization temperature. All of the initiator can be added to the reactor at once in just one portion. In such case, preferably a relatively slow initiator having a half-life of more than 1 hour is used. The initiator may also be added at at least 2, preferably at least 4, more preferably at least 10, and most preferably at least 20 moments.
Typically, one or more protective colloids are used in the polymerization process of the invention. Examples of suitable protective colloids are protective colloids such as polyvinyl alcohols (PVAs), which may, for example, be (partially) saponified polyvinyl acetates with a degree of hydrolysis of at least 40%, more preferably at least 60%, and most preferably at least 62%, and a degree of hydrolysis of at most 90%, more preferably at most 85%, and most preferably at most 80%. If for example two PVAs are employed, both PVAs may have a similar degree of hydrolysis. It may also be envisaged that the two PVAs have a different degree of hydrolysis. Although said PVAs are the preferred protective colloids for processes according to the invention, it is also possible to use other conventional protective colloids, such as cellulosics, water-soluble polymers, oil-soluble emulsifying agents or water-soluble emulsifying agents. It is also envisaged to employ a combination of two or more of the above protective colloids. The amount and type of colloid that is to be used is well-known and conventional. Optionally, such colloids are also added after the start of the pressure drop and/or during the pressure drop. If used after the start of the pressure drop and/or during the pressure drop, they can be added together with or separately from the initiator which is added in accordance with the invention.
However, in a preferred embodiment, one or more surfactants are added after the start of the pressure drop and/or during the pressure drop. If used in such a fashion, they can be added together with or separately from the initiator which is added in accordance with the invention. The addition of such surfactants was found to be very helpful, since it reduces the (excessive) formation of foam in the process. Examples of suitable surfactants are polyvinyl acetates with a degree of hydrolysis of less than 60% and conventional foam reducers (defoamers), as generally known to a person skilled in the art. Preferably, the surfactant is added together with the additional initiator.
Preferably, the addition of the initiator, of the optional colloid and the optional surfactant, either during the constant pressure time or after and/or during the pressure drop, can be effected at any suitable entry point to the reactor. Such an entry point may be positioned below or above the surface of the reaction mixture, as desired. The addition of these compounds can be separately to the reactor via individual entry points, or they can be pre-mixed and enter the reactor through one entry port, or a combination of such techniques can be used. If water is added in the course of the polymerization process, for example to compensate for the shrinkage of the reactor content due to the polymerization reaction, it can be advantageous to use the line through which this water is added to also add the initiator and/or the optional protective colloid and/or surfactant. It is also envisaged that the reactor comprises dedicated piping and a plurality of entry points located in different positions on the periphery of the said reactor, so as to ensure better, faster, and more homogeneous mixing of the initiator, protective colloid, and/or surfactant in the reaction mixture. If the reactor further comprises a reflux condensor, it is contemplated to add these compounds to the reaction mixture via the reflux condensor.
The process according to the invention is directed to polymerizing monomer mixtures comprising vinyl chloride monomer (VCM). Preferably, the process according to the invention involves the polymerization of monomer mixtures comprising at least 5% w/w of VCM, preferably at least 10 %w/w, more preferably at least 20 %w/w, and most preferably at least 50 %w/w of VCM, based on the weight of all monomer. Comonomers that can be used are of the conventional type and include vinylidene chloride, vinyl acetate, ethylene, propylene, acrylonitrile, styrene, and (meth)acrylates. More preferably, at least 80% w/w of the monomer(s) being polymerized is made up of VCM, while in the most preferred process the monomer consists essentially of VCM. As is known in the art, the polymerization temperature of such processes to a large extent determines the molecular weight of the resulting resin.
The polymerization process can be conducted as a mass process wherein the reaction mixture is predominantly monomer, or as a more preferred suspension process wherein the reaction mixture typically is a suspension of monomer in water, or as an emulsion or micro-emulsion process wherein the monomer typically is emulsified in water. In these processes the usual additives will have to be used. For example, if the monomer is present in the form of a suspension in .. water, the usual additives like surfactant(s), anti-fouling agent(s), and pH-buffer(s), can be present. Depending on the type of polymer desired, each of the above-mentioned processes may be preferred. The process according to the invention is especially suited for use in suspension processes.
After the polymerization, the resulting (co)polymer (or resin) will be worked up as is usual in the art. Polymers obtained by a suspension polymerization according to the invention, for example, will be submitted to the usual drying and screening steps. It is preferred that the resulting resin contains less than 50 ppm of residual initiator, more preferably less than 40 ppm, and most preferably less than 25 ppm of initiator, immediately after drying for 1 hour at 60°C and screening, since such resins exhibit excellent heat stability as measured with a Metrastat® PSD260 testing oven in accordance with ISO 182-2 (1990E). The improved heat stability proved that the resin hardly discoloured when submitted to melt-processing steps, e.g., to form shaped articles. Hence the process can comprise an additional process step in which excess initiator is decomposed. Preferably, said process step is taken after the polymerization reaction has finished and before the resin has dried.
Examples to demonstrate the unexpected effect of the addition of fast peroxides during the pressure drop in PVC suspension polymerization:
In a standard suspension polymerization experiment, a temperature controlled 1-litre stainless steel Büchi reactor provided with one baffle, a three-bladed stirrer, a pressure transducer, a VCM feed line, and a nitrogen purge line was charged with 425 g demineralized water, Alcotex B72 (1000 ppm on VCM) in a 5% w/w solution in demineralized water, and was pressurized to 15 barg, using nitrogen. If no leaks are observed, the reactor is evacuated and pressurized with nitrogen up to 5 barg three times to flush out virtually all air. Next, the reactor was evacuated and charged with 250 g VCM ex Akzo Nobel Salt & Basics, followed by heating up of the reactor to the polymerization temperature in 30-60 min.
The conventional peroxide, such as Trigonox® EHP (Tx EHP), used to initiate the polymerization is added via a hot-start procedure. The hot-start procedure means that the peroxide is added to the reactor at the polymerization temperature in a very short period, i.e. 1-5 min.
During the pressure drop period of the polymerization a fast initiator with a half-life at the polymerization temperature of less than 0.1 hr. is added o the reactor until the pressure in the reactor has dropped 3.5 bar. For adding of the (additional) fast initiator, a relatively low-concentration (about 1% w/w) emulsion is used. In the comparative example the addition of the (additional) fast initiator was omitted.
After reaching the said pressure drop of 3.5 bar the peroxide dosing was stopped and then the reactor was cooled to 20-25°C, evacuated, and freed of virtually all remaining VCM. The polymer was obtained after filtration, washing, and drying (at 60°C for 1 hour using a fluidized bed).
The initiators used (Tx EHP (75% w/w) dissolved in isododecane (25% w/w) and Tx 187 [0.3% w/w aqueous emulsion]), the amount dosed, the dosing procedure, and the polymerization results are presented in Table 1.
After reaching the polymerization temperature the mentioned amount of Tx EHP (calculated on VCM) in isod-odecane is added in a period of 1-5 minutes.
Table 1: The results of VCM suspension polymerization with di(2-ethylhexyl) peroxydicarbonate (Tx EHP) at 57°C without (Comparison example) and with (Example 1) adding of diisobutanoyl peroxide (Tx 187) during the pressure drop
| ||Example 1||Comparison example|
|Hot-start peroxide and quantity
||800 ppm Tx EHP
||800 ppm Tx EHP|
|Adding peroxide during pressure drop
||80 ppm Tx 187 during 30 minutes
|Constant pressure time
|Pressure drop rate
|Polymerization time until the reactor pressure has dropped 3.5 barg
From Table 1 it is deduced that the process of Example 1 clearly has a significantly higher pressure drop rate compared to the conventional process of the comparison example. This higher drop rate leads to a shorter polymerization time. The higher pressure drop rate clearly makes for better usage of the cooling capacity of the reactor.
1. Verfahren, bei dem ein oder mehrere Initiatoren verwendet werden, um ein Gemisch, das ein oder mehrere Monomere enthalt, von denen eines ein Vinylchlorid-Monomer ist, zu polymerisieren, wobei wenigstens ein Teil der Initiatoren bei der Reaktionstemperatur zu dem Polymerisationsgemisch gegeben wird, wenn der Druck im Polymerisationsreaktor aufgrund des Verbrauchs des Vinylchlorid-Monomers abfällt, und wobei der Initiator, der hinzugefügt wird, wenn der Druck im Polymerisationsreaktor abfällt, ein organisches Peroxid ist, das bei der Polymerisationstemperatur eine Halbwertszeit von 0,0001 Stunden bis 1 Stunde hat, mit der Maßgabe, dass das gebildete Polymer keiner dielektrischen Erwärmung mit Radiowellen in Gegenwart von zusätzlichem organischen Initiator ausgesetzt wird, und mit der weiteren Maßgabe, dass ein Verfahren ausgeschlossen ist, bei dem Vinylchlorid-Monomer polymerisiert wird in Suspension bei 57°C in Anwesenheit von 1.000 ppm Polyvinylalkohol, entweder indem 330 ppm Diisobutanoylperoxid über 12 Minuten und anschließend 670 ppm Diisobutanoylperoxid über 220 oder 245 Minuten hinzudosiert werden oder indem 480 ppm 1-(2-Ethylhexanoylperoxy)-1,3-dimethylbutyl-1-peroxypivalat über 15 Minuten und anschließend 1.120 ppm 1-(2-Ethylhexanoylperoxy)1,3-dimethylbutyl-1-peroxypivalat über 120 Minuten hinzudosiert werden, wobei alle Mengen auf Vinylchlorid-Monomer basieren und alle Peroxide als 0,8 Gew.-% Methanollösung hinzugegeben werden.
2. Verfahren gemäß Anspruch 1, wobei das organische Peroxid bei der Polymerisationstemperatur eine Halbwertszeit von 0,0001 Stunden bis 0,05 Stunden hat.
3. Verfahren gemäß einem der Ansprüche 1 bis 2, wobei dann, wenn der Druck im Polymerisationsreaktor aufgrund des Verbrauchs des Vinylchlorid-Monomers abfällt, auch ein Tensid hinzugefügt wird, um die Bildung von Schaum zu reduzieren.