METHOD OF MANUFACTURING OLEFIN RESIN PARTICLES AND PRE-EXPANDED PARTICLES

Abstract: A method for producing polyolefin resins granules are disclosed, which comprises extruding by using a homodirectional(co-rotating) twin-screw kneading extruder a polyolefin resin from a die nozzle having a diameter of less than 2mm and a discharge amount per hole of 0.5-8 Kg/hr into warm water of 5-90°C which is lower than a temperature of the resin by 140-220°C, and cutting the extrudate with a cutter blade in the warm water. According to this invention, uniformly dispersed compounds are obtained, and switching of a raw resin can be done speedily and economically, and further, resin granules of a desired shape can be produced.

Description: This invention relates to a method for the production of resin granules and pre-foamed beads for obtaining foamed articles in a mold from polyolefin resins, which are used in buffer packaging materials, goods-delivery boxes, heat insulating materials, core materials for car bumpers and the like. When producing pre-foamed beads of polyolefin resins which are used for obtaining foamed articles in a mold from polyolefin resins , resin granules are pre-foamed without kneading and melting again, and therefore, the shape of the resin granule has a large influence on that of pre-formed beads. It happens sometimes that a large deformation occurs at the time of foaming. For this reason, resin granules are needed which have a small uniform shape , a constant or preferably small residual strain and which can become spherical after pre-foaming. Thus, raw resins are beforehand molded into small granules of a proper shape. As this molding method for resin granules, there are a strand cut method, under water cut method and the like. In the case of the strand cut method, the residual strain is large at the time of foaming resin granules, and their shape is largely deformed due to a big shrinkage in a direction of resin granule extrusion when pre-foamed beads are produced. Therefore, in order to obtain pre-foamed beads which have a small change in shape and a desired shape, the most proper conditions must be fulfilled exactly which are determined by seizing a relation between producing conditions or properties of raw resins and a ratio of shape change . However , it is practically difficult to fulfill these producing conditions stably and exactly and the yield is forced to be low. Moreover, there are some problems that a lot of work is needed even to a small change in raw materials, that a long space is necessary to set an equipment, and that productivity is comparatively low due to a limit for increasing strand numbers, and the like. Document JP-A-01135620 relates to a method for producing strand-shaped cushioning material having very fine surface shape wherein rotary cutting blades, which have specified conditions, are installed at the discharge part of a die for hot cutting. As the under water cut method, there are methods described, for example, in Unexamined Japanese Patent (JPA 61-195808) or Unexamined Japanese Patent (JPA 1-234212). The former discloses a method of producing spherical granules of a thermoplastic resin which is characterized in that the resin temperature is adjusted so that the viscosity of the fused resin at the die entrance becomes between 1 × 10 2 and 5 × 10 4 poise and ,further, the amount of discharge is adjusted to between 0.1 and 6.0 kg/hr when the fused resin is extruded into cooling water from a nozzle of the die which is attached at the tip of the molding machine and is granulated by being cut with a rotating cutter blade which is contacted with the die surface . These methods are not necessarily sufficient because pre-foamed beads can not be obtained yet stably as large voids in the pre-foamed beads appear or the shape of the pre-foamed beads becomes non-spherical, though there is no large shrinkage in the direction of extrusion at the time of producing pre-foamed beads as can be seen in a strand cut method. Thus, even though resin granules of a desired shape can be obtained at a glance, it happens sometimes that they cannot be used since large voids appear or their shape deforms largely when they were pre-foamed. In this case, losses of resin and time and labor for producing them become quite large since the fact that the resin granules are improper becomes clear long time after evaluating operations including a foaming operation which takes a long time succeeding to production of the resin granules. Further, since this tendency becomes remarkable as the discharge amount per one hole of the die nozzle increases, the application of this method to practical production scale is not necessarily satisfactory. Pre-foamed beads are mixed if necessary, with compounding ingredients such as nucleating agents, anti-fusing agents , anti-static agents, pigments and the like. However, since the dispersion of these compounding ingredients is not necessarily sufficient due to small quantity of these compounding ingredients, properties of the obtained mixtures such as an uniformity in cell size and coloring, which is one of important factors for determining properties of a foamed article, are not always sufficient. Thus , a method is waited which can make a rapid progress in dispersibility of above-mentioned ingredients in the mixtures by a simple way. Further, a single -screw extrusion is usually used. Recently, even in the case of a foamed article of polyolefin resins, a successive production of a variety of foamed articles, which are composed of plural resins or mixtures, is not unusual. Usually, these foamed articles are produced using the same equipment from a viewpoint of economical efficiency. However, when the single -screw extrusion is used, it is a weak point that productivity is quite low, since a good deal of time and labor are needed for switching of raw resins and a loss of raw materials is also large. An object of this invention is to provide a producing method which makes it possible that the dispersion of compounding agents becomes uniform, that a switching of raw materials can be done smoothly and economically and further, that resin granules or pre-foamed beads of a desired shape can be produced by solving problems in the prior art as mentioned above. The inventors have made a series of studies and finally have found a method which can solve the above-mentioned problems and have completed this invention by using a homodirectional(co-rotating) twin-screw kneading extruder as an extruder, extruding a resin by an under water cut method and adjusting the temperature of warm water in a proper range taking into consideration it's relation with the resin temperature etc., under conditions of a proper amount of discharge per one nozzle hole and a diameter of die nozzle which are determined by a desired shape of resin granules and an amount of production . This invention provides, in a first aspect, a method for producing polyolefin resin granules which comprises the steps of: extruding by using a kneading extruder a polyolefin resin from a die nozzle into water, and cutting the extrudate with a cutter blade in the water, characterized in that: the kneading extruder is a homodirectional twin-screw kneading extruder, the die nozzle has a die nozzle hole having a diameter of less than 2 mm and a discharge amount per die nozzle hole of 2 - 8 Kg/hr, the water is warm and has a temperature of 5 - 90 °C which is lower than the temperature of the resin by 140 - 220 °C, and the peripheral speed of the cutter blade is 13 - 27 m/sec, and, in a second aspect, a method for producing polyolefin pre-foamed beads which comprises re-foaming the resin granules obtained by the above method. By using a homodirectional(co-rotating) twin-screw kneading extruder as an extruder, the both pending problems of dispersion and economy at the time of switching of a raw resin can be solved simultaneously. A small quantity of compounding agents is added to resin granules of the polyolefin resin, if necessary. For example, approximately 0.01 % by weight(100ppm) of talc is added usually as a nucleating agent to an ethylene-propylene random copolymer and this amount is adjusted properly according to the state of cells. In the prior art case where a single-screw extruder is used for granulating, it is difficult to obtain uniform cells since the amount of the nucleating agent is too small to get a good dispersion. Thus, even though a master batch method or a method of extruding resin granules twice is taken, sufficient uniformity of cells cannot be fulfilled. According to this invention, the uniformity of cells can be remarkably improved by taking use of the homodirectional twin-screw kneading extruder. Because of an improvement in dispersion of the other compounding agents, not only have properties of foamed articles in a mold been improved, but also economical effects such as omitting a blending step are obtained. When resin granules of different resins or compounds are produced successively, it is generally impossible to conduct switching successively in a case of a single-screw extruder. That is, it is necessary to start again after an operation is stopped, a screw is detached and cleaned and a resin is switched. Not only this operation needs many operators, but also a shutdown time and an induction time to a stable operation become long. Further, loss of raw resin is large. On the other hand, since the homodirectional twin -screw kneading extruder has a self-cleaning effect, it is possible to conduct switching only by exchanging a resin to another resin in a continuous operation, and loss of raw resins becomes small because raw resins are only lost in a short period for finishing a extrusion of a mixed resin. In the case where pre-foamed beads of different polyolefin resins are produced alternatively or pre-foamed beads of polyolefin resins from different resin compounds are produced alternatively, this effect is necessary and essential. The amount of discharge per one nozzle hole is set by stability of extrusion, desired amount of production and the like. Though depending on viscosity of resin or shape of die, it becomes impossible to obtain resin granules of a desired shape due to unsteady fluidity of fused resin if the amount of discharge per one nozzle hole is over 8kg/hr. Further, though depending on the ability of an extruder, above 0.5kg/hr is appropriate, and above 2 kg/hr is preferable by taking account of the practical production scale and stability of an extruder. The diameter of the die nozzle hole is set by taking account of die swell in order to obtain resin granules of a desired shape. Generally speaking, a resin granule required for obtaining a pre-foamed bead of a desired size is controlled by weight per one granule and a preferable weight of a resin granule is less than 15mg/one granule, more preferably less than 5mg/one granule and the most preferable less than 2mg/ one granule. Thus, the diameter of the die nozzle hole is set at less than 2mm. Here, a diameter of die nozzle hole means the diameter at the tip of a land of die nozzle. The shape of a resin granule is not limited if a sphere-like shape suitable for use in molded articles can be obtained after being pre-foamed. However, even if resin granules are spherical, useless pre-foamed beads for use in molded articles may result due to a large deformation after being pre-foamed if the temperature of the warm water itself or the relation between the temperature of the warm water and that of the resin is improper. While, if these conditions are fulfilled, almost spherical and useful pre-foamed beads can be obtained after being foamed, even if the shape of resin granules is somewhat flat. The setting of the warm water temperature is most important to get resin granules of a desired shape. In the case of resin granules of a general purpose which are not supplied to foaming materials, the temperature of warm water is generally set between 20-50 °C. However, even though the resin is extruded at the same resin temperature and resin granules of a normal shape can be obtained in appearance, it happens sometimes that pre-foamed beads of large voids, are mixed into normal pre-foamed ones after being pre-foamed and, therefore, they are intolerable to a practical use. Further, since it becomes clear after pre-foaming that pre-foamed beads of a useless shape have been obtained though the shape of resin granules looks like a desired form, it takes a long time for evaluating and it often happens that a lot of resin granules are lost. This invention has solved this problem by keeping the temperature of warm water itself in a special range and further controlling it according to the resin temperature. That is, the problem mentioned above has been solved by keeping the temperature of warm water in the range between 5-90°C and 140-220°C lower than the resin temperature. If the temperature of warm water is over 90°C, it is not proper since resin granules are fused together. If the temperature of warm water is less than 5°C, it is not proper since clogging of the die nozzle tends to happen. Even if the temperature of warm water itself is in the above-mentioned range, it may happen sometimes that resin granules are fused together, when the temperature of warm water is lower than that of the resin by less than 140°C. This is due to insufficient cooling of the resin granules since the difference of the temperatures between warm water and resin is small. Moreover, it is not preferable that the temperature of warm water is lower than that of the resin by more than 220°C, since cavities occur in resin granules or large voids are generated in pre-foamed beads after pre-foaming even if the resin granules have a normal shape in appearance. The reason why such phenomenon occurs is not clear, but may be guessed as follows. That is, when a resin is extruded from a die nozzle, the tip and sides of the extrudate may be cooled abruptly and its length may be fixed if the temperature difference between warm water and resin is large. Next, the inside of the extrudate is cooled slowly and a volume shrinkage may happen due to crystallization. However, the tip and the sides whose surfaces are fixed do not deform. Thus, only a back edge where cooling has not proceeded yet deforms and is pulled into the inside resulting in a cavity. Such deformation may be further expanded by pre-foaming. Therefore, even if a cavity is too small to be detected in resin granules, this cavity may be grown large remarkably to a void after pre-foaming. It is also preferable that the peripheral speed of the cutter blade is set high. Besides the temperature of warm water being set in the above- mentioned range, the peripheral speed of the cutter blade is set preferably to not less than 13m/sec, more preferably to not less than 15m/sec. If the peripheral speed is below 13m/sec, it may happen that the shape of resin granules becomes undesirable and irregular. And further, if the peripheral speed is below 13m/sec, it may happen sometimes that the resin granules are fused together. Here, the peripheral speed of a cutter blade means the same at the tip of the die nozzle. Also, it may happen that resin granules deform undesirably into an irregular form. The reason why this happens is not clear, but it may be guessed that this is due to a residual strain when the extrudate is cut. As in the case of setting the temperature of warm water, a large amount of resin granules is lost due to a long evaluation time since it becomes clear that pre-foamed beads of an improper shape were obtained only after pre-foaming, but this problem is solved by setting the peripheral speed above 13m/sec. However, in the case where the peripheral speed is too large, many troubles such as breakage of the cutter blade occur, and thus, it is preferable that the peripheral speed is below 27m/sec. The polyolefin resin used in this invention includes, for example, low density polyethylene, middle density polyethylene, high density polyethylene, linear low density polyethylene, polypropylene, ethylene-propylene copolymers, propylene-butene copolymers, ethylene-butene-propylene terpolymers, ethylene- vinyl acetate copolymers and poly(butene-1), though not limited thereto. These are used individually or in combination of two or more. Further, it is needless to say that compounding ingredients such as anti-fusing agents, nucleating agents, anti-static agents, pigments and the like can be added properly, if necessary. This invention is quite suitable for mixing a very small amount of compounding ingredients or to produce pre-foamed beads which are composed of different polyolefin resins or different resin compounds using a single equipment for resin granules, since this invention employs a homodirectional twin-screw kneading extruder. Pre-foamed beads in this invention are obtained by foaming above-mentioned resin granules approximately 5-60 times using known methods described below. (1) a method of charging olefin resin granules, a volatile foaming agent and a dispersion agent, if necessary, into a pressure vessel, heating the mixture to the neighborhood of the melting temperature of said resin to thus pressurize with agitating, then releasing said resin granules and an aqueous solution into a low pressure region( atmospheric pressure ) by opening a valve set at the bottom of the pressure vessel. (2) a method of impregnating olefin resin granules with a volatile foaming agent, charging the obtained granules into a pressure vessel, introducing steam etc. from one end of the pressure vessel with agitation, together with a small amount of an anti-fusing agent added, if necessary, to thus foam said resin granules, then taking out the pre-foamed beads. The invention will be described in more detail with reference to the following examples, which are in no way intended to restrict the scope of the invention. Example 1 Resin granules were produced by extruding a fused compound ( which was composed of 100 parts by weight of an ethylene-propylene random copolymer, 0.01 part by weight of talc as a nucleating agent and the other compounding agents) from a die nozzle attached to a tip of an extruder ( number of nozzles : 96; nozzle diameter : 1.0mm) into 75°C warm water with a discharge amount of 3.6kg/hr per one nozzle hole, cutting the extrudate with a cutter blade( number of blades : 12) provided near the die at a peripheral speed of 19m/sec and separating the resin granules obtained from circulating warm water. The temperature of the resin was, in this case, 270°C according to a thermometer attached to this extruder. Further, die nozzles were arranged circumferentially where the distance between two nozzles facing each other over the center was 120mm, the rotating number of the cutter blade were 3000rpm and the discharged amount of resin was 350kg/hr. The shape of the obtained resin granules and the weight of one granule were evaluated and the results evaluated were shown in Table 1. Examples 2-8 and Comparative Examples 1~8 Resin granules were produced in the same way as in Example 1 except that the number of nozzles was chosen from 60-250, the rotating number of the cutter blade was chosen from 1500-4300rpm, the number of blades was chosen from 8-12 properly and that the diameter of the die nozzle, the discharge amount per one nozzle hole, the temperature of the warm water, the temperature of the resin and the peripheral speed of the cutter blade were changed as shown in Table 1. Here, the discharge amount of the resin was 100∼500kg/hr. The results were shown in Table 1. Example 9 After producing resin granules of a compound comprising a linear low density polyethylene (compound 1) in the same way as in Example 1, resin granules of a compound(compound 2) were produced by mixing the compound 1 with carbon black successively. It was confirmed that the compound 1 was exchanged with the compound 2 completely after 20 minutes, judging from the color of the resin granules. Comparative Example 9 Resin granules comprising the compound 1 used in Example 9 were produced by attaching an under water cut equipment to a 115mm ø single screw extruder. According to an usual method which was used when a raw material was exchanged in the single screw extruder, namely, first a screw was detached after an operation was stopped, and it was again attached to the extruder after being cleaned. Afterwards, resin granules comprising the compound 2 was produced. It took about 8 hours until a stable production was reached after stopping the production of the resin granules comprising the compound 1. Examples 10~17 and Comparative Examples 10~12 100 parts by weight of the resin granules obtained in Example 1-8, and Comparative Examples 1,7 and 8, 5-10 parts by weight of isobutane as a volatile foaming agent, 2 parts by weight of powdered basic tricalcium phosphate, 0.03 part by weight of sodium n-paraffin sulfonate and 300 parts by weight of water were put into a pressure vessel, and the temperature was adjusted in a range of 140-148°C according to the desired foaming ratio, and , further , the inner pressure was adjusted to between 15-22 kg/cm 2 by injecting isobutane. Thereafter, while keeping the temperature and pressure constant by injecting isobutane, pre-foamed beads were obtained by releasing the aqueous dispersion through an orifice into atmospheric pressure by opening a valve provided at the bottom of the pressure vessel. The foaming ratio and the shape of the obtained pre-foamed beads were evaluated . Further, uniformity of the cell diameter was evaluated by observing the cross-section of the pre-foamed beads with a microscope. The results were shown in Table 2. Comparative Example 13 Almost spherical resin granules of 1.67mg per one resin granule were produced with use of the resin granules comprising the compound produced in Example 1 by using the equipment used in Comparative Example 9. These resin granules were pre-foamed in the same method as used in Example 10 and were evaluated in the same way as in Comparative Examples 10 and 12. The results were shown in Table 2. Examples Resin granules used Foaming ratio of pre-formed beads Uniformity of cell Evaluation of shape Reference 10 Example 1 35 ○ ○ 11 Example 2 55 ○ ○ 12 Example 3 7 ○ ○ 13 Example 4 25 ○ ○ 14 Example 5 25 ○ ○ 15 Example 6 25 ○ ○ 16 Example 7 25 ○ ○ 17 Example 8 25 ○ ○ Comparative Examples 10 Comparative Example 1 25 ○ × Large void 11 Comparative Example 7 25 ○ ○ Shape became better after pre-foaming 12 Comparative Example 8 25 ○ × Extremely flat 13 Comparative Example 13 25 × ○

Claims: A method for producing polyolefin resin granules which comprises the steps of: extruding by using a kneading extruder a polyolefin resin from a die nozzle into water, and cutting the extrudate with a cutter blade in the water, characterized in that the kneading extruder is a homodirectional twin-screw kneading extruder, the die nozzle has a die nozzle hole having a diameter of less than 2 mm and a discharge amount per die nozzle hole of 2 - 8 Kg/hr, the water has a temperature of 5 - 90 °C which is lower than the temperature of the resin by 140 - 220 °C, and the peripheral speed of the cutter blade is 13 - 27 m/sec. A method as claimed in Claim 1, wherein the polyolefin resin contains talc as a nucleating agent. A method for producing polyolefin pre-foamed beads, which comprises pre-foaming the resin granules obtained in Claim 1 or 2.

Inventors: SAKAGUCHI HIROFUMI, SENDA KENICHI, SHIMAZU HISAO, SMETS RONALDS A, VAN RAVESTYN PIERRE, SAKAGUCHI, HIROFUMI, SENDA, KENICHI, SHIMAZU, HISAO, SMETS RONALDS, A., VAN RAVESTYN, PIERRE
Applicants: KANEGAFUCHI CHEMICAL IND, KANEKA BELGIUM NV, KANEGAFUCHI KAGAKU KOGYO KABUSHIKI KAISHA, KANEKA BELGIUM N.V.
Application year: 1995
Main classification: B29B9
IPC codes: B29K23, B29C47, B29C44, C08J9, B29B9