201038383 六、發明說明： 【發明所屬之技術領域】 本發明係關於一種藉水中熱切法製造發泡性熱塑性樹 脂粒子之發泡性熱塑性樹脂粒子之製造方法、熱塑性樹脂 發泡粒子之製造方法及熱塑性樹脂發泡成形體之製造方 法。 本案係依2009年2月09日於日本所申請之特願2009-027299號，主張優先權，此處援用其内容。 【先前技術】 以往，藉水中熱切法製造發泡性熱塑性樹脂粒子之發 泡性熱塑性樹脂粒子之製造方法，例如有專利文獻1至3 所揭示之技術。 專利文獻1中係揭示一種製造分子量Mw超過170000 g/莫耳之發泡苯乙烯聚合物的方法。此方法係使至少具有 120°C溫度之含發泡劑的苯乙烯聚合物熔融物，經由有模頭 出口的孔徑為1. 5mm以下之孔的模板而運送，然後，使撥 出物進行顆粒化之方法。 於專利文獻2中係揭示：造粒用鑄模、造粒裝置及使 用其之發泡性熱塑性樹脂粒子之製造方法，而該造粒用鑄 模係具備：接觸於水流而所設之樹脂擠出面；沿著前述樹 脂擠出面上之假想圓的圓周而配置，連通於擠壓機之缸筒 而開口於前述樹脂擠出面之複數噴嘴；於配置有前述喷嘴 之圓周内側之樹脂擠出面所設的隔熱材；通過前述圓周之 中心部而延伸至外側般，設於樹脂擠出面附近之複數個筒 4 321804 201038383 型電熱管。 於專利文獻3中係揭示一種熱塑 製造方法，其係在擠壓機内所炫融 以曰心危隊 之熟塑性樹脂中壓入發 === 從附設於擠壓機前端之模額 的複數小孔直接㈣至冷卻収體巾，在糾㈣以高速 方疋轉刀切斷擠出物，同時並使播出物益 尤饵出物错由與液體之接勝進 行冷卻固化㈣到發泡性粒子。此方Μ在通過前述模頭 Ο[Technical Field] The present invention relates to a method for producing foamable thermoplastic resin particles by which a foamable thermoplastic resin particle is produced by hot cutting in water, a method for producing a thermoplastic resin expanded particle, and a thermoplastic A method of producing a resin foam molded body. This case is based on the Japanese Patent Application No. 2009-027299, which was filed on February 9, 2009 in Japan, and claims the priority. [Prior Art] Conventionally, a method for producing foamable thermoplastic resin particles by which a foamable thermoplastic resin particle is produced by a hot-cut method in water is disclosed, for example, in the techniques disclosed in Patent Documents 1 to 3. Patent Document 1 discloses a method of producing a foamed styrene polymer having a molecular weight Mw exceeding 170,000 g/mole. The method is characterized in that the styrene polymer melt containing a blowing agent having a temperature of at least 120 ° C is transported through a template having a pore diameter of 1. 5 mm or less at the outlet of the die, and then the granules are granulated. The method of transformation. Patent Document 2 discloses a granulation mold, a granulation apparatus, and a method for producing foamable thermoplastic resin particles using the same, and the granulation mold has a resin extrusion surface which is provided in contact with a water flow. a plurality of nozzles which are disposed along the circumference of the imaginary circle on the resin extrusion surface, communicate with the cylinder of the extruder and open to the resin extrusion surface; and are disposed on the inner side of the circumference of the nozzle The heat insulating material is provided; a plurality of cylinders 4 321804 201038383 type electric heating tubes provided in the vicinity of the resin extrusion surface, extending to the outside through the center portion of the circumference. Patent Document 3 discloses a thermoplastic manufacturing method in which a plastic resin is immersed in an extruder and pressed into a mature plastic resin of a core team === from a plurality of modulus attached to the front end of the extruder The small hole directly (four) to the cooling body towel, in the correction (four) with a high-speed square knife to cut the extrudate, and at the same time and make the broadcast material benefit the bait out of the wrong with the liquid to cool and solidify (four) to foam Sex particles. This square is passing through the aforementioned die Ο
的小孔模唇部時之含有發泡劑的㈣㈣W 12000至3_ sec-i，且以樹脂之表觀嫁融黏度為ι〇〇至 700 poise之方式擠出的製造方法。 [先前技術文獻] (專利文獻） (專利文獻1)特表2005-534733號公報 (專利文獻 2) W0 2008/102874 (專利文獻 3) W0 2005/028173 〇【發明内容】 (發明欲解決之課題） 藉由水中熱切法製造發泡性熱塑性樹脂粒子時，使已 添加發泡劑之熔融樹脂從複數噴嘴擠壓至水中，其後亦即 切割前述溶融樹脂而形成樹脂粒子。但，鑄模前端面係與 循環水接觸，故可奪取熱。結果，從噴嘴擠出之樹脂會固 化’堵塞喷嘴而易降低樹脂粒子的生產效率。因此，在習 知技術中，藉由適當控制鑄模内部之溫度，以防止喷嘴之 堵塞，並製造發泡性熱塑性樹脂粒子。 5 321804 201038383 專利文獻1中係於段落0021記載著「模板之溫度以 比含有發泡劑之聚苯乙烯熔融物的溫度高20至100°C的範 圍為佳」。又，於段落0036之表2中記載著在製造發泡性 聚苯乙烯顆粒之實施例2中，對於熔融溫度200°C，使模 板溫度設定於180至240°C (相對於熔融溫度為-20°C至+40 °C)之製造例。 然而，如於專利文獻1所記載，使模板溫度設定成較 熔融樹脂溫度高20至100°C之條件下，即使嘗試以水中熱 切法之發泡性熱塑性樹脂粒子的連續生產，鑄模的小孔也 會堵塞，無法連續生產小粒且粒徑一致之發泡性熱塑性樹 脂粒子。 專利文獻2中在段落0053之表1中記載著擠出樹脂 溫度為170°C時，使鑄模保持溫度設定於270至280°C (相 對於擠出樹脂溫度為+10 0 °C至+110 °C )之製造例。 如專利文獻2所記載，使鑄模保持溫度設定成相對於 擠出樹脂溫度為+ 100°C至+ ll〇°C時，可藉由水中熱切法連 續生產發泡性熱塑性樹脂粒子。但，於所得到之發泡性熱 塑性樹脂粒子中混入大的粒子，很難得到小粒且粒徑一致 之發泡性熱塑性樹脂粒子。 又，於前述製造例所得到之發泡性熱塑性樹脂粒子係 於粒子内部存有許多空隙。藉此，使此發泡性熱塑性樹脂 粒子於預備發泡後進行模内發泡成形而製造發泡成形體 時，所製造之發泡成形體的強度會降低。 在專利文獻3中係通過模頭之小孔模唇部時之含有發 6 321804 201038383 泡劑的熔融樹脂之剪斷速度設定為12〇〇〇 至 35000 sec-1， 且樹月曰之表觀溶融I占度為加％之方式擠出。 又’於段洛0027中係記載著模頭導入部之發泡性樹脂的樹 脂溫：調整成較樹脂之融點高50至100。。。 、然而’於專利文獻3所記載之前述條件下，即使嘗試 以水中熱切法之發泡性熱塑性樹脂粒子的連續生產，禱模 ο J孔也會堵塞，無法連續生產小粒且粒徑一致 熱塑性樹脂粒子。 本發㈣有鍤於前述事情者’目的在於提供—種在水 發泡性熱塑性樹脂粒子的製造中，可連續生產 、心—致之發泡性熱塑性樹脂粒子之製造方法。 [用以解決課題之手段] 二了解決上述課題，本發明係採用以下之手段。 下步:發熱塑性樹脂粒子的製造方法:具有如 ❹ 樹脂麟二=用:=脂:':裝r給熱塑性 脂擠出面之鑄模本體.用板至夕具備具有樹 粒用鑄模移動，二=^_性義朝向前述造 含有發泡劑的樹脂之步:=性:脂注入發泡劑而形成 出面開孔之対職出:、纟則讀模本體之樹脂擠 ::卩…進行切斷而得到發泡性熱塑性樹^ = 述鑄旨粒子的製造方法中’係以使前 皿度比含發泡劑之樹脂之溶融樹月旨溫度高 321804 7 201038383 115°C至200°C範圍的方式進行溫度控制，而得到發泡性熱 塑性樹脂粒子。 本發明之熱塑性樹脂發泡粒子之製造方法，係具有如 下步驟：對安裝有造粒用鑄模之樹脂供給裝置供給熱塑性 樹脂並熔融混練的步驟，而該造粒用鑄模為至少具備具有 樹脂擠出面之鑄模本體；一邊使前述熱塑性樹脂朝向前述 造粒用鑄模移動，一邊於前述熱塑性樹脂注入發泡劑而形 成含有發泡劑的樹脂之步驟；將在前述鑄模本體之樹脂擠 出面開孔之喷嘴所擠出的前述含發泡劑之樹脂藉由切刀於 冷卻介質中進行切斷而得到發泡性熱塑性樹脂粒子之步 驟；與使前述發泡性熱塑性樹脂粒子進行預備發泡而得到 熱塑性樹脂發泡粒子之步驟。 在此熱塑性樹脂發泡粒子的製造方法中，係以使前述 鑄模本體之溫度比含發泡劑之樹脂的熔融樹脂溫度高115 °0至200°C範圍的方式進行溫度控制，而得到發泡性熱塑 性樹脂粒子。 本發明之熱塑性樹脂發泡成形體之製造方法，其係具 有如下步驟；對安裝有造粒用錄模之樹脂供給裝置供給熱 塑性樹脂並熔融混練的步驟，而該造粒用鑄模至少具備具 有樹脂擠出面之鑄模本體；一邊使前述熱塑性樹脂朝向前 述造粒用鑄模移動，一邊於前述熱塑性樹脂甲注入發泡劑 而形成含有發泡劑的樹脂之步驟；將在前述鑄模本體之樹 脂擠出面開孔之喷嘴所擠出的前述含發泡劑之樹脂，藉由 切刀於冷卻介質中進行切斷而得到發泡性熱塑性樹脂粒子 8 321804 201038383 之步驟；使前述發泡性熱塑性樹脂粒子進行預備發泡而得 到熱塑性樹脂發泡粒子之步驟；與使前述熱塑性樹脂發泡 .粒子進行模内發泡成形而得到熱塑性樹脂發泡成形體之步 ‘驟。 此熱塑性樹脂發泡成形體之製造方法中，其特徵為以 使前述鑄模本體之溫度比含發泡劑之樹脂之熔融樹脂溫度 高115t至200°C範圍的方式進行溫度控制，而得到發泡性 熱塑性樹脂粒子。 ® [發明之效果] 在本發明係以水中熱切法之發泡性熱塑性樹脂粒子的 製造中，以使前述鑄模本體之溫度比含發泡劑之樹脂之熔 融樹脂溫度高115°C至200°C範圍的方式進行溫度控制，而 得到發泡性熱塑性樹脂粒子。結果，可連續生產小粒且粒 徑一致之發泡性熱塑性樹脂粒子。 進一步，依本發明所得到之發泡性熱塑性樹脂粒子係 q 粒子内部的空隙小。因此，使所得到之發泡性熱塑性樹脂 粒子進行模内發泡成形而製造發泡成形體時，可提昇此發 泡成形體之機械強度。 【實施方式】 [用以實施發明之形態] 以下，參照圖面並說明本發明之實施形態。 第1圖係表示在本發明之製造方法中所使用之造粒裝 置的一例子構成圖；第2圖係表示其造粒用鑄模的一例之 側截面圖；第3圖係第2圖之鑄模本體的樹脂擠出面的側 9 321804 201038383 面圖；第4圖係表示喷嘴之配置狀態的圖。 如第1圖及第2圖所示’本實施形態之造粒裝置T係 藉由水中熱切方式而製造發泡性熱塑性樹脂粒子用的造粒 裝置。 本造粒裝置τ係具備：於前端安裝有造粒用鑄模1的 擠壓機2(樹脂供給裝置）、可收容從造粒用鱗模1之噴嘴 15所擠出之樹脂（在本實施形態中係含有發泡劑之樹脂20) 進行切斷之切刀同時並於造粒用鑄模1之樹脂擠出面 13接觸水流之腔體（chamber)4。腔體4係連接使循環水等 的冷卻介質（以下，記為水）流動之管路5。此管路5之一 端（較腔體4上流側）係經由送水泵浦6連接於水槽7。另 下流侧)係連接於從楯環水 外，管路5之另一端（較腔體4 之脫水處理部 之發泡性熱塑The manufacturing method of the foaming agent (4) (4) W 12000 to 3 sec-i, and the method of extruding the resin with an apparent grafting viscosity of ι to 700 poise. [PRIOR ART DOCUMENT] (Patent Document 1) (Patent Document 1) JP-A-2005-534733 (Patent Document 2) W0 2008/102874 (Patent Document 3) W0 2005/028173 〇 [Summary of the Invention] When the foamable thermoplastic resin particles are produced by hot cutting in water, the molten resin to which the foaming agent has been added is extruded from the plurality of nozzles into the water, and thereafter, the molten resin is cut to form resin particles. However, the front end of the mold is in contact with the circulating water, so heat can be taken. As a result, the resin extruded from the nozzle solidifies to block the nozzle and easily reduce the production efficiency of the resin particles. Therefore, in the prior art, the temperature of the inside of the mold is appropriately controlled to prevent clogging of the nozzle, and the foamable thermoplastic resin particles are produced. 5 321804 201038383 Patent Document 1 in paragraph 0021 describes that "the temperature of the template is preferably in the range of 20 to 100 ° C higher than the temperature of the polystyrene melt containing the blowing agent". Further, in Table 2 of paragraph 0036, in Example 2 for producing expandable polystyrene particles, the templating temperature was set to 180 to 240 ° C for the melting temperature of 200 ° C (relative to the melting temperature - Manufacturing example of 20 ° C to +40 ° C). However, as described in Patent Document 1, when the template temperature is set to be 20 to 100 ° C higher than the temperature of the molten resin, even if continuous production of the foamable thermoplastic resin particles by hot cut in water is attempted, the pores of the mold are drilled. It is also clogged, and it is impossible to continuously produce foamable thermoplastic resin particles having small particles and uniform particle diameters. In Patent Document 2, in Table 1 of paragraph 0053, when the temperature of the extruded resin is 170 ° C, the mold holding temperature is set to 270 to 280 ° C (relative to the temperature of the extruded resin is +10 0 ° C to +110). °C) Manufacturing example. As described in Patent Document 2, when the mold holding temperature is set to be +100 ° C to + ll 〇 ° C with respect to the temperature of the extruded resin, the foamable thermoplastic resin particles can be continuously produced by hot cutting in water. However, when large particles are mixed in the obtained foamable thermoplastic resin particles, it is difficult to obtain foamable thermoplastic resin particles having small particles and uniform particle diameters. Further, the expandable thermoplastic resin particles obtained in the above production examples have a large number of voids in the particles. By this, when the foamable molded article is produced by in-mold expansion molding of the foamable thermoplastic resin particles after preliminary foaming, the strength of the produced foam molded article is lowered. In Patent Document 3, the shearing speed of the molten resin containing the hair styling agent of the hair of the die is set to 12 〇〇〇 to 35,000 sec-1, and the appearance of the tree 曰 曰The melt I occupied was extruded in such a manner as to add %. Further, in Duanluo 0027, the resin temperature of the foamable resin in the die introduction portion is adjusted to be 50 to 100 higher than the melting point of the resin. . . However, under the above-described conditions described in Patent Document 3, even if the continuous production of the foamable thermoplastic resin particles by the hot cut method in water is attempted, the pores of the scrambling mold are blocked, and the continuous production of small particles and uniform particle size thermoplastic resin cannot be continuously produced. particle. The present invention is directed to a method for producing a foamable thermoplastic resin particle which can be continuously produced and produced in the production of water-foaming thermoplastic resin particles. [Means for Solving the Problem] In order to solve the above problems, the present invention employs the following means. Next step: a method for producing a thermoplastic resin particle: having a resin such as ruthenium ruthenium = use: = fat: ': a mold body to which an extrusion surface of a thermoplastic resin is loaded with r. With a plate to the eve, there is a mold for moving with a tree grain, =^_Sexuality towards the above-mentioned step of making a resin containing a foaming agent: = Sex: The fat is injected into the foaming agent to form a surface opening. The 树脂 出 纟 读 读 读 读 读 读 读 读 读 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂 树脂The foaming thermoplastic tree is obtained in a broken state. ^ = The method for producing the casting particles is described in the following paragraphs: The melting degree of the resin is higher than that of the resin containing the foaming agent. The temperature is 321804 7 201038383 115 ° C to 200 ° C The temperature control was carried out to obtain foamable thermoplastic resin particles. The method for producing a thermoplastic resin expanded particle of the present invention comprises the steps of: supplying a thermoplastic resin to a resin supply device to which a granulation mold is attached, and performing melt-kneading, wherein the granulation mold has at least a resin extrusion a mold main body; a step of forming a resin containing a foaming agent by injecting a foaming agent into the thermoplastic resin while moving the thermoplastic resin toward the granulation mold; and opening a resin extrusion surface of the mold body The foaming agent-containing resin extruded from the nozzle is cut into a cooling medium by a cutter to obtain foamable thermoplastic resin particles, and the foamable thermoplastic resin particles are preliminarily foamed. The step of foaming the thermoplastic resin particles. In the method for producing a thermoplastic resin expanded particle, the temperature is controlled so that the temperature of the mold main body is higher than the temperature of the molten resin of the resin containing the blowing agent by 115 ° 0 to 200 ° C to obtain foaming. Thermoplastic resin particles. The method for producing a thermoplastic resin foamed molded article of the present invention comprises the steps of: supplying a thermoplastic resin to a resin supply device to which a granulation recording die is attached, and performing melt-kneading, wherein the granulation mold has at least a resin a mold main body of an extrusion surface; a step of forming a resin containing a foaming agent by injecting a foaming agent onto the thermoplastic resin nail while moving the thermoplastic resin toward the granulation mold; and extruding the resin in the mold body a foaming agent-containing resin extruded from a nozzle having a face opening, which is subjected to cutting in a cooling medium by a cutter to obtain a foamable thermoplastic resin particle 8 321804 201038383; and the foamable thermoplastic resin particle The step of preliminary foaming to obtain expanded beads of thermoplastic resin; and the step of in-mold foam molding of the thermoplastic resin foamed particles to obtain a thermoplastic resin foam molded article. In the method for producing a thermoplastic resin foam molded article, the temperature is controlled such that the temperature of the mold body is higher than the temperature of the molten resin of the resin containing the foaming agent by 115 to 200 ° C to obtain foaming. Thermoplastic resin particles. ® [Effects of the Invention] In the production of the foamable thermoplastic resin particles by the hot cut method in the present invention, the temperature of the mold body is higher by 115 ° C to 200 ° than the temperature of the molten resin of the resin containing the foaming agent. Temperature control was carried out in a C range manner to obtain foamable thermoplastic resin particles. As a result, the expandable thermoplastic resin particles having small particles and uniform particle diameters can be continuously produced. Further, the foamable thermoplastic resin particles obtained according to the present invention have small voids inside the particles. Therefore, when the obtained foamable thermoplastic resin particles are subjected to in-mold expansion molding to produce a foam molded article, the mechanical strength of the foam molded article can be improved. [Embodiment] [Embodiment for Carrying Out the Invention] Hereinafter, embodiments of the present invention will be described with reference to the drawings. Fig. 1 is a block diagram showing an example of a granulator used in the production method of the present invention; Fig. 2 is a side cross-sectional view showing an example of a granulation mold; and Fig. 3 is a mold of Fig. 2; The side of the resin extrusion face of the body is 9 321804 201038383. The figure 4 is a view showing the arrangement state of the nozzle. As shown in Fig. 1 and Fig. 2, the granulation apparatus T of the present embodiment is a granulation apparatus for producing foamable thermoplastic resin particles by a hot cut method in water. The granulation apparatus τ includes an extruder 2 (resin supply device) to which the granulation mold 1 is attached at the tip end, and a resin that can be extruded from the nozzle 15 of the granulation die 1 (in the present embodiment) In the middle, the resin containing the foaming agent 20) is subjected to a cutting knife and simultaneously contacts the chamber 4 of the water flow on the resin extrusion surface 13 of the granulation casting mold 1. The chamber 4 is connected to a line 5 through which a cooling medium (hereinafter referred to as water) such as circulating water flows. One end of this line 5 (relative to the upstream side of the chamber 4) is connected to the water tank 7 via a water pump 6. The other downstream side is connected to the other end of the pipe 5 from the outer ring water (the foaming thermoplastic of the dehydration treatment portion of the cavity 4)
使發泡性熱塑性樹脂粒子分離、脫水•乾燥 8。於此脫水處理部8被分離，經脫水、乾燥 性樹脂粒子係被送至容器9。繼而’符號21 係發泡劑供給口 12 ’ 23係高壓泵浦。 下之說明 其相反側 又，在造粒裝置T及造粒用鑄模1中，在以 中統一使用：擠出樹脂之側為「前方」、「前端」， 為「後方」、「後端」。 牙圃八π u叫”丨’丨、/认項视用垮模1係由錶摄 體1〇(亦被稱為模板）、於擠壓機2之前端侧（圖中蹲棋 定之模座（die Holder)ll(亦被稱為轉接器）所右側) 模本體10係藉由複數之螺栓12固定於模座11成。此 模座11係以連通於擠壓機2之缸筒而設之前端相 。又置’後端側 321804 10 201038383 向前端侧，後端側流路1 la、前端側流路lib以其順序形 成。於鑄模本體10中在後端面中央部形成突出於後方侧而 成之圓錐狀凸部10a。在鑄模本體10與模座11連接之狀 態中，於模座11之前端側流路lib内以有預定間隙而插入 鑄模本體10之圓錐狀凸部10a。 亦即，含有發泡劑之樹脂20係通過模座11之後端側 流路11a，在前端側流路lib中沿著圓錐狀凸部10a的周 面而流動，連通於鑄模本體10之後端面開口之複數樹脂流 〇路14(後述）。 鑄模本體10係具備：於其前端面接觸於水流之樹脂擠 出面13 ;使從擠壓機2所擠出之含有發泡劑的樹脂20朝 向樹脂擠出面13而移送用之複數樹脂流路14 ;設於複數 樹脂流路14之前端同時開口於樹脂擠出面13之複數喷嘴 15 ;設於樹脂擠出面13之中心位置的隔熱材16 ;從樹脂 擠出面13位在擠壓機2側，用以加溫樹脂擠出面13或樹 0 脂流路14之筒型電熱管（cartridge heater)17 ;用以加溫 鑄模本體10之短電熱管18。 筒型電熱管17及短電熱管18係從以往習知之筒型電 熱管之中，依據鑄模本體10之大小或形狀而可以適當選擇 使用。例如，筒型電熱管17及短電熱器18係可使用一使 捲繞於棒狀之陶瓷的發熱線（鉻線）插入於管體（耐熱不銹 鋼）之中，由於發熱線與管體之間隙以高熱傳導性與高絕緣 性優異之材料（MgO)封住，故可以使用電力密度高之棒狀加 熱器。筒型電熱管17及短電熱器18係於單側附有2條導 11 321804 201038383 f之筒型電熱f、亦可於兩側各附有i條導線之筒型電熱 $ (Sheath Heater)。因為於單側附有2條導線之筒型電熱 官係較於兩側各附有1條導線之筒型電熱管有更高之電力 密度，故更佳。 鎊模本II 10之樹脂擠出面13係於其中心部配置圓形 截面之隔熱材16 ’於前述隔熱材16之徑方向外側使複數 喷嘴15的擠出口沿著同心圓而設。配置有隔熱材16及 稷數噴嘴15之樹脂擠出面13的中央部分，係設計成於腔 體4之内部與水接觸。 複數之樹知机路14係具有圓形截面，朝相對於樹脂擦 出面13正父之方向延長，以沿著鑄模本體1〇之中心軸線 為中〜之圓周(於樹脂擠出面13上描繪之圓周)而以一定 之間隔配置。在本實施形態中，樹脂流路丨4設有8處，相 鄰於前述圓周的周方向之樹脂流路14相互間的中心角成 :'、、 如别述般，此各樹脂流路14係連通於模座11的 前端側流路11b。 、 複數之喷嘴15係沿著於樹脂擠出面13上所描繪之圓 周而以預定間隔配置。如第4圖所示般，具體上，1個噴 嘴15由於係在樹脂流路14之截面形狀範圍内任意地配置 有複數的單體噴嘴15a、15b、15c、…之噴嘴單元（在本發 明中此稱為「喷嘴」）所構成。於各單體噴嘴15a、i5b、 be、…的配置方法例如採用可於複數之小圓周上並排多數 者’但’不限定於如此之配置形態。 隔熱材16係設於已配置複數噴嘴15的圓周内側之樹 321804 12 201038383 脂擠出面13。此隔熱材16係用以抑制鑄模本體ι〇之溫度 降低’以免於腔體4内之水中鑄模本體的熱逃逸。於此 隔熱材16係以具有耐水性，使用表面硬度高的構造之隔熱 材為佳。例如，即使與高溫之鑄模本體1〇接觸，也配置不 引起變形等之耐熱性能與隔熱性能優異之隔熱材，再以隔 熱性能優異之氟樹脂等的防水性樹脂被覆，進一步，於樹 月曰擠出面13侧可使用使不銹鋼、陶瓷等之表面硬度高的材 料依序層合的積層型隔熱材16。 同型電熱f 17及短電熱管μ係分別為棒狀電熱管。 筒f電熱管17係於造粒用鑄模！的前端後端方向，較短電 熱管18更近於樹脂擠出面13側之位置。 筒型電熱官17係在樹脂流路14之前述圓周的周方向 兩側’使其長方向朝向圓周的徑方向而橫切前述圓周的狀 態配置。此筒型電熱管17係於樹脂擠出面13之附近，而 加熱樹脂擠出® 13、嘴嘴15、及樹脂流路14。本實施形 〜、之筒型電熱官17係分別於圓周方向以預定的中心角（此 處45的角度）设有8條。亦即，各別之嘴嘴u係配置成 以2,筒型電熱管17間而由前述關的周方向挟住。 同型電熱管17係從樹脂擠出面13之附近，亦即由樹 =4出面13朝向擠壓機2#}而設於預定的電熱管深度之範 此電熱管深度係指從樹脂擠出自Η 加 Γ電熱管17的中心部之距離。此電熱管深度係於鎢= 制久性錢成障礙之範圍，小者㈣嘴之閉塞抑 大，為佳。亦即，電熱管深度宜為10至50 mm的 321804 13 201038383 電熱管深度小於1Q _時，有可能於鱗模之加工而 塞抑制效果有可能降低。f ^ 5g咖’噴嘴之閉 30咖。 更佳之電熱管深度的範圍為15至 面積熱管Π之直徑係為了廣泛確保樹脂流路之截 =增大喷嘴數目，故可確保發熱容㈣範 二亦即’筒型電熱管17之直徑宜為15咖 為 電熱管Π之直徑小於1Q随時，很難確保必需之發 10:至^熱管亦叩貴。因此’筒型電熱管17之直徑宜為 随至15 mm’更宜為1〇麵至12则^ 同型f熱管17之長度尺寸係在鑄模本體^的半和方 置之対15更中心側延伸之位置（至少_電 :二：_足喷嘴15成為中心側之位置)至 10的略外周之位置的長度。 假 短電熱管18係相對於各筒型電熱管17而以預 而於後方側配置與筒型電熱f 17之根數同數（8根）。此短 電熱管18係使樹月旨流路14之後端側加熱。短電熱管Μ 之長度尺寸係較筒型電熱管17短。 於造粒關㈣設有用以測輯模本體的溫度或炫融 樹脂溫度之測溫體19A、19B。第i測溫體19A係測定缚模 本體10之中央部的溫度（鑄模本體之溫度：鑄模保持溫 度）。第2測溫體19B係測定鑄模座n内流動之含有發泡 劑樹脂的熔融樹脂溫度（及樹脂壓力）。 說明有關使用前述造粒裝置T之發泡性熱塑性樹脂粒 321804 14 201038383 子、熱塑性樹脂發泡粒子、及熱塑性樹脂發泡成形體的製 造方法。 第1圖所示之造粒裝置T使用的擠壓機2(樹脂供給裝 置）係依據從以往習知之各種擠壓機中造粒之樹月旨種類等 而適¥選擇使用。例如，使用螺桿（screw)之擠壓機或不使 用螺桿的擠壓機之任一者均可使用。使用螺桿之擠壓機， 可舉例如：單軸式擠壓機、多轴式擠壓機、透氣式擠壓機、 ❹串聯複式（Tandem式）擠壓機等。不使用螺桿的擠壓機可舉 例如：柱塞（plunger)式擠壓機、齒軸泵浦式擠壓機等。此 等之任一者的擠壓機亦可使用靜力混合器（static mixer)。此等之擠壓機中，從生產性之方面，宜為使用螺 杯之擠壓機。又，收容切刀3之腔體4亦可使用在熱切法 中所使用之以往周知者。- 在本發明中，熱塑性樹脂之種類係不限定。例如可使 聚苯乙烯系樹脂、聚乙烯系樹脂、聚丙烯系樹脂、聚酯系 ❹树月曰、氯化乙烯系樹脂、ABS樹脂、AS樹月旨等單獨或混合 2種類以上而使用。進一步，就樹脂製品而言，亦可使用 暫時使甩後回收所得到之熱塑性樹脂的回收樹脂。尤其， 非晶性之聚苯乙烯（GPPS)、耐衝擊聚苯乙烯（HIps)等之聚 苯乙烯系樹脂為適合使用。聚笨乙烯系樹脂例如有：苯乙 烯、曱基笨乙烯、乙烯基曱笨、氯苯乙烯、乙基苯乙烯、 異丙基苯乙烯、二甲基苯乙烯、溴苯乙烯等之苯乙烯系單 體的單獨聚合物或此等之共聚物等。尤其’以含有苯乙烯 50質量％以上之聚苯乙烯系樹脂為宜，更宜為聚苯乙烯。 321804 15 201038383 前述聚苯乙烯系樹脂亦可為以前述苯乙烯單體作為主 成分之前述苯乙烯系單體、與可與該苯乙烯系單體共聚合 之乙缔基單體之共聚物。如此之乙稀基單體例如有：甲基 (甲基）丙烯酸酯、乙基（甲基）丙烯酸酯、丁基（甲基）丙烯 酸酯、鯨蠟基（甲基）丙烯酸酯等之烷基（甲基）丙烯酸酯、 (甲基）丙嫦腈、二甲基馬來酸酯、二甲基富馬酸醋、二乙 基富馬酸酯、乙基富馬酸酯、及二乙烯基苯、伸烷基二醇 二甲基丙稀酸酯等之二官能性單體等。 只要以聚笨乙烯系樹脂為主成分，亦可添加其他之樹 月曰。添加之樹脂係為了提昇發泡成形體的耐衝擊性，例如 有已添加聚丁二烯、苯乙烯—丁二烯系共聚物、乙烯一丙烯_ 非共轆雙烯三次元共聚物等之二稀系的橡膠狀聚合物之橡 膠改質聚苯乙婦系樹脂（耐衝擊聚苯乙烯）。進—步，有聚 乙稀系樹月旨、聚丙婦系樹脂 '丙婦酸系樹月旨、丙烤猜-苯乙 烯共聚物、丙烯腈-丁二烯_苯乙稀共聚㈣。使用本發明 讀泡性熱難樹絲子的製造方法而製造發泡性聚笨乙 烯系樹脂粒子時，係成為原料之聚苯乙稀系樹脂者，可使 用以市售的-般聚苯乙烯系樹脂、以懸濁聚合法等的方法 =新製作之聚苯乙稀系樹月旨等的非回收原料的聚苯乙稀系 树月曰（以下’記載為初始聚苯乙稀系樹脂）。進—步，可以 使用種使用過之聚苯乙婦系樹腊發泡成形體進行再生處 收原料。此回收原料可使用：回收使用過之 裝發泡=體之魚箱、家電緩衝材、食品包 、 猎由㈣^imGnene)溶解方式或加熱減 321804 16 201038383 谷積方式而再生處理者。進一步，如前述之回收原料以外， 亦可使用將家電製品（例如t視、冰箱、洗衣機、冷氣機等） 或事務用機器（例如，影印機、傳真機、印表機等）所分別 回收之非發泡的聚苯乙烯系樹脂成形體進行粉碎， 練而形成再顆粒者。 施 如第1圖及第2圖所示，使用前述之造粒裝置τ而製 造發泡性熱塑性樹脂粒子時，如以下之步驟丨至5依序實 ΟThe foamable thermoplastic resin particles are separated, dehydrated, and dried. The dehydration treatment unit 8 is separated, and the dehydrated and dried resin particles are sent to the container 9. Then, the symbol 21 is a blowing agent supply port 12', which is a high-pressure pump. In the granulation apparatus T and the granulation mold 1 described above, the side of the extrusion resin is "front" and "front end", and "rear" and "rear end". .圃 圃 π 叫 叫 丨 / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / / The die body 10 is fixed to the die holder 11 by a plurality of bolts 12. The die holder 11 is connected to the cylinder of the extruder 2 The front end phase is set, and the rear end side 321804 10 201038383 is disposed toward the front end side, and the rear end side flow path 1 la and the front end side flow path lib are formed in this order. In the mold main body 10, a rear portion is formed at the center of the rear end surface. In a state in which the mold main body 10 is connected to the mold base 11, the conical convex portion 10a of the mold main body 10 is inserted into the end side flow path lib before the mold base 11 with a predetermined gap. In other words, the resin 20 containing the foaming agent passes through the end side flow path 11a of the die holder 11, and flows along the circumferential surface of the conical convex portion 10a in the distal end side flow path lib, and communicates with the mold body 10 after the end surface opening. The plurality of resin flow paths 14 (described later). The mold body 10 is provided with a resin extrusion surface 13 whose front end surface is in contact with the water flow. The plurality of resin flow paths 14 for transferring the resin 20 containing the foaming agent extruded from the extruder 2 toward the resin extrusion surface 13 are provided; the front end of the plurality of resin flow paths 14 is simultaneously opened at the resin extrusion surface 13 plural nozzle 15; heat insulating material 16 disposed at the center of the resin extrusion surface 13; 13 from the resin extrusion surface on the extruder 2 side for heating the resin extrusion surface 13 or the tree 0 grease flow a tube type heat exchanger tube 17; a short electric heating tube 18 for heating the mold body 10. The tube type electric heating tube 17 and the short electric heating tube 18 are among the conventional tube type electric heating tubes, according to the mold The size or shape of the body 10 can be appropriately selected and used. For example, the cylindrical electric heating tube 17 and the short electric heater 18 can be inserted into the tube body by using a heating wire (chromium wire) wound around a rod-shaped ceramic (heat-resistant stainless steel). Among them, since the gap between the heating wire and the tube is sealed with a material having high thermal conductivity and high insulation (MgO), a rod heater having a high power density can be used. The barrel type electric heating tube 17 and the short electric heater 18 series on one side with 2 guides 11 321804 201038383 f barrel type electric heating f, also A Sheath Heater with i-wires on each side. Because the tube-type electric heating system with two wires on one side has a tubular electric heating tube with one wire on each side. The resin extrusion surface 13 of the pound model II 10 is provided with a circular cross section of the heat insulating material 16' at the center thereof, and the plurality of nozzles 15 are provided on the outer side in the radial direction of the heat insulating material 16 The extrusion port is provided along a concentric circle. The central portion of the resin extrusion surface 13 in which the heat insulating material 16 and the number of nozzles 15 are disposed is designed to be in contact with water inside the cavity 4. The plurality of trees know that the machine path 14 has a circular cross section and is extended in the direction of the father of the resin wiping surface 13 so as to be drawn along the center axis of the mold body 1〇 (to be drawn on the resin extrusion surface 13). The circumference is configured at a certain interval. In the present embodiment, the resin flow path 4 is provided in eight places, and the central angle between the resin flow paths 14 adjacent to the circumferential direction of the circumference is: ', and the resin flow paths 14 are not described. It is connected to the front end side flow path 11b of the die holder 11. The plurality of nozzles 15 are arranged at predetermined intervals along the circumference drawn on the resin extrusion surface 13. As shown in FIG. 4, in particular, one nozzle 15 is arbitrarily arranged with nozzle units of a plurality of unit nozzles 15a, 15b, 15c, ... in the cross-sectional shape range of the resin flow path 14 (in the present invention) This is called "nozzle". The arrangement method of each of the unit nozzles 15a, i5b, be, ... is, for example, a plurality of sides which can be arranged on a plurality of small circumferences, but the arrangement is not limited to such an arrangement. The heat insulating material 16 is provided on a tree 321804 12 201038383 grease extrusion surface 13 on the inner side of the circumference where the plurality of nozzles 15 are disposed. The heat insulating material 16 is for suppressing the temperature drop of the molded body 〇 to prevent heat escape from the water casting body in the cavity 4. Here, the heat insulating material 16 is preferably a heat insulating material having a water resistance and a structure having a high surface hardness. For example, even if it is in contact with the high-temperature mold body 1〇, a heat-insulating material which is excellent in heat resistance and heat-insulating property, such as deformation, is disposed, and is coated with a water-repellent resin such as a fluororesin having excellent heat insulating properties, and further A laminated heat insulating material 16 in which a material having a high surface hardness such as stainless steel or ceramics is laminated in this order can be used. The same type of electric heating f 17 and the short electric heating tube μ are respectively rod-shaped electric heating tubes. The tube f electric heating tube 17 is used for the granulation mold! In the front end rear end direction, the shorter electric heating tube 18 is closer to the resin extrusion surface 13 side. The cylindrical electric heaters 17 are disposed on both sides in the circumferential direction of the circumference of the resin flow path 14 such that the longitudinal direction thereof is transverse to the circumference in the radial direction of the circumference. This cylindrical electric heating tube 17 is in the vicinity of the resin extrusion surface 13, and heats the resin extrusion® 13, the nozzle 15, and the resin flow path 14. The cylindrical electric heaters 17 of the present embodiment are respectively provided with eight at a predetermined central angle (the angle of 45) in the circumferential direction. That is, the respective nozzles u are arranged so as to be caught by the circumferential direction of the above-mentioned closed between the two types of tubular electric heating tubes 17. The isoelectric heating tube 17 is disposed from the vicinity of the resin extrusion surface 13, that is, from the tree=4 exit surface 13 toward the extruder 2#}, and is set at a predetermined electric heating tube depth. The electric heating tube depth refers to extrusion from the resin. The distance from the center of the electric heating tube 17 is increased. The depth of the electric heating pipe is in the range of tungsten = permanent damage, and the small (four) mouth is blocked, which is preferable. That is, the depth of the electric heating tube is preferably 10 to 50 mm. 321804 13 201038383 When the electric heating tube depth is less than 1Q _, there is a possibility that the plugging effect may be reduced in the processing of the scale mold. f ^ 5g coffee 'nozzle closed 30 coffee. The better electric heating tube depth ranges from 15 to the area of the heat pipe. In order to ensure the cross section of the resin flow path to increase the number of nozzles, it is possible to ensure the heat capacity (4), that is, the diameter of the tube type electric heating tube 17 is preferably 15 coffee for the electric heating tube diameter is less than 1Q at any time, it is difficult to ensure the necessary hair 10: to ^ heat pipe is also expensive. Therefore, the diameter of the tubular electric heating tube 17 is preferably as follows: 15 mm' is more preferably 1 to 12 degrees. ^ The length of the heat pipe 17 of the same type f is extended on the center side of the half and the side of the mold body. The position (at least _ electric: two: _ foot nozzle 15 becomes the position on the center side) to the length of the slightly outer circumference of 10. The dummy short electric heating tubes 18 are arranged in the same number on the rear side as the number of the cylindrical electric heating units 17 (8 pieces) with respect to the respective cylindrical electric heating tubes 17. This short electric heating pipe 18 heats the rear end side of the tree-shaped flow path 14. The length of the short electric heating tube 短 is shorter than that of the barrel type electric heating tube 17. In the granulation off (4), temperature measuring bodies 19A, 19B for measuring the temperature of the mold body or the temperature of the smelting resin are provided. The i-th temperature measuring body 19A measures the temperature of the central portion of the mold main body 10 (temperature of the mold main body: mold holding temperature). The second temperature measuring body 19B measures the temperature (and resin pressure) of the molten resin containing the foaming agent resin flowing in the mold base n. A method for producing foamable thermoplastic resin particles 321804 14 201038383 using the granulator T, thermoplastic resin expanded particles, and a thermoplastic resin foam molded article will be described. The extruder 2 (resin supply means) used in the granulation apparatus T shown in Fig. 1 is selected and used in accordance with the type of granulation of various types of extruders conventionally known. For example, either an extruder using a screw or an extruder not using a screw can be used. Examples of the extruder using a screw include a single-shaft extruder, a multi-axis extruder, a gas permeable extruder, and a Tandem-type extruder. An extruder that does not use a screw may be, for example, a plunger extruder, a pinion pump extruder, or the like. A static mixer can also be used for the extruder of any of these. In such an extruder, from the viewpoint of productivity, an extruder using a screw cup is preferable. Further, the cavity 4 for accommodating the cutter 3 can also be used by a conventionally known person used in the hot cutting method. - In the present invention, the kind of the thermoplastic resin is not limited. For example, a polystyrene resin, a polyethylene resin, a polypropylene resin, a polyester eucalyptus, a chlorinated vinyl resin, an ABS resin, or an AS tree can be used alone or in combination of two or more types. Further, as the resin product, a recycled resin which temporarily recovers the obtained thermoplastic resin can be used. In particular, a polystyrene-based resin such as amorphous polystyrene (GPPS) or impact-resistant polystyrene (HIps) is suitably used. Examples of the polystyrene-based resin include styrene, fluorenyl styrene, vinyl styrene, chlorostyrene, ethyl styrene, isopropyl styrene, dimethyl styrene, and bromostyrene. A single polymer of a monomer or a copolymer of these or the like. In particular, it is preferable to use a polystyrene resin containing 50% by mass or more of styrene, more preferably polystyrene. 321804 15 201038383 The polystyrene resin may be a copolymer of the styrene monomer having the styrene monomer as a main component and an ethylenic monomer copolymerizable with the styrene monomer. Examples of such an ethylene-based monomer include alkyl groups such as methyl (meth) acrylate, ethyl (meth) acrylate, butyl (meth) acrylate, and cetyl (meth) acrylate. (Meth)acrylate, (meth)propanenitrile, dimethyl maleate, dimethyl fumarate, diethyl fumarate, ethyl fumarate, and divinyl a difunctional monomer such as benzene or alkylene glycol dimethyl acrylate. As long as the polystyrene-based resin is used as the main component, other trees can be added. The resin to be added is for example, in order to improve the impact resistance of the foamed molded article, for example, a polybutadiene, a styrene-butadiene copolymer, an ethylene-propylene-non-co-bisopene terpolymer, and the like are added. A rubber-modified polystyrene resin (impact resistant polystyrene) of a rare rubbery polymer. In the next step, there is a polystyrene tree, a polyacrylic resin, a 'futosan acid tree', a propylene, a styrene-styrene copolymer, and an acrylonitrile-butadiene-styrene copolymer (four). When the foamable polystyrene-based resin particles are produced by the method for producing a foaming heat-resistant sapphire of the present invention, a commercially available polystyrene-based resin can be used as the raw material of the polystyrene-based resin. A method of a resin, a suspension polymerization method, or the like, a non-recycled raw material of a newly produced polystyrene tree, etc. (hereinafter referred to as an initial polystyrene resin) . In the next step, the polyphenylene-based tree wax foam molded body can be used to regenerate the raw materials. This recycled raw material can be used: recycled used foaming = body fish tank, home appliance cushioning material, food package, hunting by (four) ^ imGnene) dissolution method or heating minus 321804 16 201038383 grain product method and regeneration processor. Further, in addition to the above-mentioned recovered raw materials, it is also possible to separately collect household electrical appliances (for example, t-views, refrigerators, washing machines, air conditioners, etc.) or business machines (for example, photocopiers, facsimile machines, printers, etc.). The non-foamed polystyrene resin molded body is pulverized and formed to form granules. As shown in Fig. 1 and Fig. 2, when the foamable thermoplastic resin particles are produced by using the above-described granulating device τ, the following steps 丨 to 5 are sequentially performed.
G (步驟1)於前端絲有造粒賴模丨之擠壓機2將熱塑性 樹脂自供料斗21供給，再進行熔融而混練。 (步驟2)—面朝造粒用鑄模1使熱塑性樹脂移動，一面在 此熱塑性樹脂中自發泡劑供給口 22藉由高壓泵浦23而壓 入發泡劑。亦即，混合發泡劑與熱塑性樹脂而形成含發泡 劑之樹脂20。 S ' (步驟3)含發泡劑之樹脂20係從_ 2之前端經過模座 11，送至鑄模本體10之樹脂流路14。 ' (步驟4)通過樹脂流路14而運送之含發泡劑的樹脂如 從在鑄模本本體ίο的樹脂擠出面13開孔之各嘴^ a ” 出。 、擠 (步驟5)從各喷嘴15所擠出之含發泡劑之樹脂2〇 切刀3之旋轉刀於腔體4之水流中（冷卻介質中）”曰 此含發泡劑之樹脂20的造粒時，禱模本體1〇接切^ :較含發泡劑之樹脂2G之炫融樹月旨溫度高U5t = j 範圍，使各電熱管進行_fi控制。藉此，―行=: 321804 17 201038383 體ίο之溫度控制，同時並藉水中熱切法進行造教、 質之循環水的溫度係調節至1〇至6〇〇c。 。冷却介 又，所謂此熔融樹脂溫度係指自擠壓機2 ^ 模座11之含發泡劑樹脂20的溫度。在本實形=别端流入 第2測溫體19B測定此熔融樹脂溫度^ 、中，轉由 如此，鑄模本體1()之溫度為設成較熔融樹炉⑼ 115。〇至20〇°C之方式，較佳係高120¾至ι8(Γ(：曰地度高 高i2〇°C至18(TC進行溫度控制。藉由此，在以水中^佳係 製造發泡性熱塑性樹脂粒子中，可連續生產小粒且法 致之發泡性熱塑性樹脂粒子。又，若以前述條件進行^ 時，所得到之發泡性熱塑性樹脂粒子内部的空隙變少 由此，可提昇使該發泡性熱塑性樹脂粒子進行模内發、、包= 形而製造之發泡成形體的機械強度。 砮鑄模本體之溫度小於熔融樹脂溫度+丨^七時，連續 生暴發泡性熱塑性樹脂粒子之際，噴嘴15為堵塞而鑄模本 體内的樹脂壓力會變動。其結果，有可能無法連續生產小 粒真槔徑一致之發泡性熱塑性樹脂粒子。又，所得到之發 泡帙熱塑性樹脂粒子截面的空隙變多。其結果，使該發泡 性熱塑性樹脂粒子進行模内發泡成形並製造之發泡成形體 的機械強度有可能下降。 砮鑄模本體10之溫度超過熔融樹脂溫度+20CTC時，所 得到之發泡性熱塑性樹脂粒子會微發泡。其結果，有可能 無法速續生產小粒且粒徑一致之粒子。 芳冷卻介質之循環水之溫度小於l〇°C時，從循環水奪 18 321804 201038383 =自樹&播出面13之熱變大。其結果，造粒用鑄模1之 =又很難保持。另外，若循環水之溫度超過6GX：時，所切 =樹版冷卻變得不足。其結果，樹脂粒子之微發泡的抑 困難循％水之溫度較佳係2〇。〇至4〇。〇之範圍，更佳 係25 C至35°C之範圍。 於腔體4内切斷成粒狀之含發泡劑的樹月旨20係成為約 球狀之發泡性熱龍樹絲子。該發泡性_性樹脂粒子 ο ΐ藉！^IL而於官路5内搬送’到達脫水處理部8。此處， 攸循％水分離發泡性熱塑性樹脂粒子，進行脫水，乾燥， 時所刀離之水被送至水槽7。於此脫水處理部8被分離， 經脫水、乾燥之發泡性熱塑性樹脂粒子係被送至容器9， 收容於此容器内。 述發泡劑未被限定。例如可正姐、異戊炫、環戊 烧^戊一稀等單獨或混合2種類以上而使用。又，亦可 乂月J述戊燒類作為主成分而混合正丁燒、異丁烧、丙烧等 ❹使用尤其，戊烷類係容易抑制從喷嘴擠出於水流中時 之粒子的發泡，故適宜使用。 =胃發泡性驗性樹跡子係指在熱塑性樹脂中含; 路& 成形輕狀’較佳細彡以、球狀之樹脂粒子。^ ==、，、塑性樹脂粒子係可使用於所希㈣狀之發泡始 之製造。首先，使該發泡性熱塑性樹脂粒子在自^ :曰:進仃加熱而預備發泡。將此預備發泡粒子置入… 形狀之腔體的成形模胺體内，進行蒸氣加熱而4 預備發泡粒子相互_接。之後，可藉由脫模而製造心 321804 19 201038383 望形狀之發泡樹腊成形體。 如前述，在本發明中係在以水中熱切法製造發泡性熱 塑性樹脂粒子中，前述鑄模本體之溫度較含發泡劍樹腊I 溶融樹月旨溫度高115°[至2G(TC範圍之方式進行溫度控 制，同時可得到發泡性熱塑性樹脂粒子。藉由此，可連續 生產小粒且粒徑一致之發泡性熱塑性樹脂粒子。 又，藉由本發明所得之發泡性熱塑性樹脂粒子中係粒 子内部的空隙變少。藉此，可提昇使所得之發泡性熱塑性 樹脂粒子進行模内發泡成形所製造之發泡成形體的機械強 度。 在本發明的製造方法中之詳細製造條件，係可依據所 使用之樹脂種類而適當設定，但較佳之製造條件可舉例如 下之項目。⑴铸模本體1〇n喷嘴15的孔徑宜為0.2mm至 2.0腿的範圍’較佳為〇 3咖至1〇随的範圍，更佳為0.4随 至0· 7mm的範圍。⑵所得到之發泡性熱塑性樹脂粒子的粒 ^宜為0.3咖至2.0随的範圍，較佳為〇 5随至14_的 粑圍，更佳為0.7mm至1.2賴的範圍。⑶發泡性熱塑性樹 脂粒子為發泡性聚苯乙烯系樹脂粒子時，聚苯乙稀系樹脂 粒子之/量平均分子量Mw宜為12萬至4G萬的範圍，更佳 為12萬至27萬的範圍。（4)發泡性熱塑性樹脂粒子中之發 泡劑含量宜為1至1〇質量％之範圍’較佳為3至8質量％ 之範圍更佳為4至6質量％之範圍。⑸發泡劑宜為正戊 烷、異戊烷、或此等之任意比率混合的混合戊烷。混合戊 院之情形’其組成就質量比以異戊燒··正戊统=1〇 : 9〇至 321804 20 201038383 80 : 20之範圍為佳，更佳為異戊烷：正戊烷=80 ·· 80至60 : 40之範圍。（6)使發泡性熱塑性樹脂粒子進行預備發泡所 得到之熱塑性樹脂發泡粒子的平均氣泡徑以30//Π1至500 , #m之範圍為佳，較佳為50/zm至300 /zm之範圍，更佳為 100/zm 至 250/zm 之範圍。 如前述，本發明之發泡性熱塑性樹脂粒子的製造方法 中，係鑄模本體10之溫度較熔融樹脂溫度高115°C至200 °C，較佳係以高120°C至180°C之方式進行溫度控制。藉由 〇 此，在以水中熱切法製造發泡性熱塑性樹脂粒手中，可連 續生產小粒且粒徑一致之發泡性熱塑性樹脂粒子。又，此 連續生產是指從造粒開始至少12小時以上，較佳係24小 時以上連續並生產發泡性熱塑性樹脂粒子。若依本發明之 製造方法，在48小時以上之連續生產中，可連續生產噴嘴 開孔率的減少為在50%以下，所得到之發泡性熱塑性樹脂 粒子的粒徑變化率為20%以下之發泡性熱塑性樹脂粒子。 0 又，以採用前述較佳之製造條件（1)至（6 )，可得到如 下之效果。（a)為得到相同之發泡倍數，可刪減發泡劑量。 (b)經時性之發泡性下降小，粒子生命期長。（c)低壓成形 性優異（用以得到發泡成形體之加熱能量小，而能省能 源）。（d)具有充分的機會強度。（e)可得到發泡成形倍數5 至67倍。 其次，有關本發明之實施形態的變形例。依據圖面而 進行說明。但，與前述之實施形態相同或同樣的構件、零 件係使用相同之符號而省略說明，說明有關與前述實施形 21 321804 201038383 態相異之構成 的圖 第5圖所示之變形例的樹脂流路14Α，其截面形狀禮 成_形形狀，於其梯形形狀之範圍内設有任意截2= 個早體喷嘴15a、15b、15c...的喷嘴15。構成樹職路— 之外圍的斜面14a、14b(直線部）係配置成與筒型電献管17 的長方向略平行。在本變形例中，構成梯形形狀之截面的 樹脂流路14A之斜面14a、14b為相對於㈣電熱管17成 為等距離。因此，藉筒型電熱fl7而被均等地加熱之樹脂 流路的面積增加，與圓_面之難流路相比而被均等地 加熱’可更減少喷嘴的堵塞。 [實施例] [實施例1] 在實施例1中係於第丨圖所示之造粒裝置τ安裝第2 圖及第3圖所示之造粒用鑄模卜而製造發泡性聚笨乙稀 糸樹月旨粒子。 於口徑90mm(L/D=35)之單軸擠壓機安裝造粒用鑄模。 所使用之造粒賴模係具備：8個配置讀轉出面的圓 周面上之噴嘴單元（具有25個直徑〇. 6mm、模唇長3. 〇咖 的噴嘴之多孔板）、與使通過樹脂擠出面側之嘴嘴單元的各 树脂流路從兩側扶住，於電熱管深度（自樹脂擠出面起的距 離）15細1的位置橫切前述圓周而配置成放射狀之8根筒型 電熱管（直徑12mm)、與樹脂擠出面之中央部裝載的隔熱 321804 22 201038383 材。進一步，如第2圖所示，配置複數枝之測溫體i9A、 19B於鳍模本體的循環水流人側的電熱管4根與循環水流 電熱管4根分職2個區域而進行控制，使鑄模本 體之溫度（鑄模保持溫度）保持於30(TC。 在實施例1中係依序實施以下之步驟。 (「步驟1)於聚苯乙埽樹脂（東洋苯乙婦公司製，商品名 HRM10N」，維卡（Vicat)軟化點温度102。〇100質量份中 〇預先^轉鼓（tumbler)型混合機均一地混合微粉末滑石粉 0.3質量份，以每小時13〇kg的比率供給至擠壓機内。 (步驟2)使擠壓機内之最高溫度設定於22代而溶融樹脂 後，從擠壓機之中途相對於100質量份壓入6質量份之戊 烷（異戊烷/正戊烷=20/80混合物）作為發泡劑。 (步驟3)於擠壓機内持續混練樹脂與發泡劑，並使含有發 泡劑之熔融樹脂通入到模座（擠壓機與鑄模本體之連結 部），而輸送至保持於3〇〇〇c之前述鑄模本體。 〇(步驟4)於3(TC之冷卻水進行循環之腔體内擠壓含有發泡 劑的溶融樹脂’同時並使於圓周方向具有1Q片的刀具之高 速旋轉切割刀密著於鑄模，以每分鐘3300次轉切斷所擠壓 出之含有發泡劑的熔融樹脂。 (步驟5)分離從冷卻水所掩出之含有發泡劑的溶融樹脂， 進行脫水乾燥而得到球形之發泡性聚苯乙婦系樹月旨粒子。 在上述步驟中’在模座的熔融樹脂溫度為18〇。(：，發 泡性聚苯乙烯樹脂粒子之擠出量為138kg/h。 播出開始第1小時係於造粒用鱗模之樹脂導入部的壓 321804 23 201038383 力為10. OMPa，乾燥後之樹脂粒子100粒的質量為 0. 0417g，鑄模之開孔率為92. 0%，為良好的造粒環境。 擠出開始第48小時亦於造粒用鑄模之樹脂導入部的 壓力為10. 5MPa，乾燥後之樹脂粒子100粒的質量為 0. 0427g，鑄模之開孔率為90. 0%時，可維持良好的造粒狀 況。亦即，於此實施例1中’係可確認出有48小時以上之 安定並可造粒。 [比較例1] 除了使鑄模本體之溫度（鑄模保持溫度）為220°C以 外，其餘係與實施例1同樣做法，以擠出量138kg/h得到 約球狀之發泡性聚苯乙烯樹脂粒子。在此時之模座的熔融 樹脂溫度為180°C。 在此比較例1中’由於在擠出開始1小時以内於鑄模 之樹脂導入部的壓力就到達鑄模之耐壓上限（25MPa)，故停 止擠壓。無法擠壓1小時，故不能評估。 [比較例2] 除了使鑄模本體之溫度定為29(TC以外，其餘係與實 施例1同樣做法，以掩出量138kg/h得到約球狀之發泡性 聚苯乙烯樹餘子。在此時之模雜融樹脂溫度為18(TC。 、於擠出開始第1小時係於造粒用鎢模之樹脂導入部的 壓力為12. OMPa，乾燥後之樹脂粒？ 1〇〇孝立的質量為 〇. 〇446g，鑄模之開孔率為86 〇%，為良好的造粒環境。 、擠出開始第48小時亦於造粒用錄模之樹脂導入部的 壓力為13, OMPa，乾燥後之樹脂粒子1〇〇幸立的質量為 321804 24 201038383 0.0451g，鑄模之開孔率為85.0%，可維持良好的造粒環境。 亦即’於此比較例2中係可確認有48小時以上安定且可造 粒。 對於實施例1及比較例1至2的發泡性聚苯乙烯樹脂 粒子之製造時，及所得到之發泡性聚苯乙烯樹脂粒子，實 施以下各項目的測定、評估。其結果歸納於表丨並記載。 <鑄模之開孔率> 開孔率係以下式（1)所定義。 〇 、 式（1)開孔率（鑄模表面的擠出噴嘴之擠出時開孔率） =開孔數/鑄模全噴嘴數Xl〇〇(%) 擠出量係以下式（2)所定義。 式（2)擠出量（kg/h)=每lhr，以切刀所切出之全發 泡性粒子之總質量 =開孔數X切出個數xl粒質量 =開孔數X切刀片數X切刀旋轉數X1粒質量 〇 從式（2)，開孔數係可以下述（3)定義。 式（3)開孔數=擠出量（kg/h)/[切刀片數父切刀旋轉 數（rph)xl粒質量（kg/個）] 從式（1)及式（3)，開孔率係可以下式（4)算出。 式（4)開孔率（E)=開孔數/全擠出噴嘴數χ1〇〇(%)= [Q/(NxRx60x(M/100)/l〇〇〇)]/Hxl〇〇(%) [Q為擠出量（kg/h) ’N為切刀的片數，R為切刀旋轉數 (rpm)，Μ為100粒質量（g)(從發泡性粒子選擇任意的1〇〇 粒’以最小刻度0. 0001 g之電子天秤計量之值作為1 〇〇粒 321804 25 201038383 質量），Η表示鎊模之全噴嘴數] <開孔率之評估基準> 開孔率（Ε)係以如下之基準進行評估。 © ： 50%^Ε 〇 ： 40%^Ε<50°/〇 Δ · 30%^Ε<40% x : Ε<30% 。 <發泡性粒子之空隙觀察> 以剃刀刃切斷於實施例1及比較例2得到的發泡性粒 子，使其切斷面以掃描型電子顯微鏡（曰立製作所公司製， S-3000N)擴大至70倍而攝影，觀察粒子内之空隙。 第6圖係於本發明之實施例1所製造的發泡性聚苯乙 烯系樹脂粒子之截面放大影像。第7圖係於比較例2所|g 造的發泡性聚苯乙晞系樹脂粒子之截面放大影像。 <發泡成形體之製造> 如前述，首先，使於擠出第48小時所得到之發泡性聚 苯乙烤糸樹脂粒子在2 0 °C下放置1日。其後，相對於發、、包 性聚苯乙烯系樹脂粒子100質量份’添加硬脂肪酸辞〇 J 質量份、羥基硬脂酸三甘油酯0· 05質量份、硬脂醆單甘油 醋0. 0 5質量份，進行混合而被覆於樹脂粒子表面。其後， 投入於小型批式預備發泡機（内容積40升），一邊授掉，一 邊藉吹入壓0.05MPa(壓力計壓）的水蒸氣進行加熱，製作 體發泡倍數50倍（體密度0. 02g/cm3)之預備發泡粒子。 繼而’使所得到之預備發泡粒子在23°c下熟成i日 321804 26 201038383 其後’使用自動成形機（積水工機製作所製，ACE-3SP型）， 而該自動成形機係安裝有以外形尺寸3〇〇χ4〇Οχιοο廳(肉厚 30丽）於内部具有肉厚5mm、10mm、25nmi之中分隔部的模具； 以下述成形條件成形預備發泡粒子，得到發泡倍數5 〇倍 (密度〇. 02g/cm3)之發泡成形體。 成形條件（ACE-3SP，QS成形模式） 成形洛氣壓 0. 0 8ΜΡει(墨力計壓） 模具加熱 3秒 .一者加熱（壓力設幻(壓力計壓） 另一者加熱 2秒 兩面加熱 12秒 水冷卻1〇秒 設定取出面壓0. 〇2MPa <預備發餘子之财填紐卿估基準〉 藉目視觀察上述發泡成开彡 〇 下述之評估。 崎體，有關模具填充性實施如 @:充分填充至肉厚 〇：可看出肉厚5咖 俱形成中分隔部。 5mm中分隔部分。 中分隔部分之填充非常過大發泡粒， 二==:::可看物真充不良造成之粒子 不良’完全未形成中分隔部。 χ :肉厚5mm中分隔部係充填 <雜子100倍之合計質量〉 子中，任意選痒之粒子100 在發泡性聚笨乙烯系樹脂教 321804 27 201038383 粒的合計質量以0. 02至0. 09g的範圍為佳，粒子100粒的 合計質量超過0. 09g時，於成形模具細部之填充變困難。 其結果，可形成之模具有可能被限定於單純形狀者。另外， 粒子100粒的合計質量少於0. 02g時，粒子之生產性有可 能差。亦即，在粒子100粒的合計質量中，更佳之範圍為 0. 04至0. 06g。又，聚苯乙烯系樹脂以外之樹脂係於上述 範圍乘樹脂之比重的值，成為較佳之粒子100粒的合計質 量範圍。 <預備發泡粒子之體發泡倍數的測定方法> 使充分乾燥之預備發泡粒子於量筒（例如500ml容量） 内，使用漏斗而自然落下。其後，至預備發泡粒子之容積 成為一定為止，振碰量筒之底而填充預備發泡粒子。測定 此時之預備發泡粒子的容積與質量，依下述（5)算出預備發 泡粒子之體發泡倍數。又，容積係以1 mL單位讀取，質量 以最小刻度0. 〇lg之電子天秤測定。聚笨乙烯系樹脂之樹 脂比重定為1.0而計算，體發泡倍數四捨五入小數點以下 1次方。 式（5) 體發泡倍數（倍）=預備發泡粒子之容積（mL)/ 預備發泡粒子之質量（g)X樹脂比重 <發泡成形體之發泡倍數的測定方法> 從已充分乾燥之發泡成形體，切出測定用試驗片（例 300x400x30丽），測定此試驗片之尺寸與質量。以此測定之 尺寸作為基礎而算出試驗片之體積，依下式（6)算出發泡成 形體之發泡倍數。又，聚苯乙烯系樹脂之樹脂比重為1. 〇。 28 321804 201038383 式（6) 發泡倍數（倍）=試驗片體積（cm3)/試驗片質量 (g)x樹脂比重 <維卡軟化點之測定方法> ‘ 使用東芝機械公司製射出成形機（IS-80CNV)，以缸筒 溫度220 C成形I2.7mmx64mmx6.4mm尺寸的試驗片。使用 此試驗片，依據JISK 7206,以荷重50N之條件測定（單位： °〇 ° ^ 〈強度之評估〉 〇 以JISA 9511 : 2006「發泡塑膠保溫材」記載的方法， 測定彎曲強度。亦即，使用Tensilon萬能試驗機UCT-10T (Orientech公司製）’使試驗帶尺寸為75mmx300mmx30mm， 壓縮速度為l〇mm/分，前端治具為加壓楔l〇R及支撐台 10R，支點間距離為200mm而進行測定，藉次式（7)算出彎 曲強度。試驗片之數目為3個，求出其平均值。 式（7)彎曲強度（MPa)=3FL/2bh2 〇 [F表示彎曲最大荷重（N)，L表示支點間距離（mm)，b表示 試驗片之寬(mm) ’ h表示試驗片之厚度（mm)]又，就彎曲強 度之評估’使彎曲強度之值為〇.28MPa以上作為〇，小於 0. 28MPa 作為X。 29 321804 201038383 [表l ]G (Step 1) The thermoplastic resin is supplied from the supply hopper 21 to the extruder 2 having the granulated ruthenium mold, and is melted and kneaded. (Step 2) - The thermoplastic resin is moved toward the granulation casting mold 1, and the foaming agent is injected into the thermoplastic resin from the blowing agent supply port 22 by the high pressure pump 23. That is, the foaming agent-containing resin 20 is formed by mixing a foaming agent with a thermoplastic resin. S ' (Step 3) The resin 20 containing the blowing agent is sent from the front end of the _ 2 through the mold base 11 to the resin flow path 14 of the mold body 10. (Step 4) The foaming agent-containing resin conveyed through the resin flow path 14 is ejected from each of the nozzles which are opened in the resin extrusion surface 13 of the mold body 355. Squeeze (Step 5) from each The resin containing the foaming agent extruded from the nozzle 15 is rotated in the water flow of the cavity 4 (in the cooling medium) by the rotary knife of the boring cutter 3, 祷 granulation of the resin 20 containing the foaming agent 1〇Cut ^ : Compared with the resin containing 2B of foaming agent, the temperature is high and U5t = j range, so that each electric heating tube can be controlled by _fi. In this way, the temperature control of the line =: 321804 17 201038383 body, and the temperature of the circulating water is adjusted to 1〇 to 6〇〇c by means of hot cut in water. . Further, the temperature of the molten resin refers to the temperature of the blowing agent-containing resin 20 from the die holder 2 of the extruder. In the present embodiment, the temperature of the molten resin is measured in the second temperature measuring body 19B, and the temperature of the mold body 1 () is set to be higher than that of the molten tree furnace (9) 115. 〇 to 20 ° ° C, preferably high 1203⁄4 to ι8 (Γ (: 曰 high degree i2 〇 ° C to 18 (TC temperature control. By this, in the water ^ good system foaming In the thermoplastic resin particles, the foamable thermoplastic resin particles of the small particles can be continuously produced. Further, when the conditions are carried out under the above conditions, the voids in the obtained foamable thermoplastic resin particles are reduced, thereby improving The mechanical strength of the foamed molded article produced by molding the foamable thermoplastic resin particles in the form of a mold and a package. The temperature of the cast mold body is less than the temperature of the molten resin + 丨^7, and the continuous foaming thermoplastic resin is continuously emulsified. When the particles are clogging, the pressure of the resin in the mold body fluctuates, and as a result, it is impossible to continuously produce the foamable thermoplastic resin particles having the same true diameter and the same diameter. The voids in the cross section are increased. As a result, the mechanical strength of the foamed molded article obtained by in-mold foam molding of the expandable thermoplastic resin particles may be lowered. When the resin temperature is +20 CTC, the obtained foamable thermoplastic resin particles are slightly foamed. As a result, it is impossible to rapidly produce small particles having uniform particle diameters. The temperature of the circulating water of the aromatic cooling medium is less than 10 °C. When the temperature of the circulating water is more than 6GX: The cut = tree plate cooling becomes insufficient. As a result, the difficulty of microfoaming of the resin particles is preferably 2%. The range of 水 to 4 〇. The range of 〇, preferably 25 C to 35 ° The range of C. The foaming agent-containing tree 20 which is cut into a granular form in the cavity 4 is a spherical foaming hot dragon tree. The foaming resin particle ο ΐ! ^IL is transferred to the dehydration treatment unit 8 in the official road 5. Here, the foamable thermoplastic resin particles are separated by % water, dehydrated, and dried, and the water that has been separated from the knife is sent to the water tank 7. The dehydration treatment unit 8 is separated, and the defoamed and dried foamable thermoplastic resin particles are sent to the container 9 to be collected. It is contained in the container. The foaming agent is not limited. For example, it can be used alone or in combination of two or more types, such as Zhengjie, isoprene, cyclopentanone, and pentylene. In particular, the pentane type is used as a main component and is mixed with n-butyl sulphate, isobutyl sulphate, or propyl bromide. In particular, pentane is suitable for use in foaming when it is extruded from a nozzle into a water stream. Authentic tree traces refer to those contained in thermoplastic resins; roads & formed light-like, preferably fine-grained, spherical resin particles. ^ ==,,, plastic resin particle system can be used for the desired (four) shape First, the foamable thermoplastic resin particles are preliminarily heated by heating from the crucible. The pre-expanded particles are placed in a molded melamine of a cavity of a shape. The steam is heated and the 4 preliminary foamed particles are connected to each other. Thereafter, a foamed wax-shaped molded body of a shape of 321804 19 201038383 can be produced by demolding. As described above, in the present invention, in the case where the foamable thermoplastic resin particles are produced by hot cutting in water, the temperature of the mold body is 115° higher than that of the foamed sword tree I melting tree [to 2G (TC range) By the method of controlling the temperature, the foamable thermoplastic resin particles can be obtained, whereby the foamable thermoplastic resin particles having a small particle size and uniform particle diameter can be continuously produced. Further, the foamable thermoplastic resin particles obtained by the present invention are The voids in the inside of the particles are reduced. Thereby, the mechanical strength of the foamed molded article obtained by subjecting the obtained foamable thermoplastic resin particles to in-mold expansion molding can be improved. The detailed production conditions in the production method of the present invention, It can be appropriately set depending on the kind of the resin to be used, but preferred manufacturing conditions can be exemplified as follows. (1) The diameter of the mold body 1 〇n nozzle 15 is preferably in the range of 0.2 mm to 2.0 legs, preferably 〇3 coffee to The range of 1 〇 is more preferably 0.4 to the range of 0·7 mm. (2) The particle size of the foamable thermoplastic resin particles obtained is preferably in the range of 0.3 to 2.0, preferably 〇5 to 14_ In the range of 0.7 mm to 1.2 Å, the foaming thermoplastic resin particles are foamable polystyrene resin particles, and the average molecular weight Mw of the polystyrene resin particles is preferably 120,000. The range of 4 to 10,000, more preferably in the range of 120,000 to 270,000. (4) The content of the foaming agent in the foamable thermoplastic resin particles is preferably in the range of 1 to 1% by mass, preferably 3 to 8 by mass. The range of % is more preferably in the range of 4 to 6 mass%. (5) The blowing agent is preferably n-pentane, isopentane, or a mixture of pentane in any ratio. It is preferably in the range of isopentane·n-pental=1〇: 9〇 to 321804 20 201038383 80:20, more preferably isopentane: n-pentane=80··80 to 60:40. (6) The thermoplastic resin expanded particles obtained by preliminary foaming the expandable thermoplastic resin particles have an average cell diameter of from 30//Π1 to 500, preferably in the range of #m, preferably from 50/zm to 300/ The range of zm is more preferably in the range of 100/zm to 250/zm. As described above, in the method for producing the expandable thermoplastic resin particles of the present invention, The temperature of the mold body 10 is higher than the temperature of the molten resin by 115 ° C to 200 ° C, preferably by 120 ° C to 180 ° C. By this, the foaming property is produced by hot cutting in water. In the hand of the thermoplastic resin pellet, the foamable thermoplastic resin particles having a small particle size and uniform particle diameter can be continuously produced. Further, the continuous production means continuous foaming thermoplasticity at least 12 hours from the granulation, preferably 24 hours or more. According to the production method of the present invention, in the continuous production of 48 hours or more, the reduction in the open cell ratio of the continuous production nozzle is 50% or less, and the particle diameter change rate of the obtained expandable thermoplastic resin particles is obtained. 20% or less of expandable thermoplastic resin particles. Further, in the above preferred production conditions (1) to (6), the following effects can be obtained. (a) To obtain the same expansion ratio, the foaming dose can be reduced. (b) The decrease in foaming properties over time is small, and the life of the particles is long. (c) Excellent low-pressure moldability (the heating energy for obtaining the foamed molded body is small, and energy can be saved). (d) Have sufficient opportunity strength. (e) A foam forming ratio of 5 to 67 times can be obtained. Next, a modification of the embodiment of the present invention will be described. It will be explained based on the drawing. It is to be noted that the same reference numerals are given to the same members or components as those of the above-described embodiment, and the description thereof will be omitted. The resin flow of the modification shown in Fig. 5 which is different from the above-described embodiment 21 321804 201038383 will be described. The cross-sectional shape of the road 14 is formed into a shape of a trapezoidal shape, and a nozzle 15 of any of the early nozzles 15a, 15b, 15c, ... is provided in the range of the trapezoidal shape. The inclined faces 14a and 14b (straight line portions) on the periphery of the tree-shaped road are arranged to be slightly parallel to the longitudinal direction of the tubular electric tube 17. In the present modification, the slopes 14a and 14b of the resin flow path 14A constituting the trapezoidal cross section are equidistant with respect to the (four) electric heating pipe 17. Therefore, the area of the resin flow path which is uniformly heated by the cylindrical electric heating fl7 is increased, and is uniformly heated as compared with the difficult flow path of the circular surface, and the clogging of the nozzle can be further reduced. [Examples] [Example 1] In Example 1, the granulation apparatus τ shown in Fig. 1 was attached to the granulation casting mold shown in Fig. 2 and Fig. 3 to produce a foaming polystyrene. Thin eucalyptus moon particles. A granulation mold was attached to a single-axis extruder having a diameter of 90 mm (L/D = 35). The granulation mold used is provided with: eight nozzle units on the circumferential surface of the read-out surface (having a porous plate having 25 diameters 〇. 6 mm, lip length 3. 〇 的 nozzle), and passing resin Each of the resin flow paths of the nozzle unit on the side of the extrusion surface is held by both sides, and is arranged in a radial shape at a position where the depth of the electric heating tube (distance from the resin extrusion surface) is 15 and 1 is transverse to the circumference. Tube-type electric heating tube (diameter 12mm), thermal insulation 321804 22 201038383 loaded with the central part of the resin extrusion surface. Further, as shown in FIG. 2, the temperature measuring bodies i9A and 19B in which the plurality of branches are arranged are controlled in two regions of the circulating water flow person side of the fin mold body and the four branches of the circulating water flow electric heating tube. The temperature of the mold body (molding temperature of the mold) was maintained at 30 (TC.) The following procedure was carried out in the same manner as in Example 1. ("Step 1") Polystyrene resin (manufactured by Toyo Benzene Co., Ltd., trade name HRM10N) Vicat has a softening point temperature of 102. 〇 100 parts by mass of a tumbler type mixer is used to uniformly mix 0.3 parts by mass of the fine powder talc, and is supplied at a rate of 13 〇kg per hour. (Step 2) After setting the maximum temperature in the extruder to 22nd generation and melting the resin, 6 parts by mass of pentane (isopentane/n-pentane) is injected from the extruder to 100 parts by mass. =20/80 mixture) as a foaming agent. (Step 3) Continuously knead the resin and foaming agent in the extruder, and pass the molten resin containing the foaming agent to the mold base (the connection between the extruder and the mold body) And transported to the aforementioned mold body held at 3〇〇〇c. Step 4) Adhesively squeezing the molten resin containing the foaming agent in the chamber in which the cooling water of the TC is circulated, and sealing the high-speed rotary cutter having a 1Q piece in the circumferential direction to the mold to be per minute. The molten resin containing the foaming agent extruded is cut by 3300 times. (Step 5) The molten resin containing the foaming agent masked from the cooling water is separated and dehydrated and dried to obtain a spherical foamable polyphenylene. In the above procedure, the temperature of the molten resin in the mold base was 18 〇. (: The amount of the expandable polystyrene resin particles was 138 kg/h. The first hour of the broadcast began. 0%为为良好的质量为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为为。 。 。 。 。 。 。 。 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 When % is used, a good granulation condition can be maintained. That is, in this embodiment 1, the system can be It was confirmed that the stability was 48 hours or more and granulation was carried out. [Comparative Example 1] The same procedure as in Example 1 was carried out except that the temperature of the mold main body (molding holding temperature) was 220 ° C, and the extrusion amount was 138 kg / h, the spherical foamable polystyrene resin particles were obtained. The molten resin temperature of the mold base at this time was 180 ° C. In Comparative Example 1, 'the resin was introduced into the mold within 1 hour from the start of extrusion. The pressure of the part reached the upper pressure limit of the mold (25 MPa), so the extrusion was stopped. It could not be pressed for 1 hour, so it could not be evaluated. [Comparative Example 2] In addition to setting the temperature of the mold body to 29 (TC, the rest was In the same manner as in Example 1, about 138 kg/h of the masking amount was obtained to obtain a spherical expandable polystyrene tree. OMPa, the resin pellet after drying, 1 〇〇, the temperature of the resin in the resin introduction part of the granulation tungsten mold is 12. OMPa. The mass of the stand is 〇 446g, and the opening ratio of the mold is 86 〇%, which is a good granulation environment. The pressure at the resin introduction portion of the granulation recording film at the 48th hour from the start of extrusion is 13, OMPa. The quality of the resin particles after drying is 321804 24 201038383 0.0451g, and the opening ratio of the mold is 85.0%, which can maintain a good granulation environment. That is, it can be confirmed in Comparative Example 2 It is stable for 48 hours or more and can be granulated. In the production of the expandable polystyrene resin particles of Example 1 and Comparative Examples 1 and 2, and the obtained expandable polystyrene resin particles, the following items are carried out. The results are summarized and reported. The results are summarized in the table. <Opening ratio of mold> The opening ratio is defined by the following formula (1): 〇, formula (1) opening ratio (extrusion nozzle on the surface of the mold) Opening ratio at the time of extrusion) = number of openings / total number of nozzles of the mold Xl 〇〇 (%) The amount of extrusion is as follows ( 2) Defined. Formula (2) Extrusion amount (kg/h) = total mass of total foaming particles cut by a cutter per lhr = number of openings X number of cuts xl grain mass = open Number of holes X number of cutting blades X number of rotations of the cutter X1 grain mass 〇 From the formula (2), the number of openings can be defined by the following (3). Equation (3) Number of openings = amount of extrusion (kg/h) / [Number of cutting blades: number of parent cutter rotations (rph) xl grain mass (kg/piece)] From equations (1) and (3), the opening ratio can be calculated by the following equation (4). Rate (E) = number of openings / total number of extrusion nozzles χ 1 〇〇 (%) = [Q / (NxRx60x (M / 100) / l 〇〇〇)] / Hxl 〇〇 (%) [Q is extrusion Amount (kg/h) 'N is the number of cutters, R is the number of cutter revolutions (rpm), and Μ is 100 pellets (g) (choose any 1 pellet from the foaming particles) with a minimum scale 0. 0001 g electronic scale measurement value as 1 321 321 321804 25 201038383 mass), Η indicates the total number of nozzles of the pound model] < evaluation criteria for opening ratio > opening ratio (Ε) is as follows Benchmarks were evaluated. © : 50%^Ε 〇: 40%^Ε<50°/〇Δ · 30%^Ε<40% x : Ε<30%. <Void observation of foaming particles> The foamable particles obtained in Example 1 and Comparative Example 2 were cut with a razor blade, and the cut surface was enlarged to 70 times by a scanning electron microscope (S-3000N, manufactured by Konica Seisakusho Co., Ltd.), and the particles were observed. Fig. 6 is a cross-sectional enlarged view of the expandable polystyrene resin particles produced in Example 1 of the present invention. Fig. 7 is a cross-sectional enlarged image of the foamable polystyrene resin particles produced in Comparative Example 2. <Production of the foamed molded article> As described above, first, the expandable polystyrene resin particles obtained at the 48th hour of extrusion were allowed to stand at 20 ° C for 1 day. Then, with respect to 100 parts by mass of the hair and the polystyrene-based resin particles, the amount of the hard fatty acid is added as J mass%, the hydroxystearic acid triglyceride is 0.05 part by mass, and the stearin monoglyceride is 0. 0 parts by mass, mixed and coated on the surface of the resin particles. Then, it is put into a small batch type pre-foaming machine (40 liters of internal volume), and it is heated by blowing water of 0.05 MPa (pressure gauge pressure) while blowing, and the body expansion ratio is 50 times. Pre-expanded particles having a density of 0.02 g/cm3). Then, the obtained preliminary foamed particles were aged at 23 ° C, i. 321804 26 201038383, and then 'automatic molding machine (manufactured by Sekisui Engineering Co., Ltd., ACE-3SP type) was used, and the automatic molding machine was installed. The mold having a size of 3〇〇χ4〇Οχιοο (30 mils thick) has a mold having a partition portion of 5 mm, 10 mm, and 25 nm in thickness; the pre-expanded particles are formed under the following molding conditions to obtain a foaming ratio of 5 〇 ( Foamed molded body having a density of 〇. 02 g/cm 3 ). Molding conditions (ACE-3SP, QS forming mode) Forming Luo gas pressure 0. 0 8 ΜΡ ει (mold gauge pressure) Mold heating for 3 seconds. One heating (pressure setting magic (pressure gauge pressure) The other heating 2 seconds heating on both sides 12 Separate water for 1 〇 second to set the surface pressure to be removed 0. 〇 2MPa <Preparation of the surplus of the money to fill the New York estimate benchmarks > Visually observe the above-mentioned foaming into the following evaluation. Saki, about mold filling Implementation such as @: Fully filled to thick meat 〇: It can be seen that the thickness of the meat is 5 in the middle partition. 5mm middle partition. The middle partition is filled with too large foaming granules, two ==::: Poor particles caused by poor filling 'completely not formed in the middle partition. χ : The thickness of the partition is 5mm in the thickness of the partition. <100 times the total mass of the miscellaneous substance. In the sub-option, any optional itching particles 100 in the foaming polystyrene Resin teaching 321804 27 201038383 The total mass of the granules is preferably in the range of 0.02 to 0.09 g, and the total mass of the particles of 100 particles exceeds 0.09 g, which makes it difficult to fill the details of the forming mold. The mold may be limited to a simple shape. 01至0. 06克。 Further, polystyrene, the total mass of the particles is less than 0. 02g, the productivity of the particles may be poor. The resin other than the resin is a value of the specific gravity of the resin in the above range, and is a total mass range of 100 particles of the preferred particles. <Method for measuring the bulk expansion ratio of the preliminary expanded particles> Preparation for sufficient drying The particles are naturally dropped by using a funnel in a measuring cylinder (for example, a volume of 500 ml). Thereafter, until the volume of the preliminary expanded particles is constant, the bottom of the measuring cylinder is filled with the preliminary expanded particles. The preliminary expanded particles are measured at this time. For the volume and mass, the bulk expansion ratio of the pre-expanded particles is calculated according to the following (5). The volume is read in units of 1 mL, and the mass is measured by an electronic scale with a minimum scale of 0. 〇lg. The resin specific gravity of the resin is set to 1.0, and the bulk expansion ratio is rounded to the nearest decimal point. Formula (5) Volume expansion ratio (times) = volume of pre-expanded particles (mL) / quality of pre-expanded particles (g) X resin Specific gravity <Measurement method of expansion ratio of foamed molded article> From the foamed molded article which has been sufficiently dried, a test piece for measurement (for example, 300×400×30 丽) was cut out, and the size and mass of the test piece were measured. The volume of the test piece was calculated based on the size, and the expansion ratio of the foamed molded body was calculated according to the following formula (6). The specific gravity of the resin of the polystyrene resin was 1. 〇 28 321804 201038383 (6) Foam multiple (times) = test piece volume (cm3) / test piece mass (g) x resin specific gravity < method of measuring Vicat softening point > ' Using Toshiba Machine Co., Ltd. injection molding machine (IS-80CNV), using a cylinder The test piece of the size of I2.7 mm x 64 mm x 6.4 mm was formed at a cylinder temperature of 220 C. This test piece was measured according to JIS K 7206 under the conditions of a load of 50 N (unit: ° 〇 ° ^ <Evaluation of strength> 弯曲 The bending strength was measured by the method described in JISA 9511: 2006 "foamed plastic insulation material". Using Tensilon universal testing machine UCT-10T (manufactured by Orientech), the test strip size is 75mmx300mmx30mm, the compression speed is l〇mm/min, and the front end fixture is the pressure wedge l〇R and the support table 10R. The distance between the fulcrums is The measurement was carried out at 200 mm, and the bending strength was calculated by the following formula (7). The number of test pieces was three, and the average value was obtained. The bending strength (MPa) of the formula (7) = 3FL/2bh2 〇 [F represents the maximum load of bending ( N), L represents the distance between the fulcrums (mm), b represents the width of the test piece (mm) 'h indicates the thickness of the test piece (mm), and the evaluation of the bending strength 'the value of the bending strength is 〇.28 MPa or more As 〇, less than 0. 28MPa as X. 29 321804 201038383 [Table l]
實施例1 比較例1 比較例2 鑄模的構造 喷嘴 個 200 200 200 喷嘴内徑 mm 0· 6 0. 6 0. 6 模唇長度 mm 3. 0 3. 0 3. 0 擠出量 kg/h 138 138 138 發泡劑（戊烷） 質量份 6 6 6 熔融樹脂溫度 °C 180 180 180 鑄棋保持溫度 °c 300 200 290 循環水溫 r 30 30 30 循環水量 升/分鐘 280 280 280 循環水壓 MPa 0. 14 0. 14 0. 14 [第1小時] 鑄模壓力 MPa 10. 0 12. 5 開孔率（E) % 92. 0 在1小時以内 86. 0 (開孔數） (個） 184 鑄模耐壓上限 172 評估 ◎ (25MPa) ◎ [第48小時] 鑄模壓力 MPa 10. 3 13. 0 開孔率（E) % 90. 0 85. 0 (開孔數） (個） 180 170 評估 ◎ ◎ [第48小時] 100粒之質量 g 0. 0426 0. 0451 發泡性粒子體密度 kg/升 0. 60 0. 58 大粒子（粒徑1. 4mm以上） 0/ n i n r 之比率 U . 0 發泡性粒子内之空隙 〇 X 發泡粒子之模具填充性 ◎ ◎ 強度 MPa 0. 29 0. 26 評估 ◎ X 總合評估 ◎ X X 本發明之實施例1中係使鑄模本體之溫度（鑄模保持 30 321804 201038383 溫度）保持於較熔融樹脂溫度高12(rc dUUC而進行谨 轉，從造粒開始至48小時經過時點，鑄模壓力之上曰丨嗅 喷嘴之開孔率仍高（參照表1)。亦即，48小時以上之 運轉非常有可能。續 在實施例1中係相對於造粒開始1小時後之製造物1〇〇 粒的質量為0. 0417g，48小時後之製造物1〇〇粒的質量為 0. 0426g(參照表1)。亦即，連續運轉之製造物的質量增加 率小至2%左右。 〇 於實施例1所得到之發泡性聚苯乙烯樹脂粒子（泉肜 第6圖）係相較於比較例2所得到之樹脂粒子（參照第; 圖），粒子内之空隙（在第6圖及弟7圖中於粒子内可看到 之空隙）的數目少。 使於實施例1所得到之發泡性聚苯乙埽樹脂粒子預傷 發泡後，進行模内發泡成形所得到之發泡成形體係與比較 例2所得到者比較，表示有高的強度（參照表1)。 〇 然而，在比較例1中，使鑄模本體之溫度（鑄模保持溫 度）保持於較熔融樹脂溫度高2〇°C之200。(：而進行運轉。在 比較例1中，喷嘴會快速堵塞，同時從造粒開始在1小時 以内壓力上昇至鑄模耐壓上限，無法以後之運轉（參照表 1)。 又’在比較例2中，使鎊模本體之溫度（禱模保持溫度） 保持於較熔融樹脂溫度高ll〇°C之290°C而進行運轉。在比 較例2中，從造粒開始至48小時後，鑄模壓力之上昇.亦穩 定，噴嘴之開孔率亦高，連續運轉為可能。 31 321804 201038383 但，從造粒開始至48小時經過後，於比較例2所得到 之發泡性聚苯乙烯樹脂粒子，係相較於實施例1所得到之 樹脂粒子，1〇〇粒子之質量重達〇.〇45g，同時體密度降低， 成為略大粒之粒子。進一步，在比較例2中係粒徑1.4mm 以上之大粒子的比率高達0· 5%(在實施例1中為0. 1%) ’粒 徨參差不齊變大。 於比較例2所得到之發泡性聚笨乙烯樹脂粒子（參照 第7圖），係相較於實施例1所得到之樹脂粒子（參照第6 圖），粒子内之空隙變多。 使於比較例2所得到之發泡性聚笨乙烯樹脂粒子預備 發泡後’進行模内發泡成形所得到之發泡成形體係與實施 例1所得到者比較，顯示有低的強度。 [產業上之利用可能性] 若依本發明，在以水中熱切法之發泡性熱塑性樹脂粒 子的製造中，可抑制伴隨擠出時間的經過而有之鑄模小孔 的堵塞，可製造安定而小粒且均一之發泡性熱塑性樹脂粒 子。在本發明所得到之發泡性熱塑性樹脂粒子係藉由模内 發泡成形法發泡成形為各種形狀，可作為緩衝材或保溫材 等利用之發泡成形體的製造。 【圖式簡單說明】 第1圖係本發明之實施形態的造粒裝置之構成圖。 第2圖係表示本發明之實施形態的造粒用鑄模的概略 構成之側截面圖。 第3圖係表示第2圖之鑄模本體的樹脂擠出面的側面 32 321804 201038383 圖。 第4圖係表示喷嘴之配置狀態的一例子圖。 第5圖係表示有關本發明之實施形態的變形例之喷嘴 1 的配置狀態的一例子圖。 第6圖係本發明之實施例1所製造之發泡性聚苯乙烯 系樹脂粒子之截面放大影像。 第7圖係比較例2所製造之發泡性聚苯乙烯系樹脂粒 子之截面放大影像。 【主要元件符號說明】 1 造粒用每核 2 擠壓機（樹脂供給裝置） 3 切刀 4 腔體 5 管路 6 送水泵浦 7 水槽 8 脫水處理部 9 容器 10 鑄模本體 11 模座 12 螺栓 13 樹脂擠出面 14、 14A 樹脂流路 14a > 14b斜面（直線部） 15 喷嘴 16 隔熱材 17 筒型電熱管 18 短電熱管 19A 、19B 測溫體 21 送料斗 22 發泡劑供給 23 壓泵浦 T 造粒裝置 33 321804Example 1 Comparative Example 1 Comparative Example 2 Construction of a mold Nozzle 200 200 200 Nozzle inner diameter mm 0·6 0. 6 0. 6 Lip length mm 3. 0 3. 0 3. 0 Extrusion amount kg/h 138 138 138 blowing agent (pentane) parts by mass 6 6 6 molten resin temperature °C 180 180 180 casting chess holding temperature °c 300 200 290 circulating water temperature r 30 30 30 circulating water volume / minute 280 280 280 circulating water pressure MPa 0. 14 0. 14 0. 14 [1st hour] Molding pressure MPa 10. 0 12. 5 Opening ratio (E) % 92. 0 Within 1 hour 86. 0 (number of openings) (piece) 184 Mold Upper pressure limit 172 Evaluation ◎ (25MPa) ◎ [48th hour] Molding pressure MPa 10. 3 13. 0 Opening ratio (E) % 90. 0 85. 0 (Number of openings) (set) 180 170 Evaluation ◎ ◎ [48th hour] Mass of 100 grains g 0. 0426 0. 0451 Foaming particle density kg / liter 0. 60 0. 58 Large particles (particle size 1. 4mm or more) 0 / ninr ratio U. 0 hair Mold filling in the foaming particles 〇X The filling of the foaming particles ◎ ◎ Strength MPa 0. 29 0. 26 Evaluation ◎ X Total evaluation ◎ XX In the first embodiment, the temperature of the mold body (the mold is maintained at a temperature of 30 321804 201038383) is maintained at a temperature 12 (rc dUUC) higher than the temperature of the molten resin, and is rotated from the start of granulation to 48 hours, above the mold pressure. The opening rate of the sniffer nozzle is still high (refer to Table 1). That is, the operation of 48 hours or more is very likely. Continued in Example 1 is the production of 1 granule after 1 hour from the start of granulation. The mass of the product is 0. 0417g, and the mass of the manufactured material after 48 hours is 0. 0426g (refer to Table 1). That is, the mass increase rate of the continuously running product is as small as about 2%. The foamable polystyrene resin particles obtained in 1 (Fig. 6 of the spring) are compared with the resin particles obtained in Comparative Example 2 (see Fig. 1), and the voids in the particles (in Fig. 6 and the younger brother 7) In the figure, the number of voids which can be seen in the particles is small. The foamed polystyrene resin particles obtained in Example 1 are pre-injured and foamed, and then foamed by in-mold expansion molding. The system is compared with the one obtained in Comparative Example 2, indicating that there is high strength (refer to Table 1). ). 〇 However, in Comparative Example 1, the temperature of the mold body (molding mold holding temperature) was maintained at 200 °C higher than the temperature of the molten resin. In the first comparative example, the nozzle was quickly clogged, and the pressure was raised to the upper limit of the mold pressure within one hour from the start of granulation, and it was impossible to operate later (see Table 1). In the middle, the temperature of the body of the pound mold (the temperature of the prayer mold was maintained) was maintained at 290 ° C higher than the temperature of the molten resin. In Comparative Example 2, the mold pressure was from the start of granulation to 48 hours later. The rise is also stable, and the opening ratio of the nozzle is also high, and continuous operation is possible. 31 321804 201038383 However, the expandable polystyrene resin particles obtained in Comparative Example 2 after the granulation started, after 48 hours passed, Compared with the resin particles obtained in Example 1, the mass of the ruthenium particles was as high as 〇45 ,, and the bulk density was decreased to become particles of slightly larger particles. Further, in Comparative Example 2, the particle diameter was 1.4 mm or more. The ratio of the large particles is as high as 0·5% (0.1% in Example 1). The unevenness of the granules is large. The foamable polystyrene resin particles obtained in Comparative Example 2 (see the seventh) Figure), compared to the resin particles obtained in Example 1. Referring to Fig. 6), the voids in the particles were increased. The foamed molding system obtained by performing in-mold expansion molding after preliminary foaming of the foamable polystyrene resin particles obtained in Comparative Example 2 and Examples In comparison with the one obtained, it is shown that the strength is low. [Industrial Applicability] According to the present invention, in the production of the foamable thermoplastic resin particles by the hot cutting method in water, the passage of the extrusion time can be suppressed. The clogging of the small holes of the mold can produce stable, small-sized and uniform foamable thermoplastic resin particles. The foamable thermoplastic resin particles obtained in the present invention are foam-formed into various shapes by in-mold expansion molding. It can be used as a foaming molded body for use as a cushioning material or a heat insulating material. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a configuration diagram of a granulating apparatus according to an embodiment of the present invention. Fig. 2 is a view showing the implementation of the present invention. Fig. 3 is a side cross-sectional view showing a schematic configuration of a mold for granulation in a form. Fig. 3 is a side view showing a side surface of a resin extrusion surface of a mold body of Fig. 2, 32 321804, 201038383. Fig. 4 is a view showing a state of arrangement of nozzles. Fig. 5 is a view showing an example of an arrangement state of a nozzle 1 according to a modification of the embodiment of the present invention. Fig. 6 is an expanded polystyrene system produced in Example 1 of the present invention. Fig. 7 is a cross-sectional enlarged image of the expandable polystyrene resin particles produced in Comparative Example 2. [Explanation of main component symbols] 1 granulation per core 2 extruder (resin supply) Device) 3 Cutter 4 Cavity 5 Pipe 6 Water pump 7 Water tank 8 Dehydration treatment unit 9 Container 10 Mold body 11 Mold base 12 Bolt 13 Resin extrusion surface 14, 14A Resin flow path 14a > 14b Bevel (straight line 15 nozzle 16 heat insulation material 17 tubular electric heating tube 18 short electric heating tube 19A, 19B temperature measuring body 21 feeding hopper 22 blowing agent supply 23 pressure pumping T granulator 33 321804