200916294 九、發明說明： 【發明所屬之技術領域】 本發明係關於以熱切法（hot cut method)為了成形熱 塑性樹脂的粒子所需之造粒用模具（dies)及造粒裝置，尤 其關於可防止噴嘴（nQzzle)阻塞，可有效率地生產粒徑均 勻：粒子之以粒用杈具及造粒裝置。本發明另關於使用前 述模具之發泡性熱塑性樹脂粒子之製造方法。 本案係根據2007年2月23曰在曰本申請之特願篇一 43927號而主張優先權，在此援用該案之内容。 【先前技術】 用末成形熱塑性樹脂之顆粒（Pellet)的裝置（稱為造 粒機（pelletizer))為周知的I W冉為u 置此裝置一般係具備擠製 機如他〇、安褒於該擠製機的前端之模具（dies)、及 切斷益（cutter)而構成，且係条丨田 ,,^ ώ 成 係利用擠製機將經過熔融混練 的樹月曰材料自模具擠出，並用 造所希望大小之顆粒。 斷㈣擠出物切斷’而製 將自模具的噴嘴播出的樹脂材料切斷之方法 熱切法及冷切法（coldcutraethorH。、人、/ 已知有 喷嘴样出的於f浐鉍料、曾 々切法係將從模具的 ‘出樣曰材枓導入水槽中冷卻而成 佼加以切斷之方法。另一方 nd)狀 開口之握且-#二/ ”、、切去係使有複數個喷嘴 開口之換具病面與循環的水流 水流中擠出之高溫樹脂切斷 並以切_剛在 粒，因係在樹脂未充分硬化 …刀法進仃之以 冷切法的缺點之樹脂粉體化。同時^斷’因此不會發生 M熱切法進行之造粒， 319991 200916294 lb 還具有可得到球狀的粒子等優點。 不過，熱切法中由於模具的樹脂排 -因此水流側會從樹脂排出 、U妾觸’ =;π融點以下之情形。結果，會發生喷嘴阻 降低。即使沒有發生嘴嘴阻塞的情 二致，：tΐ嘴口徑變小的情形，而發生顆粒的粒徑不 得可：致二質降低。再者’阻塞變多，樹脂的擠出就變 r、署二：，堡力會變得異常地高，會對模具的上 置，例如擠製機等造成不良的影響。 萝 防止利文獻1 I4中揭示的技術曾經提出作為: 技術。、切法進行造粒所用的造粒用模具中的噴嘴阻塞之 專利文獻1中揭示：在模具内各流路的中心設 加熱器，並與各流路對應而分別配設複數個喷嘴， 勻加熱喷嘴之方式的造粒用模具。 I利文獻2中揭示：在以旋轉切斷器切斷從模且擠 彳溶融樹脂而得到樹脂粒子之熱塑性樹脂粒子的製造方法 2 ’以使用I面隔熱的模具為特徵之熱塑性樹脂粒子的制 造方法。 衣 專利文獻3、4為本案申請人曾提出專利申請之發明， 此兩專利文獻中揭示：以不在位於水流的流入方向及x流 方向上的區域、以及位於與水流的流入方向及流出方向垂 2方向上的區域形成喷嘴，在該等區域設置用以加熱樹 曰抓路内的柄脂之熱媒流路作為特徵之造粒用模具。 319991 6 200916294 (專利文獻1)日本特開平7-1 78726號公報 (專利文獻2)日本特開平5-301218號公報 (專利文獻3)國際公開W02004/080678號公報 (專利文獻4)國際公開W02005/028173號公報 【發明内容】 (發明所欲解決之課題） 然而，專利文獻1至4中揭示的先前技術具有如下 述之問題。 專利文獻1中揭示的先前技術，係以使棒狀加熱器的 則端與模具的樹脂排出面接近的方式配置棒狀加熱器，然 而棒，加熱器在構造上並無法將鎳鉻合金（nichrome)線言^ 置到前端部，因此加熱器前端部並不發熱。因此，就此 具構造而言’报難對最需要加溫之模具前端部的樹脂排出 面進行充分的加溫，無法完全防止阻塞。另外，由於 在模具設置複數個圓形樹脂流路，因此有構造複雜且模^ 的製作成本變高等問題。 /、 、專利文獻2中揭示的先前技術’係以製造並未混合發 泡劑之早純的樹脂顆粒為前提，與如同本發明之混合 =劑之熱塑性樹脂（發泡性熱塑性樹脂粒子)之造粒技術^ =性熱塑性樹脂粒子的情況，與單純之樹脂顆粒的 抑制粒子之發泡，因此需要將猶環水的溫 :。 下口此’樹脂溫度與循環水溫度的差變 :::隔熱材並無法抑制水流從模具的前端部奪走孰 此’使得喷嘴之阻塞變得容易發生。此外，在發泡=塑 319991 7 200916294 性樹脂粒子的製造中，樹脂會因為發泡劑而軟化，所以必 須使切斷器的刀刃與模具表面接觸（壓抵在模具表面）而切 斷排出的樹脂。如專利文獻2所揭示之以隔熱材覆蓋表面 之拉具構造，隔熱材會因切斷器的刀刀摩擦而在短時間内 磨耗’因此模具的耐久性會有問題。 專利文獻3、4中揭示的技術，係藉由不在位於水流的 流入方向及流出方向上的區域、以及位於與水流的流入方 向及机出方向垂直的方向上的區域形成嘴嘴，冑由在該等 區域設置用以加熱樹脂流路内的樹脂之熱媒流路，使得喷 嘴的阻塞不易發生，而可改善發泡性熱塑性樹脂粒子的生 產性。+然而，此方法必須要有熱媒體之加熱循環裝置以及 通往模具之配管，有設備成本變高之問題。此外，還有為 Z使高溫之油等的熱媒體不漏出，檢查保養的成本也會變 南之問題。 本4明係有鑑於上述課題而完成者，其目的在提供一 種可防止熱切法所用的造粒用模具中的噴嘴阻塞，而可有 效率地生產粒徑均勻的粒子之造粒用模具。 (解決課題之手段） 為了達成前述目的，本發明提供一種造粒用模具，具 備有.與水流接觸而設置之樹脂排出面、以及與擠製機之 缸筒（c y 1 i n d e r)相連通而在前述樹脂排出面開口之複數個 噴嘴（nozzle)，前述喷嘴係沿著前述樹脂排出面上的假想 圓的圓周而配置’且在配置前述噴嘴之圓周内侧的樹脂排 出面 <，卩to熱材，在樹脂排出面的附近以通過前述圓周的 8 319991 200916294 中心部而延伸科側的方式設有複數個1式加熱器 (cartridge heater) ° 本發明之造粒用模具中，較佳者4，前述管式加熱器 係沿著前述肖脂排出面之前述水流的流入方向及流出方 向、以及與前述水流的流入方向及流出方向垂直之方向而 一此外，本發明之造粒用模具中’較佳者為，具備有與 則述㈣機之缸筒相連通且連結至前述喷嘴之複數個樹脂 流路，前述樹脂流路係沿著前述樹脂排出面上的假想圓的 ，周而配置，前述管式加熱器係相對於前述樹脂流路配置 =述圓周的周方向兩側，且以長度方向向著前述 徑向而橫切過前述圓周之狀態來配置。 此外，本發明之造粒用模具中，較佳者為，前 力:熱㈣加熱器深度(亦即從樹脂排出面到管式加熱器: 中心部的距離）為1〇至50mm。 、 另外，本發明提供一種造粒裝置， ：& 相關之造粒用模具；前端安梦古义 H} ^發明 機;以及收容用以將自前述造粒用模二用製 ::r:器;並且使前述造粒用模具之樹==: *接觸之腔室（chamber)。 ，、木 另外，本發明提供-種發泡性熱塑性樹脂_ 方法，具有：將熱塑性樹脂供給至安事 衣乂 粒用模具之播製機，使溶融混練之步驟；二二日:：造 性樹脂向著前述造粒用模具移動—邊將發泡劑注 319991 9 200916294 ' 成含有發泡劑的樹脂之步驟；以及在水流中 -泡劑的：;述造粒用模具之噴嘴排出的前述含有發 柳月“刀斷而得到發泡性熱塑性樹脂粒子之步驟。 ’本發明提供一種熱塑性樹脂發泡粒子之製造方 用料熱塑性樹脂供給至安裝有前述本發明之造粒 !機’使之_昆練之步驟…邊使前述熱塑 询性丄匕:則迷造粒用模具移動一邊將發泡劑注入前述熱 Γ、二==形成含有發泡劑的樹脂之步驟；在水流中利用 劑：前述造粒用模具之喷嘴排出的前述含有發泡 ::;Γ到發泡性熱塑性樹脂粒子之步驟；以及預備 子^= 熱塑性樹脂粒子而得到熱塑性樹脂發泡粒 本發明提供—種熱塑性樹脂發泡成形體之製造 粒用rl被將熱塑性樹脂供給至安裝有前述本發明之造 u擠製機，使之炫融混練之步 、=向著前述造粒用模具移動-邊將發泡200916294 IX. Description of the Invention: [Technical Field] The present invention relates to a dies and a granulation device for granulation required for forming a particle of a thermoplastic resin by a hot cut method, and particularly relates to prevention The nozzle (nQzzle) is blocked, and the particle size can be efficiently produced: the particles are used for the cooking utensils and the granulator. The present invention further relates to a method for producing foamable thermoplastic resin particles using the above mold. This case claims priority based on the special request No. 43927 of the application of this application on February 23, 2007. The content of the case is hereby referred to. [Prior Art] A device (called a pelletizer) for forming a pellet of a thermoplastic resin (referred to as a pelletizer) is a well-known IW, which is generally provided with an extruder such as an extruder and an ampoule. The dies of the front end of the extruder and the cutters are formed, and the stalks are smashed, and the 树 系 system uses the extruder to extrude the melted and kneaded tree sap material from the mold. And use the particles of the desired size. The method of cutting off the resin material that is ejected from the nozzle of the mold by the cutting of the extrudate, and the cold cutting method (coldcutraethor H, human, / known nozzles, The method of the cutting method is to cut the mold from the mold into the water tank and cut it into a water tank. The other side nd) has an open grip and -#二/", and the cut system has a plurality of The nozzle surface of the nozzle is cut off from the high temperature resin which is extruded in the circulating water stream, and is cut in the grain, because the resin is not sufficiently hardened... the resin is disadvantageous in cold cutting. Powdering. Simultaneously breaking 'There is no granulation by M-cutting method, 319991 200916294 lb also has the advantage of obtaining spherical particles. However, in the hot cutting method, due to the resin row of the mold - the water flow side will Resin discharge, U 妾 touch ' =; π melting point below. As a result, the nozzle resistance will decrease. Even if there is no mouth clogging, the diameter of the granule will decrease. Nothing: the second quality is reduced. The extrusion of the resin will change, and the second one: the force will become abnormally high, which will adversely affect the topping of the mold, such as the extruder. The technology disclosed in the literature 1 I4 Patent Document 1 discloses a technique in which a nozzle in a granulation mold for granulation is cleaved by a cutting method, and a heater is provided in the center of each flow path in the mold, and is disposed corresponding to each flow path. A granulation mold in which a plurality of nozzles are used to uniformly heat the nozzles. Ili Document 2 discloses a method for producing thermoplastic resin particles obtained by cutting a molten resin from a mold and extruding a molten resin to obtain resin particles. A method for producing a thermoplastic resin particle characterized by using a mold having an I-side heat insulation. Patent Literatures 3 and 4 are the inventions of the patent application filed by the applicant, and the two patent documents disclose that the water flow is not in the flow direction and a region in the x-flow direction and a region in the direction perpendicular to the inflow direction and the outflow direction of the water flow form a nozzle in which a heat medium for heating the handle grease in the tree trunk is provided. Japanese Patent Laid-Open No. Hei 5-301218 (Patent Document 3) International Publication No. WO2004/080678 (Patent Document 4) International Publication No. WO2005/028173 (Summary of the Invention) However, the prior art disclosed in Patent Documents 1 to 4 has the following problems. The technique is to arrange the rod heater so that the end of the rod heater is close to the resin discharge surface of the mold. However, the rod and the heater are not structurally capable of placing the nichrome wire to the front end. Therefore, the front end of the heater does not generate heat. Therefore, in terms of this structure, it is difficult to sufficiently heat the resin discharge surface of the tip end portion of the mold which is most heated, and it is impossible to completely prevent clogging. Further, since a plurality of circular resin flow paths are provided in the mold, there are problems in that the structure is complicated and the manufacturing cost of the mold is increased. The prior art disclosed in Patent Document 2 is based on the premise that the resin particles of the present invention are mixed with the thermoplastic resin (foaming thermoplastic resin particles) of the present invention. In the case of the granulation technique ^ = thermoplastic resin particles, and the simple resin particles inhibit the foaming of the particles, it is necessary to adjust the temperature of the water. The difference between the resin temperature and the circulating water temperature is ::: The heat insulating material does not inhibit the flow of water from the front end portion of the mold. This makes the nozzle clogging easy. In addition, in the production of foaming = plastic 319991 7 200916294 resin particles, the resin is softened by the foaming agent, so the blade of the cutter must be brought into contact with the surface of the mold (pressed against the surface of the mold) to cut off the discharge. Resin. As disclosed in Patent Document 2, the structure of the holder having the surface covered with the heat insulating material causes the heat insulating material to be worn in a short time due to the friction of the cutter of the cutter. Therefore, the durability of the mold may be problematic. The techniques disclosed in Patent Documents 3 and 4 form a nozzle by not being in a region in the inflow direction and the outflow direction of the water flow, and in a region in a direction perpendicular to the inflow direction and the machine direction of the water flow. These regions are provided with a heat medium flow path for heating the resin in the resin flow path, so that the clogging of the nozzle is less likely to occur, and the productivity of the foamable thermoplastic resin particles can be improved. + However, this method requires a heat medium heating cycle device and piping to the mold, which has a problem that the equipment cost becomes high. In addition, there is a problem that the heat medium such as high-temperature oil does not leak out, and the cost of inspection and maintenance also becomes problematic. In view of the above-mentioned problems, the object of the present invention is to provide a granulation mold which can efficiently produce particles having uniform particle diameter by preventing nozzle clogging in a granulation mold used in the hot cutting method. (Means for Solving the Problem) In order to achieve the above object, the present invention provides a granulation mold comprising: a resin discharge surface provided in contact with a water flow, and a cylinder cy 1 inder connected to the extruder a plurality of nozzles opening the resin discharge surface, wherein the nozzles are disposed along a circumference of a virtual circle on the resin discharge surface and are disposed on a resin discharge surface inside the circumference of the nozzles. In the vicinity of the resin discharge surface, a plurality of type 1 heaters are provided so as to extend the branch side through the center portion of the above-mentioned circumference of 8 319991 200916294. In the granulation mold of the present invention, preferably 4, The tube heater is a direction perpendicular to an inflow direction and an outflow direction of the water flow and a direction perpendicular to an inflow direction and an outflow direction of the water flow along the cholester discharge surface, and the granulation mold of the present invention Preferably, the resin passage is provided with a plurality of resin flow paths connected to the cylinder of the fourth machine and connected to the nozzle, and the resin flow path is discharged along the resin. In the imaginary circle on the surface, the tubular heater is disposed on the both sides of the circumferential direction of the circumferential direction of the resin flow path, and is transversely cut across the circumference in the radial direction. Configuration. Further, in the granulating mold of the present invention, it is preferable that the front force: heat (four) heater depth (that is, the distance from the resin discharge surface to the tube heater: the center portion) is 1 〇 to 50 mm. In addition, the present invention provides a granulating device, a & granulation mold; a front end An Meng Guyi H} ^ invention machine; and a housing for use in the granulation mold:: r: And a chamber in which the aforementioned granulation mold tree ==:* is contacted. In addition, the present invention provides a foamable thermoplastic resin method comprising the steps of: supplying a thermoplastic resin to a seeding machine for using a mold for granules, and melting and kneading; 22nd day: Creativity The resin is moved toward the granulation mold--the step of injecting the foaming agent into the resin containing the foaming agent; and in the water stream-foaming agent: the above-mentioned content discharged from the nozzle of the granulating mold The step of obtaining a foamable thermoplastic resin particle by a knife is broken. The present invention provides a thermoplastic resin for producing a thermoplastic resin expanded particle, which is supplied to a granulation machine to which the above-described present invention is attached. The procedure of Kunming is to make the aforementioned thermoplastic 丄匕: the step of injecting the foaming agent into the heat enthalpy while moving the granules, and the step of forming a resin containing a foaming agent; and using the agent in the water stream The step of foaming: Γ 发泡 发泡 发泡 发泡 发泡 发泡 发泡 发泡 发泡 发泡 发泡 发泡 喷嘴 喷嘴 喷嘴 喷嘴 喷嘴 造 造 造 造 造 造 热塑性 造 造 造 造 造 造 造 造 造 造 造 造 热塑性 热塑性 热塑性 热塑性 热塑性In the production of a thermoplastic resin foamed molded article, the thermoplastic resin is supplied to the squeezing machine to which the above-described present invention is attached, and the step of smashing and kneading is carried out, and the granulation mold is moved to the granulation mold. bubble
用、二生=形成含有發泡劑的樹脂之步W =斷益切斷自前述造粒用模具之喷嘴排出的前述含有發 ，包蜊的樹脂而得到發泡性熱塑性樹脂 發泡性埶塑性榭浐朽辜1供找a 称’使剛述 土 ϋ樹絲子預備發泡而得到熱塑性樹脂發泡粒 形二=述熱塑性泡粒子在模内發泡成 于J…土 f生树脂發泡成形體之步驟。 子之1:方t發明提供一種依照前述發泡性熱塑性樹脂粒 衣4方法而得到之發泡性熱塑性樹脂粒子。 319991 10 200916294 k ' 料’本發明提供—種使前述發泡性 預備發泡而得到之熱塑性樹脂發泡粒子。 U日拉子 〜^外，本發明提供—種使前述熱塑性樹脂發泡粒子在 ’核内發泡成形而得到之熱塑性樹脂發泡成形體。 (發明之效果） 由於本發明之造粒用模具係沿著樹脂排出面上的假相 圓的圓周而配置嘖喈，Β — $ 〜 、 且在配置前述喷嘴之圓周内側的樹 周曰：！面Γ有隔熱材，在樹脂排出面的附近以通過前述圓 槿杰〜部而延伸到外側的方式設有複數個管式加熱器之 構成，因此喷嘴之阻荬雜政 土難以發生，可改善因阻塞而導致之 r產效率的降低，且可製造粒徑均勻之高品質的粒子。 【實施方式】 以下，參照圖式說明本發明。 弟1圖及第2圖係顯示本發明之一實施形態之圖。第 1圖係顯示造粒裝置的構成圖’第2A圖係造粒用模具的截 面圖，第2B圖係顯示該造粒用模具的樹脂排出面之側面 ^。此等圖中，符號1為造粒用模具，符號2為擠製機， 付號3為料斗（hopper)，符號4為發泡劑供給口，符號$ ^壓泵’符號6為腔室’符號7為切斷器，符號8為送 水泵，符號9為水槽，符號1〇為脫水處理 管路’符號12為容器，符號13為模座( — )，： 谠14為含有發泡劑之樹脂，符號15為螺才全，符號16為樹 腊流路，符號π為噴嘴，符號18及19為管式加熱器，符 遽20為短加熱器，符號21為隔熱材，符㉟μ為樹脂排出 Π 3J999] 200916294 ，符號L為加熱器深度(從樹 18、19的中心部之距離）。 囬“到s式加熱器 本貫施形態之造粒裝置的主要構成 •所不之造粒用模具！、前端安^該m 圖 機2、及使水流與造粒用模具！:果，、1之擠製 室6。腔室6收容有用以切斷自·造粒用曰模且：二接觸之腔 出的樹脂之切斷器7。此外，腔室6連接有用以H7排 流通之管路U，此管路Η的一端經由送水果 水槽9。管路U的另一端設有將發泡 循環水分離出來，並加以脫水、 广曰粒子攸 此脫水處理部10分離出來，並經過脫水、乾燥 塑性樹脂粒子係送到容器丨2。 *泡陡熱 在施^之造粒用模具卜係以複數個螺检15固定 2座13的削端侧，而該模座13係固定在擠製機2的前 。：造粒用模具1具備有··與水流接觸而設置之樹脂 排出面22、以及與擠製機2之缸筒相連通而在樹脂排出面 22開口之複數個噴嘴17。嘴嘴17係沿著樹脂排出面22 上的假想圓（圖中未表示）的圓周而配置，且在配置喷嘴P 之圓周内側的樹脂排出面22設有隔熱材21。另外，在樹 脂排出面22的附近以通過前述圓周的中心部而延伸到外 側的方式設有複數個管式加熱器18、]9。此外’在造粒用 模具1之比樹脂排出面22靠近擠製機2側的位置插入複數 個短加熱器20，使短加熱器2〇可連結至造粒用模具^的 喷嘴17之樹脂流路〗6進行加熱。 319991 12 200916294 • 在第2圖所示的例子中，< 少此 管式加熱器18、19, 叹树脂排出面22的附近之 -的徑向貫通模以而:置^過模具1的中心且沿著模具1 •著與管式加熱器心=根長形管式加熱器18、及沿 前端到達模具1的中、、、、向垂直之方向而設置且具有 組合成十字形而構附近，長度之兩根管式加熱器19 6内使水流與樹脂排二’加熱器18係沿著在腔室 、出面以之流下方向而水流相對於樹脂排 水流之流下方向垂直之方二19係沿著與前述 的附近之此等管式加熱器:置伟:::脂排出面22 脂排T…央部之隔熱材21的内=熱設於樹 用模具的大小或形狀”===力^器中因應造粒 用：將捲繞於例如棒狀陶究之用：官式加熱器可使 (耐熱不錄鋼管）t，並將私赦:…、士（鎖絡合金線）插入管 導性及古π缝卜線與官之間隙封裝入高熱傳 V及回巴緣性的材料_)而作成高功率密度（卿厂 有另外，加_8可為單側具 -根管式加熱器，亦可為兩側各具有 根卜線之官式加熱器（|肖式加熱器（sheathed =高=為單側具有兩根導線之管式加熱器的功 用於本實施形態之造粒 周知的各種隔熱材中適當地 耐水性且構造上表面硬度高 用模具1中之隔熱材21，可從 % #使用，但以使用特別具有 之隔熱材為佳。例如，以使用 319991 13 200916294 w -下述之隔熱材為佳，亦即使用：在造粒用模具1的内部側， 配》又即使與南、溫的模具接觸也不會發生變形等之耐熱性能 -及隔熱性能良好的隔熱材，並以隔熱性能良好的氟樹脂等b .的防水性樹脂加以覆蓋，再在樹脂排出面22侧依序積層不 銹鋼、陶竟等表面硬度高的材料而成之積層式的隔熱材 Z1 〇 在弟2圖所示的例子中，在造粒用模具i之樹脂排出 中：部配置隔熱材21 ’在樹脂排出面22的外侧則 2數個噴嘴17沿著前述假想圓的圓周而 ==117之樹輸面22的巾央料，係設成在 觸。前述假想圓之中，與配置成十字 “广U 18、19的配設位置重疊的位置，並不設置 喷嘴17。在本例中，喷嘴 个。又置 1 7祕。 、嗝1 7係幵/成為·將有多數個噴嘴 '圓周弧段上而成之噴嘴單元，在前述假相圓上成 穿β回 噴嘴7之配置方法並不限於此例。 對於顯示本發明之實施形態的變形例圖。以下， 貫ί形態相同或同樣的構材，部份使用相同的 ::::。$其巩明’針對與上述實施形態不同的構成進行 第6Α圖係造粒用握 粒用模具的樹脂排出面二截面圖’第6β圖係顯示該造 粒用槿呈μ? 側面圖。此等圖中，符號41為造 粒用权具，符號48 门〜 50C> 49 為 e 式加熱器，符號 50(50A、50B、 川C 50D)為熱電偶等 埶哭深产t手〜測概肢（》皿度感測器），符號L·為加 —冰度（㈣脂排出面㈡到管式加熱器价㈣中心部 319991 14 200916294 之距離）。 本具知形態之造粒用模具41，係具有設置成在腔室6 内與水流接觸之樹脂排出面22’且在配置複數個喷嘴17 (與擠製機2之缸筒相連通而在樹脂排出面22開口者)之圓 2内側的樹脂排出面2 2，設有隔熱材2卜另外，將以通過 月·J述0周的中心部而延伸到外侧的方式之複數個管式加敎 器“、49設置在樹脂排出面22的附近。此外，造粒用模 具41具備有與擠錢2之缸筒相連通且連結至噴嘴 複數個樹脂流路16，樹脂流路16係沿著樹脂排出面^上 的假想圓（未圖示）的圓周而配置。 、。管式加熱器48、49 ’係、配置在樹脂流路16之對於前 述圓周的周向兩側，且以並長产 + 八長度方向向者丽述圓周的徑向 =過：述圓周之狀態配置，結果，成為可從 月:排出㈣側之樹脂流路16進行加熱之形態。此外，在 造粒用模具41之比樹脂排出而9 9 土 ι. 奸入古… 曰排出面22罪近擠製機2側的位置 插入有稷數個短加熱器2〇,使短 之缸筒側的樹脂流路16進行加熱。…。2°可對擠製機2 =6圖所示的例子中，管式加熱器I.係由通 中心且沿著模具41的徑向貫通模具41而設置 、= = =式加熱器48、及具有前端到達模具 長度之六根管式加熱器49，以中心線間夾 相互、，且&而構成。此等管式加熱器4 設於樹脂排出面22的中央部之隔敎材。9知配置成可對 加熱。 熱材21的内面附近進行 31999] 15 200916294 • 吕式加熱器48、49可從周知的管式加n分 =模具的大小或形狀而適當地選擇J加== 用：將捲繞於例如棒狀陶瓷之蘇勒^用s式加熱益可使 •(耐敎不銹锢;I，，、線（鎳鉻合金線）插入管 、j <，、、个罅綱官）中，並在發埶 吕 性及古^ @ ^值 毛…、線與官之間隙封裝 胜及施緣性優的材料（_而作成之 门傳熱 加熱器。管式加熱器48可為 ：革被度的棒狀 埶器，亦可早側具有兩根導線之管式加 …、时丌了為在兩側各具有一根導 敛器（sheath h + 、、 吕式加熱态（鞘式加 …时Uheath heater))，不過因為在 管式加熱器的功率密度較高故較佳。，、有兩根¥線之 管式加熱器48、49之加熱器深度 的加工面及耐久性造成問題的範圍内， 4! 1 7阻塞的效。Λ ^ Μ Λ 奴小者其抑制噴嘴 土的放果較大。加熱^米度L以 ::不到1。_則有可能對模具41的加工面= =的則有可能使得抑制噴嘴阻塞的效果降 更仏的範圍為15至30_。 _ 在第6圖所示的例子中，係在造粒用模具Ο之樹 出面22的中心部配置隔熱材2卜在 、曰 . w月曰排出面22的外伽 則有多數個噴嘴17及樹脂流路16沪菩a 而βΛ、 ^ /〇考削述假想圓的圓周 成。配置了隔熱材21及噴嘴17之樹脂排出面22的中 、錢’係設成在腔室6的内部與水接觸。前述假 之與中心線間夾45。角而配置之管式加妖哭 丄^ ,、、、口口 、49白勺中間 相▲的位置，設有一個噴嘴單元及樹脂流路16。 同時，第6圖所示的例子，毋庸說’也與第2圖所亍 的例子-樣，其中之管式加熱器48、49及隔熱材以的種 319991 16 200916294 ,類、以及噴嘴π的配置方法，並不限於本例中之說明者。 接著，說明使用第1圖所示的造粒裝置之發泡性熱塑 -性樹脂粒子之製造方法，其中該造粒裝置安裝有第2圖所 -示的造粒用模具1(或第6圖所示的造粒用模具41)。 使用於該造粒裝置之擠製機2,可從過去在樹脂成形 領域中周知的各種.播製機中依照所要造粒的樹脂種類等而 適當地選擇’可使用例如使用螺桿（screw)的擦製機或未使 用螺桿的撥製機之任何-種。使用螺桿的擦製機，以例如 單軸播製機、雙軸擠製機、通氣式（vent加）擠製機、串 列型（tandem type)擠製機等為佳。未使用螺桿的擠製機， 可列舉如柱塞式（Plunger type)播製機、齒輪果式（卿 :二漸㈣。不論是在哪一種擠製機都可使用靜 心益（static mixer)。此等擠製機中，從生產性的層 面而言以使用螺桿之擦製機為佳。另外，在收容切斷哭曰7 =室6中也一樣，可使用熱切法中所使用之以往周知的 d:發:並不限定熱塑性樹脂的種類，可將例如聚 月匕取聚乙稀系樹脂、聚丙婦系樹月1、聚醋系樹 二樹脂，(丙歸腈—丁二歸-笨乙烯共聚物） 種：上乙烯共聚物)樹脂等單獨使用或混合兩 ==亦可使用從曾經使用過的樹脂製品回收而得 二的回收樹脂。其中，尤以通用級聚苯乙稀 m相擊性以 319991 17 200916294 . 纟使用刖述造粒裝置來製造發泡性熱塑性樹脂粒子的 情況，係將熱塑性樹脂供給至前端絲有造粒用模呈i之 •，製機2内，使之炫融混練1後，—邊使熱塑性樹脂向 -者造粒用模具i移動’一邊藉由高壓泵5將發泡劑從發泡 劑供給口 4壓入到該埶塑性槲士々 ”、、土注树月日，使發泡劑與熱塑性樹脂 混合而形成含有發泡劑的樹脂"。含有發泡劑的樹脂14, 係從播製機2的前端經過模座13而壓送至造粒用模呈工 广6。通過樹脂流路16而輸送之含有發泡劑 树月曰14,係從造粒用模w之各噴幻7送出， 腔室6内的水流中由切斷器7的刀刀加以切斷。 幾、斤^至6内切斷成粒狀之含有發泡劑的樹脂14,成為 之發泡性熱塑性樹脂粒子。此發泡性熱塑性樹脂 it子=水流而輸送到管路11内，然後到達脫水處“ ’在此將發泡性熱㈣樹脂粒子從循環水分離出來，並 吏之脫水、乾燥，分離出的水則送到水槽9。在 理部10分離出來並經脫水、乾燥之、 Μ ^ 子’:、送到容器]2而收容在容器12内“，'，，、塑性樹脂粒 則述發泡劑並沒有特別的限制 戊貌、環錢、㈣二料單獨使肖以人了；^戊燒、異 亦可以上述戍貌類作為主成分，再以上使用。 丙烷等而使用。其巾，尤以容…：正丁垸、異丁燒、 最適合使用。 P 1粒子的發泡之戊烷類 脂中脂粒子，係指使在前述熱塑性樹 以劑再成形成粒狀，較佳為小球狀之樹月旨 319991 18 200916294 .粒子。此發泡性熱塑性樹脂粒子’可用來製造發泡樹脂成 形品’亦即在自由空間内對發泡性熱塑性樹脂粒子進行加 熱使之預備發泡，再將此預備發泡粒子放入具有所希望形 狀的模穴(cavity)之成形模具的模穴内，以蒸氣加心預 備發泡粒子溶融而相互黏結後，進行脫模即製成所希望形 狀的發泡樹脂成形品。 在上述製造方法中，藉由使用第2圖所示的造粒用模 具1(或第6圖所示的造粒用模具41)，利用管式加熱器 18、19(48、49)的加熱效果使噴嘴17之阻塞難以發生，可 改善因阻塞而導致之生產效率的降低，且可製造粒徑均勾 之高品質的粒子。 以下，藉由實施例來實際證明本發明之效果。 [實施例] [實施例1 ] 、使用第1圖所示之造粒裝置，並安裝上第2圖所示之 造粒㈣具’而製造出發泡性聚苯乙烯樹脂粒子。 在口徑90_(L/D=35)的單軸擠製機，安裝上第2圖所 示構造之造粒用模具{在圓周上配置16個各具㈣個直和 0· 、嘴口長度（I and】ength)3· 〇的噴嘴之嘖嘴單元， 並在表面中央部安裝隔熱材，且將直徑12_的管式加熱器 配置在加熱器深度(從樹脂排出面到管式加熱器的中心部 之距離)為15_的位置之模具}，且將預先以滾筒式混合機 (tUmblermixer)將微粉末滑石〇·3質量份均勾混合到聚苯 乙稀樹脂（東洋苯乙稀公司製，商品名「圃⑽」）ι〇〇質 319993 19 200916294 量份中所得到的混合物，以每小時130公斤之速率供給到 擠製機内。將擠製機内的最高溫度設定在22(TC，使樹脂 熔融後，在擠製機中途將相對於樹脂1〇〇質量份為6質量 份之作為發泡劑的戊烷（異戊烷/正戊烷=20/80之混合物） 壓入。在擠製機内一邊使樹脂與發泡劑混練，一邊進行冷 部使在擠製機前端部之樹脂溫度成為17〇r，同時使之通 過與擠製機連接且藉由加熱器而保持在27〇t>c之前述模 具，然後在擠出到有3(rc之冷卻水循環之腔室内的同時， 使圓周方向具有10片刀刀之高速旋轉切斷器密貼於模 具而以每分鐘3300轉的轉速加以切斷，然後進行脫水乾 ’知而得到球形的發泡性聚苯乙烯樹脂粒子。此時，循環水 為300公升/分鐘，發泡性苯乙烯樹脂粒子的排出量為 公斤/小時。 播出開始第1小時之通往模具之樹脂導入部的壓力為 16. OMPa，乾燥後的樹脂粒子1〇〇粒的 模具之開孔率為49.0%之良好值。 593克 擠出開始帛4M、時，通往模具之樹脂導入部的壓力為 n.3MPa，100粒質量為〇.〇61δ克，模具之開孔率為㈣， 確認可進行48小時以上的穩定擠出。 另外，有關在播出開始第4Μ、時獲取之發泡性笨乙稀 二：子’以後述的方法製作體積發泡倍數5〇倍(體積密 ⑽之預備發泡粒子’再使用此預備發泡粒子 泡倍數5〇倍（密度G.G2克心3)之發泡成形體。目 視親祭所得到的發泡成形體，對於預借發、泡粒子往成形金 319991 20 200916294 此外，模具之開孔率係以下述之 屬模之充填性進行評價 方法求出。 〈模具之開孔率〉 孔數= 率二模具表面之排出喷嘴在播出時的開孔率)--開 孔數/杈具全部喷嘴數xl〇〇(%)。 泡性:t:(:二斤」小時)=每一小時以切斷器切出之所有發 X切斷哭的、刀心貝/=開孔數X切出的個數xl粒質量=開孔數 X切斷盗的刀刀數X切斷器的旋轉數X1粒質量。 因此，開孔數為如下式 -的:=ί’出量(公斤/小時)/[切斷器的刀刀數 >< 切斷 口。、疋（rph，轉數/每小時）xi粒質量（公斤/個）]，所 以開孔率可用下式算出。 所 開孔率（E>開孔數/全部排出噴嘴數χ1〇〇(%) =[Q/(NxRx60x(M/1〇〇)/i〇〇〇)]/Hx1〇〇(%) β (式巾’ Q表示排出量(rpm;公斤，小時），Μ示切斷 益刀刃的片數’ R表示切斷器的旋轉數(轉數/每分鐘），μ 表示⑽粒質量（克）（將從發泡性粒子任意選出ι〇〇粒，並 以最小刻度為0.0。01 1之電子秤秤重所得到的值設定為 100粒質量），Η表示模具的全部噴嘴數。） 〈開孔率的評價基準〉 開孔率係依以下的基準進行評價。And the second generation = the step of forming a resin containing a foaming agent W = breaking the above-mentioned hair-containing resin which is discharged from the nozzle of the granulation mold to obtain a foaming thermoplastic resin foaming plasticity榭浐 辜 辜 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供 供The step of forming the body. In the first aspect of the invention, a foamable thermoplastic resin particle obtained by the method of the foamable thermoplastic resin coating 4 is provided. 319991 10 200916294 k 'Materials' The present invention provides a thermoplastic resin expanded particle obtained by preliminary foaming the foaming property. In addition, the present invention provides a thermoplastic resin foam molded article obtained by foam molding the above-mentioned thermoplastic resin expanded particles in a "nucleus". (Effect of the Invention) The granulation mold of the present invention is disposed along the circumference of the pseudo-circular circle on the resin discharge surface, and is disposed on the inner side of the circumference of the nozzle. The surface of the resin has a heat insulating material, and a plurality of tubular heaters are provided in the vicinity of the resin discharge surface so as to extend to the outside through the rounded surface, so that the nozzles are difficult to occur. It is possible to improve the productivity of the r due to clogging, and to produce high-quality particles having a uniform particle size. [Embodiment] Hereinafter, the present invention will be described with reference to the drawings. 1 and 2 show a diagram of an embodiment of the present invention. Fig. 1 is a cross-sectional view showing a structure of a granulation apparatus. Fig. 2A is a cross-sectional view of a granulation mold, and Fig. 2B is a side view showing a side of a resin discharge surface of the granulation mold. In the figures, the symbol 1 is a granulating mold, the symbol 2 is an extruder, the pay number 3 is a hopper, the symbol 4 is a blowing agent supply port, and the symbol $^pressure pump' symbol 6 is a chamber' Symbol 7 is a cutter, symbol 8 is a water pump, symbol 9 is a water tank, symbol 1 is a dehydration treatment line 'symbol 12 is a container, symbol 13 is a mold base (-), and 谠14 is a foaming agent. Resin, symbol 15 is the screw, symbol 16 is the tree wax flow path, symbol π is the nozzle, symbols 18 and 19 are the tube heater, symbol 20 is the short heater, symbol 21 is the heat insulation material, the symbol 35μ is Resin discharge Π 3J999] 200916294, symbol L is the heater depth (distance from the center of the trees 18, 19). "The main components of the granulation device to the s-type heater, the granulation mold, the granulation mold, the front end, the m-machine 2, and the water flow and granulation mold!:,,, The extrusion chamber 6 of 1. The chamber 6 houses a cutter 7 for cutting the resin from the granulation mold and the two contact chambers. Further, the chamber 6 is connected to a tube which is circulated in the H7 row. The road U, one end of the pipe raft is sent to the fruit tank 9. The other end of the pipe U is provided with the foaming circulating water separated, dehydrated, and the granules are separated by the dehydration treatment unit 10, and dehydrated. The dry plastic resin particles are sent to the container 丨2. * The foaming heat is applied to the granulation mold by a plurality of screw inspections 15 to fix the cut end side of the two seats 13, and the mold base 13 is fixed in the squeeze The granulation mold 1 includes a resin discharge surface 22 that is provided in contact with the water flow, and a plurality of nozzles 17 that communicate with the cylinder of the extruder 2 and open on the resin discharge surface 22. The mouthpiece 17 is disposed along the circumference of an imaginary circle (not shown) on the resin discharge surface 22, and the nozzle is disposed The resin discharge surface 22 on the inner side of the circumference of the circumference P is provided with a heat insulating material 21. Further, a plurality of tube heaters 18, 9 are provided in the vicinity of the resin discharge surface 22 so as to extend outward through the center portion of the circumference. In addition, a plurality of short heaters 20 are inserted at a position closer to the extruder 2 than the resin discharge surface 22 of the granulation mold 1, so that the short heater 2 can be coupled to the resin of the nozzle 17 of the granulation mold. The flow path is 6 and heated. 319991 12 200916294 • In the example shown in Fig. 2, <the tubular heaters 18 and 19 are less than the radial through-mold of the vicinity of the resin discharge surface 22: The center of the mold 1 is placed along the mold 1 and the tube heater core = the root tube heater 18, and the front end reaches the middle of the mold 1, and is disposed in the vertical direction and has In the vicinity of the cross-shaped structure, the length of the two tube heaters 196 causes the water flow and the resin row two heaters 18 to flow down the chamber and the flow direction, and the water flow flows down the resin drainage flow. The direction perpendicular to the square of the 19th series along with the aforementioned tube Device: set Wei::: fat discharge surface 22 grease row T... inside the heat insulation material 21 of the central part = heat set in the size or shape of the mold for the tree" === force in the device for granulation: roll For example, it is used for rod-shaped ceramics: the official heater can make (heat-resistant steel pipe) t, and insert the private 赦:..., 士(锁合金合金线) into the pipe guide and the ancient π stitch line and the official The gap is encapsulated into a material with high heat transfer V and back edge _) and is made into high power density. (In addition, the _8 can be a single-sided tube-root heater, or it can have roots on both sides. Official heater of the line (|Shaw-type heater (sheathed = high = tube heater with two wires on one side) is used for proper water resistance in various heat-insulating materials known in the granulation of this embodiment. Further, the heat insulating material 21 in the mold 1 having a high upper surface hardness can be used from % #, but it is preferable to use a heat insulating material which is particularly provided. For example, it is preferable to use 319991 13 200916294 w - the following heat insulating material, that is, to use: on the inner side of the granulating mold 1, and even if it is in contact with the south and warm mold, deformation does not occur. Heat-resistance - and heat-insulating materials with good heat-insulating properties, and covered with water-repellent resin such as fluororesin with good heat-insulating properties, and then high-surface hardness such as stainless steel and ceramics are sequentially laminated on the resin discharge surface 22 side. In the example shown in the second drawing, in the example shown in the second drawing, the heat-dissipating material 21' is placed on the outer side of the resin discharge surface 22 in the resin discharge of the granulation mold i. The plurality of nozzles 17 are along the circumference of the aforementioned imaginary circle and the roots of the tree-transporting surface 22 of the ==117 are set to be in contact. Among the above-mentioned imaginary circles, the nozzles 17 are not provided at positions overlapping with the arrangement positions of the wide "U 18 and 19". In this example, the nozzles are provided. Further, 1 7 secrets are set. / The method of arranging a nozzle unit in which a plurality of nozzles have a circumferential arc segment, and the β-return nozzle 7 is formed on the pseudo-phase circle is not limited to this example. A modification example showing an embodiment of the present invention is shown. In the following, the same or the same constituents are used, and the same parts are used:::: $. Its Gongming' is a resin different from the above-described embodiment, and the resin of the granulation mold for granulation is carried out. The second section of the discharge surface 'the 6th figure shows that the granulation is shown in μ? side view. In these figures, the symbol 41 is the granulation tool, the symbol 48 door ~ 50C> 49 is the e-type heater, the symbol 50 (50A, 50B, Chuan C 50D) for thermocouples, etc. crying deep production t hands ~ measuring the limbs (" dish sensor", symbol L · for the addition of - ice ((4) fat discharge surface (two) to the tube Heater price (4) Center part 319991 14 Distance from 200916294) This morphological granulation mold 41 has The resin discharge surface 22' which is in contact with the water flow in the chamber 6 and the resin discharge inside the circle 2 in which a plurality of nozzles 17 (communicating with the cylinder of the extruder 2 and opening on the resin discharge surface 22) are disposed In addition, a plurality of tubular dampers ", 49 which are extended to the outside by the center portion of the month of the month, are provided in the vicinity of the resin discharge surface 22, and the surface of the resin discharge surface 22 is provided. . Further, the granulation mold 41 is provided with a plurality of resin flow paths 16 that communicate with the cylinders of the money 2 and are connected to the nozzles, and the resin flow path 16 is along a virtual circle (not shown) on the resin discharge surface. Configured in the circumference. ,. The tube heaters 48, 49' are disposed on both sides of the resin flow path 16 on the circumferential side of the circumference, and are in the radial direction of the circumference of the length of the length of the length of the eight-length direction. As a result, it is a form in which the resin flow path 16 on the side of the discharge (four) side can be heated. In addition, in the granulation mold 41, the ratio of the resin is discharged, and the 9 土 ι 奸 奸 奸 古 古 古 古 22 22 22 22 22 22 22 22 近 近 近 近 近 近 近 近 近 近 近 近 近 近 近 近 近 近 近 近The resin flow path 16 on the cylinder side is heated. .... 2° in the example shown in the figure of the extruder 2 = 6, the tube heater I. is provided by the center and through the mold 41 in the radial direction of the mold 41, = = = heater 48, and The six tube heaters 49 having the front end reaching the length of the mold are formed by sandwiching each other between the center lines. These tube heaters 4 are provided in the center of the resin discharge surface 22. 9 know that it can be configured to be heated. The vicinity of the inner surface of the hot material 21 is carried out 31999] 15 200916294 • The luer heaters 48, 49 can be appropriately selected from the well-known tube type plus n = mold size or shape. J plus == used: will be wound on, for example, a rod The s-type heating of the ceramics can be used to heat the s-type heating (I, ,, 线, wire (nickel-chromium wire) into the tube, j <,,, 罅 罅), and埶 性 及 及 及 及 及 及 及 及 及 及 及 及 及 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 Rod-shaped sputum can also be used to add two wires on the early side of the tube. When it is smashed, there is a guide on each side (sheath h + , 吕 加热 (shelf type... Uheath Heater)), but it is preferable because the power density of the tube heater is high, and the processing depth and durability of the heater depth of the two-wire tube heaters 48 and 49 are within the range , 4! 1 7 blocking effect. Λ ^ Μ Λ 奴 者 者 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 抑制 加热 加热 加热 加热 加热 加热 加热 加热 加热When the machined surface = =, the effect of suppressing the clogging of the nozzle may be reduced to a range of 15 to 30 mm. _ In the example shown in Fig. 6, the center portion of the tree surface 22 of the granulation mold is disposed. The outer layer of the heat-insulating material 2, the outer surface of the discharge surface 22 of the 曰. w曰 有 has a plurality of nozzles 17 and a resin flow path 16 and a β Λ, ^ / 削 test the circumference of the imaginary circle. The middle portion of the resin material discharge surface 22 of the hot material 21 and the nozzle 17 is in contact with water in the interior of the chamber 6. The false and the center line are sandwiched by 45. , , , , mouth, 49, the position of the middle phase ▲, a nozzle unit and a resin flow path 16. At the same time, the example shown in Fig. 6 is not to say 'also with the example of the second figure- For example, the arrangement of the tube heaters 48 and 49 and the heat insulating material 319991 16 200916294, and the arrangement of the nozzles π are not limited to those described in the present example. A method for producing foamable thermoplastic resin particles of a granulation device, wherein the granulation device is mounted with the second image The granule mold 1 (or the granulation mold 41 shown in Fig. 6). The squeezing machine 2 used in the granulation apparatus can be made from various kinds of weaving machines known in the field of resin molding in the past. The resin type of the granules and the like are appropriately selected as 'any one of a squeegee using, for example, a screw using a screw or a machine using no screw. A squeegee using a screw, for example, a single-axis splicing machine, A twin-screw extruder, a vent-type extruder, a tandem type extruder, etc., and an extruder that does not use a screw may be exemplified by a Plunger type. Machine, gear fruit type (Qing: two gradually (four). Static mixers can be used in any type of extruder. In such an extruder, it is preferable to use a screw-type wiping machine from the viewpoint of productivity. In addition, in the case of accommodating and cutting the crows 7 = chamber 6, the conventionally known d: hair used in the hot cutting method can be used. The type of the thermoplastic resin is not limited, and for example, polystyrene can be obtained. Resin, Polypropylene Women's Tree Moon 1, Polyacetate Tree II Resin, (Aluminum Nitrile - Ding Ergui - Stupid Ethylene Copolymer) Species: Ethylene Copolymer) Resin or the like used alone or mixed two == can also be used from A recycled resin obtained by recycling a resin product that has been used. In particular, the general-purpose polystyrene m-phase strikeability is 319991 17 200916294. When a foaming thermoplastic resin particle is produced by using a granulation apparatus, a thermoplastic resin is supplied to the front end yarn and a granulation mold. In the machine 2, after the kneading and kneading, the thermoplastic resin is moved to the granulation mold i, and the blowing agent is supplied from the blowing agent supply port 4 by the high pressure pump 5. Pressed into the plastic warrior 々", the earth is poured into the tree, and the foaming agent is mixed with the thermoplastic resin to form a resin containing a foaming agent. The resin 14 containing the foaming agent is from the seeding machine. The front end of the second mold is fed to the granulation mold by the mold base 13 and the granulation mold is conveyed by the resin flow path 16 to be sent from the granulation mold. The water flow in the chamber 6 is cut by a knife of the cutter 7. The resin 14 containing the foaming agent is cut into a granular shape into a foaming thermoplastic resin particle. This foaming thermoplastic resin is transferred to the pipe 11 in the flow of water, and then reaches the dehydration section "'The foaming heat here (4) The resin particles are separated from the circulating water, dehydrated and dried, and the separated water is sent to the water tank 9. The chemical agent 10 is separated and dehydrated, dried, Μ ^ ':, sent to the container 2 and contained in the container 12 ", ',,, plastic resin particles, there is no particular limitation on the foaming agent. Appearance, ring money, (four) two materials alone to make Xiao Yiren; ^ E-burn, different can also be used as the main component of the above-mentioned appearances, and then used above. Propane, etc.. Its towel, especially to accommodate...: 正丁垸The isobutylene is most suitable for use. The P1-particle foaming pentane lipid-in-lipid refers to the formation of a granular shape in the thermoplastic tree, preferably a small spherical tree. 200916294. Particles. The foamable thermoplastic resin particles ' can be used to produce a foamed resin molded article', that is, the foamable thermoplastic resin particles are heated in a free space to be foamed, and then the preliminary foamed particles are placed. In the cavity of the molding die having a cavity having a desired shape, the foamed particles are melted and the foamed particles are melted and bonded to each other, and then released into a foamed resin molded article having a desired shape. In the manufacturing method, by using the second figure The granulation mold 1 (or the granulation mold 41 shown in Fig. 6) shown in the drawing is difficult to cause the clogging of the nozzle 17 by the heating effect of the tube heaters 18 and 19 (48, 49), thereby improving the cause. The production efficiency is lowered by the blockage, and high-quality particles having a particle size can be produced. Hereinafter, the effects of the present invention are actually demonstrated by the examples. [Examples] [Example 1] Using Figure 1 The granulation apparatus shown is attached to the granulation (4) shown in Fig. 2 to produce foamable polystyrene resin particles. Installation is carried out in a uniaxial extruder having a diameter of 90 mm (L/D = 35). The granulating mold of the structure shown in Fig. 2 is arranged on the circumference of a nozzle unit of 16 nozzles each having four (four) straight and 0·, mouth length (I and ength) 3· , on the circumference, and on the surface A heat insulating material is installed in the center, and a tubular heater having a diameter of 12 mm is disposed at a depth of the heater (a distance from the resin discharge surface to the center of the tubular heater) to a position of 15 mm, and will be advanced Mixing 3 parts by mass of talc talc with a tumbler mixer (tUmblermixer) to polystyrene resin (Toyo Phenyl Ethylene) Company-made, trade name "圃(10)") ι 3 319993 19 200916294 The mixture obtained in the parts is supplied to the extruder at a rate of 130 kg per hour. The maximum temperature in the extruder is set at 22 (TC, after the resin is melted, 6 parts by mass of the resin is pentane (isopentane / positive) relative to 1 part by mass of the resin in the middle of the extruder. a mixture of pentane = 20/80) is pressed in. In the extruder, the resin is kneaded with the foaming agent, and the cold portion is made to make the temperature of the resin at the front end portion of the extruder 17 〇r, and at the same time pass and squeeze. The machine is connected and held by the heater in the aforementioned mold of 27〇t>c, and then extruded into a chamber having 3 (rc cooling water circulation), and has a high-speed rotary cutting of 10 blades in the circumferential direction. The breaker was attached to the mold and cut at a rotation speed of 3,300 rpm, and then dehydrated and dried to obtain spherical foamable polystyrene resin particles. At this time, the circulating water was 300 liters/min, and foaming was performed. The discharge amount of the styrene resin particles is kg/h. The pressure at the resin introduction portion of the mold at the first hour of the start of the broadcast is 16. OMPa, and the opening ratio of the mold of the resin particles after drying is 1 Good value of 49.0%. 593g extrusion starts 帛4M, when The pressure at the resin introduction portion of the mold is n.3 MPa, the mass of 100 grains is 〇.〇61δg, and the opening ratio of the mold is (4), and it is confirmed that stable extrusion can be performed for 48 hours or more. The foaming property of the fourth Μ, the time is obtained by the method described later, and the volume expansion ratio is 5 〇 times (the volume of the pre-expanded particles of the dense volume (10) is re-used. Foamed molded body (density G.G2 core 3). Visually molded foamed molded body, for pre-borrowing, foaming particles, forming gold 319991 20 200916294 In addition, the opening ratio of the mold is as follows The filling method of the mold is determined by the evaluation method. <Opening ratio of the mold> Number of holes = Rate of opening of the discharge nozzle of the mold surface at the time of the broadcast) - Number of openings / Number of nozzles of the cookware xl〇 〇 (%). Foaminess: t: (: 2 kg) hours = every hour cut by the cutter, X cut off, knife heart / = number of holes X cut out Xl grain quality = number of openings X number of knives cut off X number of rotations of the X cutters X1 grain quality. Therefore, the number of holes is as follows: = ί 'out Quantity (kg/hr) / [number of cutters for the cutter] < cut-off port, 疋 (rph, number of revolutions per hour) xi grain mass (kg / piece)], so the opening ratio can be used as follows Calculated. Opening ratio (E> number of openings/number of all discharge nozzles χ1〇〇(%) = [Q/(NxRx60x(M/1〇〇)/i〇〇〇)]/Hx1〇〇(%) β (type towel 'Q indicates the discharge amount (rpm; kg, hour), indicating the number of cut-off blades' R' indicates the number of revolutions of the cutter (revolutions per minute), and μ means (10) grain mass (g) (The value obtained by arbitrarily selecting ι 〇〇 from the foamable particles and weighing the electronic scale with a minimum scale of 0.011 is set to 100 grains), and Η indicates the total number of nozzles of the mold. <Evaluation Criteria for Opening Ratio> The opening ratio was evaluated based on the following criteria.
◎ : 50%SE Ο : 40%^E< 50% Δ ： 30°/^E<40% 319991 21 200916294 x · E< 30% * 〈發泡成形體之製造〉 冑如前述實施而在擠出開始第4 8小時得到之發泡性 ，苯乙烯樹脂粒子在20°C放置一天後，相對於發泡性苯乙烯 樹脂粒子100質量份，添加硬脂酸鋅〇.丨質量份、羥基硬 脂酸三酸甘油酯0.05質量份、硬脂酸單甘油酯量 份，加以混合使之被覆於樹脂粒子表面後，投入小型批: Γ式預備發泡機（内容積40L)，一邊攪拌一邊以吹入^ 〇. 05MPa(表壓）之水瘵氣進行加熱，而製作體積發泡倍數 5〇倍（體積密度〇· 〇2克/cm3)之預備發泡粒子。 接著’使所得到之預備發泡粒子在2rc熟成一天後， 使用安裝有外形尺寸300x400xl00mm (厚度30mm)且内部具 有厚度為5mm、1 〇丽、25mm的間隔部的模具之自動成形機 (積水工機製作所製，ACE-3SP型），以下述成形條件進行 成形而得到發泡倍數50倍（密度0· 02克/cm3)之發泡成形 成形條件（ACE-3SP QS成形模式） 成形蒸氣壓 0. 08MPa(表壓） 模具加執 3秒 方向加熱（壓力設定） 0. 03MPa(表壓） &方向加埶 2秒 兩面加熱 12秒 水冷 10秒 °又疋取出面壓 0.02Mpa 22 319991 200916294 •〈預備發泡粒子之模具充填性之評價基準〉 充填^視觀察上述發泡成形體，^下的基準評估模具 ◎:元全填滿厚度5mni間隔部份 〇：雖然厚度5_間隔部份之充填不密實而可觀 過大的發泡粒，但間隔部份仍算形成 △:在厚度間隔部份可相由於充填不 粒子缺損，間隔部份並未完全形成 之 成X :厚度5_間隔部份充填不良，間隔部份完全未形 〈粒子100粒之合計質量〉 上從發泡性聚苯乙婦樹脂粒子中任意選出粒 r質量以落在0.02至。，。9克的範 。之 =對於成形模具細部的充填性會變得困難，有赶可= 可成形的模具限定在單純形狀者。不到q 使仔 生產性變差之虞。更佳的範圍為0.04至0.06克有=的 在聚苯乙烯㈣脂以外之樹脂 "， 脂的比重所得到的值則常在較佳的粒子乘以樹 的範圍内。 子100粒之合計質量 〈預備發泡粒子之體積發泡倍數的洌定方法〉 用漏斗使充分乾燥後的預備發自 u列如500毫升容量）内，敲擊 …一。下到1同 子，直到預傷發泡粒子的容積到充填預備發泡粒 備發泡粒子的容積與質量而利用；：：為止。測定此時預 式异出體積發泡倍數。 319991 200916294 n、谷：係以1毫升為單位讀取，質量係以最小刻度為 告、之電子秤測量。而且，以苯乙烯系樹脂的樹脂比重 二 來汁，且體積發泡倍數係將小數點以下1位四 • 捨五入而得。 、體積發泡倍數（倍）=預備發泡粒子的容積（毫升）/預備 發泡粒子的質量（克）x樹脂比重 、 〈迤泡成开> 體之發泡倍數的測定方法〉 從充分乾燥後的發泡成形體切出測定用試驗片（例如 300x400X30_)’測量此試驗片的尺寸與質量，以測量出的 尺寸為基礎算出試驗片的體積，然後利用下式算出發泡倍 數。其中，以苯乙烯系樹脂的樹脂比重當作】.〇來計算。 發泡倍數（倍試驗片體積（cm3)〆試驗片質量（克众樹 脂比重 [實施例2 ] 使用第1圖所示之造粒裝置，並安裝上第6圖所示之 造粒用模具而製造出發泡性聚苯乙烯樹脂粒子。 在口徑90匪（L/D=35)的單軸擠製機，安裝上第6圖所 不構造之造粒用模具{在圓周上配置8個各具有15個直徑 〇. 6 mm、嘴口長度3. Omm的噴嘴之喷嘴單元，並在表面中 央部安裝隔熱材，且將直徑12_的管式加熱器48、仞配 置在加熱器深度（從樹脂排出面到管式加熱器的中心部之 距離）為15丽的位置之模具丨，且將預先以滾筒式混合機將 微粉末滑石0. 3質量份均勻混合到聚苯乙烯樹脂（東洋笨 乙烯公司製，商品名「HRM10N」）1〇〇質量份中所得到的混 319991 24 200916294 .合物，以每小時130公斤之速率供給到擠製機内。將擠製 機内的最南溫度設定在220°C ’使樹脂熔融後，在播製機 中途將相對於樹脂100質量份為6質量份之作為發泡劑的 .戊烷（異戊烷/正戊烷=20/80之混合物）壓入。在擠製機内 -邊使樹脂與發泡劑混練…邊進行冷卻使錢製機前端 =之樹脂溫度成為17Gt，同時使之通過與播製機連接且 糟由加熱器而保持在280°C之前述模具，然後在擠出到有 :30°C之冷卻水循環之腔室内的同時，使圓周方向具有ι〇 片刀刃之高速旋轉切斷器密貼於模具上，而以每分鐘33〇〇 轉的轉速加以切斷，然後進行脫水乾燥而得到球形的發泡 性聚，乙烯樹脂粒子。此時的猶環水為3〇〇公升/分鐘，發 泡性苯乙烯樹脂粒子的排出量為138公斤/小時。 在此實施例2中，擠出開始第1小時之通往模且41 :::旨：：部的昼力為16鳥，乾燥後的樹脂粒子⑽ 值。貝里為o.om克，模具之開孔率為δ2 5%之極良好的 力為彳4Μ、時之職模具41之樹料人部的壓 力為n.OMPa，刚粒質量為"7 隨，確認可進行48小時以上的穩定擠出Γ之開孔率為 粒子有ϊ =始=小時獲取之發泡性苯乙烯樹脂 U2克/em3)之 ^作體積發泡倍數5〇倍（體積密度 造發泡倍數克再❹此職發泡粒子製 觀察所得到的發泡成形體估包成形體°目視 战办，矸估預備發泡粒子對成形模具 319991 25 200916294 之充填性。 [實施例3 ] 在實施例3中，除了使實施例2中使用之模具的與噴 嘴單元連結之樹脂流路擴張（增加斷面積），且使安裝/的模 具中每一噴嘴單7L之噴嘴數從15個增加到25個以外，其 餘與實施例2 —樣，而以138公斤/小時的排出量得到球形 的發泡性聚苯乙烯樹脂粒子。 / 在此實施例3中，擠出開始第丨小時之通往模具之樹 脂，入部的壓力為13.6MPa，乾燥後的樹脂粒子丨、〇〇'粒的 質量為0· 0454克，模具之開孔率為76· 8%之良好值。 播出開始第48小時之通往模具之樹脂導入部的墨力 為13.8 MPa，100粒質量為〇.〇459克，模具之開孔率為 76.0%，確認可進行48小時以上的穩定擠出。 使用在擠出開始第48小時獲取之發泡性苯乙婦樹脂 粒子’與實施例1 一樣製作體積發泡倍數50倍（體積穷戶 〇.〇2克/W)之預備發泡粒子，再使用此預備發泡粒子y 造發泡倍數5〇倍（密度〇. 02克/⑽3)之發泡成形體。目視 親祭所得到的發泡成形體，評估預傷發泡粒子對成形模且 之充填性。 、八 [實施例4 ] f、實施例4中’除了使用將實施例3中使用之模具之 加熱為深度從15咖變更為训 产 尺马刈咖之杈具以外，其餘與實施 例〇 —樣，而以138公斤/小時的排 、 聚苯乙烯樹脂粒子。 ^非出里付到球形的發泡性 319991 26 200916294 在此實施例4中，播出開始第！小時之通往模且之樹 脂導入部的壓力為16 〇MPa，乾燥後的樹脂粒子1〇〇粒的 質量為0.0511克，模具之開孔率為68 2%之良好值。 ^ 擠出開始第48小時之通往模具之樹脂導入部的壓力 為16.5 MPa’ 100粒質量為〇.〇552克，模具之開孔率為 ,63. 1 %，確認可進行48小時以上的穩定播出。 使用在擠出開始第48小時獲取之發泡性苯乙烯樹脂 粒子，與實施例1 一樣製作體積發泡倍數5〇倍（體積密度 〇. 02克/cm )之預備發泡粒子，再使用此預備發泡粒子製 造發泡倍數50倍(密度〇. 02克/cm3)之發泡成形體。目視 觀察所得到的發泡成形體，評估預備發泡粒子對成形模呈 之充填性。 〃 [實施例5 ] 在實施例5中，除了使用將實施例3中使用之模具之 加熱器深度從l5mm變更為45mm之模具以外，其餘與實施 例3樣而以138公斤/小時的排出量得到球形的發泡性 聚苯乙稀樹脂粒子。 在此實施例5中，擠出開始第！小時之通往模具之樹 脂導入部的壓力為16.7MPa，乾燥後的樹脂粒+ ι〇〇粒的 質量為0.0657克，模具之開孔率為53. 1%之良好值。 私出開始第4 8小時之通往模具之樹脂導入部的壓力 為lUMPa ’ 1〇〇粒質量為〇. 〇865克，模具之開孔率為 40.3%，確認可進行48小時以上的穩定擠出。 有關在擠出開始第48小時獲取之發泡性苯乙烯樹脂 319991 27 200916294 •粒子，與實施例i-樣製作體積發泡倍數5〇倍（體積密声 〇.〇2克/cm3)之預備發、泡粒子，再使用此預備發泡粒子ς 造發泡倍數50倍（密度〇· 02克心3)之發泡成形體。目$ 1察所Μ㈣，評估職發泡粒子 模之充填性。 m [比較例1] 除了將板具換為第3圖所示之公知構造的模具Μ之 Γ外，其餘與實施例1 一樣，以138公斤/小時的排出量 球形的發泡性聚苯乙烯樹脂粒子。 弟3A圖係比較例1中使用的模具31之斷面圖，第3β 的樹脂排出面之側面圖。此模具31除了 斤示之模具1中所用之配置成十字形的管 式加熱盗18、1 9之外，且古也愈^ y 相同的構造。 /、有…例1中所用的模具1 姓t此比較例1 t，擠出開始第1小時之通往模具3i 香，广且力為21.7Mpa之高，⑽粒質量為0.1322 克拉具31之開孔率為22. 〇%。 出開：觀察到樹脂導入部的壓力升高，到擠 因 吟方；到達輪具31之耐壓上限值（25 Mpa)， 口此在第6小時停止擠出。 [比較例2] 外.1於… 圖所不之公知構造的模具32之 ^ 1 一樣，而以⑽公斤/小時_山 到球形的發泡性苯乙稀樹腊粒子。 里付 319991 28 200916294 ，帛4A圖係比較例2中使用的模具&之斷面 的樹脂排出面之侧面圖。此模具物 ”有第2圖所示之模具！中所用之配置成十 ： ’熱器19,但模具中央部並未設置發熱部。除此之外^ 口 與貫施例1中所用的模具丨相同的構造。 八有 在此比較例2中，擠出開始第1小時之通往模呈32 之樹脂導人部_力為略微偏高之2^ Mpa，iqq粒、 為〇. 1030克，模具32之開孔率為28. 2%。 "里 隨著時間增長可觀察到樹脂導入部的 出開始第1 0小時到i衾握i Q0 >上f J ^ “到達換具32之耐壓上限值(25 Mpa)，因 此在弟1 0小時停止播出。 [比較例3 ] 除了藉由以油當熱媒體之間接加熱將模具33保持在 以外，其餘與實施例卜樣，而以138公斤/小時= 排出置得到球形的發泡性苯乙烯樹脂粒子。 第5A圖係比較例3中使用的模具33之斷面圖，第5β ^系顯示模具33的樹脂排出面之側面圖。此模具33中並 ^又置弟2圖所示之模具1中所用的隔熱材21，而是形成 為.在板具33内設有作為熱媒之油的流路 油從設於模具上下的埶媼Α π 便间，皿的 …、媒入口 24流入，通過中央之環狀流 路1嫂從設於模具左右之熱媒出口 25流出，而後回到 油加熱器之構造。 在此比較例3中，播出開始第1小時之通往模具33 之樹脂導入部的壓力為18，Pa，10。粒質量為克， 319991 29 200916294 , 模具33之開孔率為32. 0%。 擠出開始第48小時’通往模具33之樹脂導入部的塵 力為21.8 MPa，100粒質量為0.0994克，模具33之門孔 率為29. 2%。 發泡粒子製造發泡倍數50倍（密度〇. 〇2 此比較例3也和實施例1 一樣’使用在擠出開始第48 小時獲取之發泡性苯乙烯樹脂粒子製作體積發泡倍數Μ 倍（體積密度0.02克/cm3)之預備發泡粒子，再使用此預備 2克/cm )之發泡成 評估預備發泡粒子 形肢。目視觀察所得到的發泡成形體， 對成形模具之充填性。 將實施例1至5及比較例 1至3之結果整理 記载於表 319991 30 200916294 [表1 ] 比較例3 油流路式 S ° ° jii： CNI O CO oo CO CO 18.0 · 32.0 Δ 21.8 29.2 X 0. 0994 X 設置 成本高 比較例2 加熱器深度 15mm O CD Ο , ” ••你 C^J Ο 〇〇 Λ oo CO CD C 〇〇 o oo x Cn3 CNI 1H ^ w -*-{ 哲故1 ,. •f盲丨丨 Ξ «4c 比較例1 表層無加熱器 O CD Ο . ^ •.你 CNJ O CO ^ 00 co CO 卜〇 —· d x csa c<i τ: -Μ I , 七畜丨丨 CO 實施例5 加熱器深度 45nun O CD O , O · ·杯 CN3 O CO ' 00 CO ψ^< ς〇 卜— CO CO @ ίΛ 18.0 40.3 〇 0. 0865 〇 實施例4 加熱器深度 30mm O CD C5 , O · ·你 CM O CO ^ oo CO T·^ CO C=» CS3 CD OO @ —CO Lf5 — CD CO @ — CD 0.0552 ◎ 實施例3 加熱器深度 15mm C=> CD O , O · •你 CM O CO •oo CO CD CO OO CO CD © —卜 oo o CQ CD @ — 卜 0. 0459 ◎ 實施例2 漩柘蹤g ^ Ln 卖摊甚坊 Ο ς〇 O , —O CO 00 co »—H C£> 16.8 82.5 ◎ 17.0 80.0 ◎ 0.0726 〇 實施例1 筚μ名二 W染咏 O CO o . Cs3 〇 CC oo CO CO <=> 〇 cd σι O CO o 卜*卜· o — 寸 0.0618 〇 棋具的構造 y—v /—v y—v 單画画 挺勃靶 fi τί ιιφί if 33 -35 D 笨笨妒堕 排出量（kg/h) 發泡劑（戊烷）質量份 擠出樹脂溫度（°C) 模具保持溫度（°c) 循環水溫（"c) 第1小時棋具壓力（Mpa) 間礼率E (%) 評怙 第48小時棋具壓力（Mpa) 間孔率E (« 評估 第48小時100粒質量(g) 預備發泡粒子之棋具充填 性（體稍倍數50倍） 備往 31 319991 200916294 從表1之結果可知，本發 , ^ 月您戶'轭例1，從造粒開私 第1小時之模具壓力為16 開始◎ : 50% SE Ο : 40%^E< 50% Δ : 30°/^E<40% 319991 21 200916294 x · E< 30% * <Production of foamed molded article> Extrusion as described above The foaming property obtained in the 48th hour was started, and after the styrene resin particles were allowed to stand at 20 ° C for one day, zinc stearate 丨 丨 mass parts, hydroxy stearin was added to 100 parts by mass of the expandable styrene resin particles. 0.05 parts by mass of acid triglyceride and a part by weight of stearic acid monoglyceride, which were mixed and coated on the surface of the resin particles, and then placed in a small batch: a mash-type preliminary foaming machine (internal volume 40 L), which was blown while stirring The helium gas of the pressure of 05 MPa (gauge pressure) was heated to prepare a preliminary expanded particle having a volume expansion ratio of 5 times (volume density 〇·〇2 g/cm3). Then, 'the obtained preliminary foamed particles were cooked in 2 rc for one day, and an automatic molding machine equipped with a mold having an outer dimension of 300 x 400 x 100 mm (thickness: 30 mm) and having a thickness of 5 mm, a brilliant, and 25 mm inside was used. ACE-3SP type, which was molded by the machine manufacturer, was molded under the following molding conditions to obtain a foam molding molding condition (ACE-3SP QS molding mode) in which the expansion ratio was 50 times (density 0. 02 g/cm3). 08MPa (gauge pressure) Mold plus 3 seconds direction heating (pressure setting) 0. 03MPa (gauge pressure) & direction plus 2 seconds heating on both sides for 12 seconds water cooling 10 seconds ° and removing the surface pressure 0.02Mpa 22 319991 200916294 • <Evaluation Criteria for Mold Fillability of Prepared Foamed Particles> Filling and visualizing the above-mentioned foamed molded body, the following evaluation of the mold ◎: the full filling of the thickness of the interval of 5 mni 〇: although the thickness of the interval of 5_ The foaming particles are not densely packed and can be oversized, but the spacing is still formed as △: in the thickness interval, the filling portion is not filled with particles, and the spacing portion is not completely formed into X: thickness 5_interval Defective filling, the spacer portion is not formed completely <100 total mass of particles> r arbitrarily selected particles from the mass of expandable polystyrene resin particles on women to fall to 0.02. ,. 9 grams of van. = The filling property of the forming die detail becomes difficult, and there is a case where the mold that can be formed is limited to a simple shape. Less than q makes the productivity worse. A more preferred range is from 0.04 to 0.06 grams of resin other than polystyrene (tetra) grease. The value obtained by the specific gravity of the fat is often in the range of better particles multiplied by the tree. Total mass of 100 particles <Method for determining the volume expansion ratio of the pre-expanded particles> The preparation for sufficiently drying the funnel with a funnel is sent from the column of u (for example, 500 ml capacity), and tapped. The first to the same is used until the volume of the foamed particles is pre-injured to the volume and mass of the foamed particles to be filled with the preliminary foaming particles; The pre-formed volume expansion ratio at this time was measured. 319991 200916294 n, Valley: is read in 1 ml, the quality is measured by the electronic scale with the smallest scale. Further, the specific gravity of the resin of the styrene resin is two, and the volume expansion ratio is obtained by rounding off one decimal place below the decimal point. Volume expansion ratio (times) = volume of pre-expanded particles (ml) / mass of pre-expanded particles (g) x specific gravity of resin, "foaming opening" > method for measuring foaming ratio of body > from full The test piece for measurement (for example, 300×400×30_) of the foamed molded article after drying was measured. The size and mass of the test piece were measured, and the volume of the test piece was calculated based on the measured size, and then the expansion ratio was calculated by the following formula. Among them, the specific gravity of the resin of the styrene resin is calculated as ". Expansion ratio (multiple test piece volume (cm3) 〆 test piece mass (gram specific resin specific gravity [Example 2] The granulation device shown in Fig. 1 was used, and the granulation mold shown in Fig. 6 was attached. The foaming polystyrene resin particles are produced. In a uniaxial extruder having a diameter of 90 匪 (L/D = 35), a granulation mold which is not constructed in Fig. 6 is attached. 15 nozzles with a diameter of 66 mm and a mouth length of 3. Omm, and a heat insulating material is installed at the center of the surface, and the tube heaters 48 and 直径 with a diameter of 12 mm are disposed at the depth of the heater (from 3质量份 uniformly mixed to a polystyrene resin (Toyo stupid), a micro-powder talc is uniformly mixed with a micro-powder talc in advance by a tumbler mixer. The ethylene compound company, trade name "HRM10N") is a mixture of 319991 24 200916294 obtained in 1 part by mass, supplied to the extruder at a rate of 130 kg per hour. The southernmost temperature in the extruder is set at After the resin is melted at 220 ° C, it will be relative to the resin in the middle of the seeding machine. 100 parts by mass of 6 parts by mass of a pentane (isopentane/n-pentane = 20/80 mixture) as a foaming agent is pressed in. In the extruder, the resin is kneaded with the foaming agent. The cooling makes the resin front end = the temperature of the resin becomes 17 Gt, while passing it through the above-mentioned mold which is connected to the seeding machine and kept at 280 ° C by the heater, and then extruded to a cooling water cycle of: 30 ° C. At the same time in the chamber, a high-speed rotary cutter having a 〇 blade edge in the circumferential direction is adhered to the mold, and is cut at a rotation speed of 33 rpm, and then dehydrated and dried to obtain a spherical foam. Polymerized, vinyl resin particles. At this time, the water of the quaternary ring was 3 liters/min, and the discharge amount of the foamable styrene resin particles was 138 kg/hr. In the second embodiment, the first hour of the extrusion was started. The way to the mold and 41::::: The force of the part is 16 birds, the value of the resin particles after drying (10). Berry is o.om grams, the mold opening ratio is δ2 5% extremely good force For the 彳4Μ, the pressure of the tree part of the mold 41 is n.OMPa, the grain quality is "7, confirm The opening ratio of the stable extrusion enthalpy of 48 hours or more is 粒子 始 = initial = hour, the foaming styrene resin U2 g / em3) is used as the volume expansion ratio of 5 times (volume density foaming) In addition, the foamed molded body obtained by observation of the foamed particles was observed, and the filling property of the preliminary foamed particles to the forming die 319991 25 200916294 was evaluated. [Example 3] In Example 3, except that the resin flow path connected to the nozzle unit of the mold used in Example 2 was expanded (increased sectional area), and the number of nozzles per 7 L of each nozzle in the mounted mold was increased from 15 to 25. In the same manner as in Example 2 except for one, the spherical expandable polystyrene resin particles were obtained at a discharge amount of 138 kg/hr. / In this Example 3, the resin to the mold at the beginning of the second hour of extrusion, the pressure at the inlet portion was 13.6 MPa, and the mass of the resin particles 干燥 and 〇〇' after drying was 0. 0454 g, and the mold was opened. The porosity was a good value of 76·8%. The ink force of the resin introduction portion to the mold at the 48th hour from the start of the broadcast was 13.8 MPa, the mass of 100 grains was 〇. 〇 459 g, and the opening ratio of the mold was 76.0%. It was confirmed that stable extrusion was possible for 48 hours or more. . The foamed styrene resin particles obtained at the 48th hour from the start of extrusion were used to prepare a preliminary expanded foam having a volume expansion ratio of 50 times (volume 〇.〇2 g/W) as in Example 1. A foamed molded article having a foaming ratio of 5 〇 (density 〇 2.0 g / (10) 3) was produced using this preliminary expanded particle y. The foamed molded body obtained by the pro-sacrifice was visually observed, and the filling property of the pre-injured expanded particles to the forming mold was evaluated. [Embodiment 4] f, in the embodiment 4, except that the heating of the mold used in the embodiment 3 is changed from the 15 coffee to the cookware of the training scale, the rest is the same as the embodiment - Like, with 138 kg / h of row, polystyrene resin particles. ^ Non-existing to the spherical foaming property 319991 26 200916294 In this embodiment 4, the broadcast starts! The pressure at the resin introduction portion of the mold was 16 MPa, and the mass of the resin particles 1 after drying was 0.0511 g, and the opening ratio of the mold was 68 2%. ^ The pressure at the resin introduction part of the mold at the 48th hour from the start of extrusion is 16.5 MPa' 100 granules is 〇 〇 552 g, and the opening ratio of the mold is 63. 1%. It is confirmed that it can be carried out for more than 48 hours. Stable broadcast. Using the expandable styrene resin particles obtained at the 48th hour from the start of extrusion, the preliminary expanded particles having a volume expansion ratio of 5 times (volume density 〇.02 g/cm) were produced in the same manner as in Example 1, and this was used. The foamed molded article was produced by preparing the expanded beads to have a foaming ratio of 50 times (density 〇. 02 g/cm 3 ). The obtained foamed molded article was visually observed, and the filling property of the preliminary expanded particles to the forming mold was evaluated.实施 [Example 5] In Example 5, except for the mold in which the depth of the heater of the mold used in Example 3 was changed from 15 mm to 45 mm, the discharge amount of 138 kg/hr was the same as in Example 3. Spherical foamable polystyrene resin particles were obtained. In this embodiment 5, the extrusion starts! The value of the opening of the mold is 0.057 MPa, the mass of the resin pellet + ι granules after drying is 0.0657 g, and the opening ratio of the mold is 53.1%. The pressure at the resin introduction portion leading to the mold at the 48th hour of the private start is 1UMPa '1 〇〇 质量 质量 〇 〇 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 865 Out. For the foaming styrene resin obtained at the 48th hour of the start of extrusion, 319991 27 200916294 • Particles, and the preparation of the sample i-like volume expansion ratio 5 times (volume dense sound 〇. 〇 2 g / cm 3) The foamed and formed particles were used, and the foamed molded article having a foaming ratio of 50 times (density 〇 · 2 g of the core 3) was further produced by using the prepared expanded beads. Objective $1 to check the Μ(4), to evaluate the filling of the foaming particles. m [Comparative Example 1] A spherical polystyrene foam having a discharge amount of 138 kg/hr was used in the same manner as in Example 1 except that the mold was replaced with a mold of a known structure shown in Fig. 3. Resin particles. 3A is a cross-sectional view of the mold 31 used in Comparative Example 1, and a side view of the resin discharge surface of the third β. This mold 31 is of the same construction as the tubular heat guns 18, 19 which are arranged in a cross shape for use in the mold 1 shown in Fig. 1. /, there is the mold 1 used in Example 1 last name t this comparison example 1 t, the first hour of extrusion to the mold 3i fragrance, wide and force is 21.7Mpa high, (10) grain quality is 0.1322 carat with 31 The opening ratio is 22. 〇%. Opening: It was observed that the pressure in the resin introduction portion was increased to the crushing point; the upper limit of the pressure resistance of the wheel 31 was reached (25 Mpa), and the extrusion was stopped at the sixth hour. [Comparative Example 2] The outer layer 1 was the same as the ^1 of the mold 32 of the well-known structure, and (10) kg/hr_mountain to the spherical foaming styrene wax particles.付付 319991 28 200916294, 帛4A is a side view of the resin discharge surface of the section of the mold & used in Comparative Example 2. This mold "has the mold shown in Fig. 2! The arrangement used in the figure is ten: 'The heater 19, but the heat-generating part is not provided in the center part of the mold. In addition, the mold used in the example 1 is used.丨The same structure. Eight in this Comparative Example 2, the first hour of the start of the extrusion to the mold is 32 resin lead _ force is slightly higher 2 ^ Mpa, iqq grain, is 〇. 1030 grams The opening ratio of the mold 32 is 28.2%. "In the beginning of the growth of the resin introduction portion, the 10th hour to the i衾 grip i Q0 > The upper limit of the withstand voltage (25 Mpa), so the broadcast stopped at 10 hours. [Comparative Example 3] Spherical expandable styrene resin particles were obtained by discharging at 138 kg / hr = except that the mold 33 was held by heating with an oil as a heat medium. Fig. 5A is a cross-sectional view of a mold 33 used in Comparative Example 3, and a fifth side view showing a resin discharge surface of the mold 33. In the mold 33, the heat insulating material 21 used in the mold 1 shown in FIG. 2 is further disposed, but the flow path oil provided as the oil of the heat medium in the plate member 33 is formed from the upper and lower sides of the mold. The 埶媪Α π toilet, the dish..., the medium inlet 24 flows in, passes through the central annular flow path 1嫂, flows out from the heat medium outlet 25 provided at the left and right sides of the mold, and then returns to the structure of the oil heater. In Comparative Example 3, the pressure of the resin introduction portion to the mold 33 at the first hour of the start of the broadcast was 18, Pa, and 10. 0%。 The opening ratio of the mold 33 is 32.0%. 2%。 The dust penetration of the resin introduction portion of the mold 33 was 21.8 MPa, the mass of 100 grains was 0.0994 g, and the door opening ratio of the mold 33 was 29.2%. The foamed particles were produced at a foaming ratio of 50 times (density 〇. 〇2 This Comparative Example 3 was also the same as in Example 1). The foaming styrene resin particles obtained at the 48th hour from the start of extrusion were used to produce a volume expansion ratio Μ times. The pre-expanded particles (bulk density: 0.02 g/cm3) were further foamed to prepare the pre-foamed particle shaped limb using this preliminary preparation of 2 g/cm. The obtained foam molded body was visually observed for the filling property of the molding die. The results of Examples 1 to 5 and Comparative Examples 1 to 3 are shown in Table 319991 30 200916294 [Table 1] Comparative Example 3 Oil flow path type S ° ° jii: CNI O CO oo CO CO 18.0 · 32.0 Δ 21.8 29.2 X 0. 0994 X Setting cost is high Comparative Example 2 Heater depth 15mm O CD Ο , ” ••你C^J Ο 〇〇Λ oo CO CD C 〇〇o oo x Cn3 CNI 1H ^ w -*-{ 1 ,. •f blind 丨丨Ξ «4c Comparative example 1 No heater O CD Ο . ^ •. You CNJ O CO ^ 00 co CO 〇 〇 —· dx csa c<i τ: -Μ I , seven animals丨丨CO Example 5 Heater Depth 45nun O CD O , O · · Cup CN3 O CO ' 00 CO ψ ^ < ς〇 Bu - CO CO @ Λ Λ 18.0 40.3 〇 0. 0865 〇 Example 4 Heater Depth 30mm O CD C5 , O · · You CM O CO ^ oo CO T·^ CO C=» CS3 CD OO @ —CO Lf5 — CD CO @ — CD 0.0552 ◎ Example 3 Heater depth 15mm C=> CD O , O · • You CM O CO • oo CO CD CO OO CO CD © — oo o CQ CD @ — 卜 0. 0459 ◎ Example 2 柘 柘 g g ^ Ln 卖 甚 Ο , O , — O CO 00 co »—HC£> 16.8 82.5 ◎ 17.0 80.0 ◎ 0.0726 〇Example 1 筚μ名二W染咏O CO o . Cs3 〇CC oo CO CO <=> 〇cd σι O CO o 卜*卜· o — inch 0.0618 〇 chess structure y-v /—vy—v Single painting, very target fi τί ιιφί if 33 -35 D Stupid discharge (kg/h) Foaming agent (pentane) parts by mass Extrusion resin temperature (°C) Mold holding temperature (°c) Circulating water temperature ("c) 1st hour chess pressure (Mpa) ritual rate E (%) Evaluation of the 48th hour chess pressure (Mpa) Interval ratio E («Evaluation 48th hour 100 grain quality (g) The filling of the board with foamed particles (50 times the volume of the body) Prepared for 31 319991 200916294 From the results of Table 1, we know that this month, ^ month your household 'yoke example 1, the first hour from granulation The mold pressure is 16
Mra弟小時之模且犀六 -為17. 3 MPa，比比較例！至3 …土力 低可連續運轉。而且，喑 •嘴之開孔率在經過48小時是維持在47%。 賀 此外，實施例2至5，你袢私叫上处 攸坆粒開始第1小時之模且壓 力為13.6至16.8 MPa，笛丨π士 惧、錢 10 n a第48小時之模具壓力為13 8至 18.〇_’比比較例…低，可連續運轉。而且，喷J 之開孔率在經過！小時時是53%以上’經過則 40%以上，尤其是實施例2、3,在 才疋在 隹經過1小時時有76%以上， 在經過48小時時在76%以上，確切、閉^丨i坐丄七 的經過而變化。 確-開孔率幾乎不隨著時間 另外，加熱器深度為45咖之實施例5，相較於加敎哭 :度為30·之實施例4 ’開孔率是下降。因此可說：：： 态，未度以10至50mni為佳，更佳為15至3〇mm。 伊另一方面’在比較例卜2,可看到因噴嘴阻塞所致之 、=具壓力上昇的情形很顯著，6至1M、時程度之運轉就到 =耐壓上限。喷嘴之開孔率，在經過ι小時時 到 22. 0 至 28. 2%。 _ 比較例3與比較们、2相比，模具壓力上昇的 到抑制’開孔率也變高。不過，比較例3所用的模且犯 =實施例！相比，要在模具内設置環狀油流路，模具的構 化變複雜，且需要油的加熱器及循環泵，使油循環之配管 也需要保溫等，設置成本很高。另外，還有流路會因為劣 化的油或異物而喊，當錢難以進行時加熱平衡就會破 319991 200916294 士秋’而有無法均匀士 (^ Φ u u 也保持楔具的溫度等缺點。 I產業上的可利用性）Mra brother's model of the hour and the rhinoceros - for 17. 3 MPa, than the comparative example! Up to 3 ... low ground for continuous operation. Moreover, the opening ratio of the mouth was maintained at 47% after 48 hours. In addition, in Examples 2 to 5, you smothered the first hour of the granules and the pressure was 13.6 to 16.8 MPa. The mold pressure of the flute 丨 士 fear, money 10 na 48 hours was 13 8 To 18. 〇 _ 'lower than the comparative example... can run continuously. Moreover, the opening rate of the spray J is passing! When the hour is more than 53%', then 40% or more, especially in the second and third cases. I change by the passing of the seven. Indeed - the open cell rate hardly fluctuates over time. In addition, the heater depth is 45% of Example 5, compared to the twisting of the entanglement: the degree of opening of Example 4' is reduced. Therefore, it can be said that the ::: state is preferably 10 to 50 mni, more preferably 15 to 3 mm. On the other hand, in the comparative example 2, it can be seen that the pressure rise is caused by the nozzle clogging, and the pressure rise is significant. From 6 to 1 M, the operation of the time is up to the upper limit of the withstand voltage. The opening ratio of the nozzle is 22. 0 to 28. 2% after ι hours. _ Comparative Example 3 has a higher mold opening pressure than the comparison, and the opening ratio is also increased. However, the model used in Comparative Example 3 was made = the example! In contrast, in order to provide an annular oil flow path in the mold, the structure of the mold becomes complicated, and an oil heater and a circulation pump are required, so that the piping for the oil circulation needs to be insulated, and the installation cost is high. In addition, there are also flow paths that will be shouted by degraded oil or foreign matter. When the money is difficult to carry out, the heat balance will break. 319991 200916294 Shi Qiu' and there is no uniformity (^ Φ uu also keeps the temperature of the wedge and so on. I Industrial availability)
依照本發明，A ^ ^ γ 在乂熱切法進行熱塑性樹脂粒子的成形 _^ =造粒用模具之喷嘴阻塞，可有效率地生產粒 圖 圖式簡單說明】 第1圖係顯示本 發明之造粒裝置之構成的一個例子 第2A圖係本發明之生 a 月之化粒用杈具之一貫施形態中的造 粒用核具的斷面圖。 弟2B圖係顯示本發明生 + ¾月之以粒用杈具之一實施形態中 勺k粒用模具的樹脂排出面之側面圖。 第3A圖係比較例j中用的模具斷面圖。 第3B圖係顯示比較例1中用 面圖 平乂灼i T用的杈具之樹脂排出面的側 面圖 第4A圖係比較例2中用的模具斷面圖。 第4B圖係顯示比較例2中用的模具之樹雜 排出面的側 第5A圖係比較例3申用的模具斷面圖。 圖。 第5 B圖係顯示比較例3中用的模具之樹月旨排出面側面 第6A圖係本發明之造粒用模具之其他實施形 造粒用模具斷面圖。 心 態 苐（3B圖係顯示本發明之造粒用模具之其他實施形 319991 200916294 中的造粒用模具的樹脂排 【主要元件符號說明】 1、41造粒用模具 3 料斗 5 高壓泵 7 切斷器 9 水槽 11 管路 13 模座 15 螺栓 17 喷嘴 20 短加熱器 22 樹脂排出面 24 熱媒入d 出面之側面圖。 2 播製機 4 發泡劑供給口 6 腔室 8 送水泵 10 脫水處理部 12 容器 14 含有發泡劑的樹脂 16 樹脂流路 18、 19、48、49管式加熱 21 隔熱材 23 流路 25 熱媒出口 50(50A至50D)測溫體 31、32、33 模具According to the present invention, A ^ ^ γ is formed by forming a thermoplastic resin particle by a hot-cutting method, and is blocked by a nozzle of a granulation mold, and can efficiently produce a granular pattern. An example of the configuration of the granulating device Fig. 2A is a cross-sectional view of the granulation nucleus in the conventional embodiment of the granules for granules of the present invention. Fig. 2B is a side view showing the resin discharge surface of the k-grain mold in the embodiment of the pellet cooker according to the present invention. Fig. 3A is a cross-sectional view of the mold used in Comparative Example j. Fig. 3B is a side view showing the resin discharge surface of the cookware for use in Comparative Example 1. Fig. 4A is a cross-sectional view of the mold used in Comparative Example 2. Fig. 4B is a view showing the side of the discharge surface of the mold used in Comparative Example 2. Fig. 5A is a cross-sectional view of the mold applied in Comparative Example 3. Figure. Fig. 5B is a side view showing the side of the discharge surface of the mold used in Comparative Example 3. Fig. 6A is a cross-sectional view showing another embodiment of the granulation mold of the present invention. Mental state 苐 (3B diagram shows the resin row of the granulation mold in the other embodiment of the granulation mold of the present invention 319991 200916294 [Main element symbol description] 1, 41 granulation mold 3 hopper 5 high pressure pump 7 cut 9 Sink 11 Pipe 13 Mold base 15 Bolt 17 Nozzle 20 Short heater 22 Resin discharge surface 24 Side view of the heat medium into the d. 2 Seeding machine 4 Foaming agent supply port 6 Chamber 8 Water pump 10 Dehydration treatment Portion 12 Container 14 Resin containing foaming agent 16 Resin flow path 18, 19, 48, 49 Tube heating 21 Heat insulating material 23 Flow path 25 Heat medium outlet 50 (50A to 50D) Temperature measuring body 31, 32, 33 Mold
L 加熱益深度（從樹脂排出面到管式加熱器的中心部 之距離） 319991 34L Heat benefit depth (distance from the resin discharge face to the center of the tube heater) 319991 34