201221635 六、發明說明： 【發明所屬之技術領域】 本發明係關於-種生質原料之快迷熱解 法’尤指-種可量產製造液態生質油之快速熱解反應系統。 【先前技術】 近年來國際能源（特別是石油）價格 上 、q盈向漲：，且能 源需求亦曰趨緊張。台灣的天然資源極戶斤<201221635 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a rapid pyrolysis reaction system for producing a raw material, particularly a rapid pyrolysis reaction system for producing a liquid crude oil. [Prior Art] In recent years, international energy (especially oil) prices have risen and q has increased: and energy demand has become increasingly tense. Taiwan’s natural resources are extremely heavy
又H乏，JQ^章及民 生所需的能源幾乎全數仰賴進口，因此，^ 對於任何形式之 再生能源之開發益形重要。再生能源是—種、綠色&、， 危害環境污染，其中又以生質原料咖邮叫最適 液體燃料及化學物品。生質原料包含各類有機廢棄物，如： 農業或林業廢棄物、廚餘、動物排泄物、廢輪胎..等所 製成的液體燃料，又稱為生質油（bio-oil)，可進—步提煉成 高價值的燃料，如生質柴油(bio-diesel)。此種將生質原料轉 化為生質油之製程技術’不僅可將廢棄物轉換為寶貴的能 源’且可達到能源再生及再利用之經濟效益與廢棄物減量 之環保目的，可謂一舉兩得。 目前轉化生質原料之技術可大致可區分如下： 1_生物/化學轉換(bio/chemical conversion):如經發酵 (fermentation)、S旨化（esterification)等程序產生酒精 汽油（gasohol)、沼氣(bio-gas)或生質柴油；或利用生 物菌種等方法產生氫氣、曱醇等燃料。 2·熱轉換（thermal conversion):如以直接燃燒（direct 201221635 combustion) ^ ^ ^(Pyrolysis)^^ ^b(gasificati〇n)；r 式，產生合成燃氣(syngas)或燃油等。 其中熱解技術主要係指由固態之生質原料或廢棄物， 直接經無氧熱裂解(thermal Pyr〇lySis)製成液態燃料，其程 序又稱為液化(liquefaction)。若經適當的純化過程，液態燃 料之熱值可有效提昇’增加其利目前發展的快速熱 解(fast pyrolysis)技術係在高溫、缺氧狀態下，快速加熱生 質原料或廢棄物形成氣體及固悲焦炭，將所產生的氣體快 速冷凝，以獲得生質油；另外，所得到之固態焦炭經進一 步處理可獲得高附加價值的化學品。快速熱解的主要操作 溫度略高於傳統熱解方法’約在450。〇至6〇〇。〇之間，停滞 時間則小於1秒。由於快速升溫、迅速冷卻，可避免二次 熱解(cracking) ’因此，可獲取液體產量約6〇〜75 wt〇/〇。 使用熱解技術產製之衍生燃油的優點為，具高熱值且 運儲方便’可作為鋼爐之輔助燃料或直接使用於發電機， 符合廢料再利用與潔淨生產之環保與經濟效益。生質原料 或廢棄物熱解生產合成燃油的技術，目前雖未完全商業 化，但快速熱解技術將是未來的發展趨勢。 國外已發展之快速熱解反應器有旋風式反應器（vortex reactor)、攜帶床反應器（entrained flow reactor)、旋轉錐反 應器（rotating cone reactor)、真空移動床（vacuum transported bed)、循環流化床(circulating fluid bed)等多種。目前快速 熱解反應系統可產出液態生質油50〜75 wt%、焦炭15〜25 wt%及不冷凝氣體10〜20 wt%，但快速熱解反應設備仍存在 201221635 一些缺點，如能量耗損大、價格昂貴、設備擴大困難、熱 載體（砂）與生質原料需要通入氮氣進行流化、熱載體與 焦炭(char)分離不易、進料易發生懸料、掛料或凝結成塊造 成阻塞等問題。 因此，如何開發出一種生質原料熱解系統，以改善習 知技術之缺點，並降低熱解系統之製造成本及提昇生產效 率與生質油品質，是本發明所欲揭露之處。 ®【發明内容】 發明人有感於上述習知快速熱解反應系統之未臻完 善，遂竭其心智悉心研究克服，憑其從事該項技術研發多 年之經驗，進而開發出一種生質原料轉化為生質油之快速 熱解系統及其方法，以期達到降低製造成本及提昇生產效 率與生質油品質之目的。 為達上述目的，本發明提供一種生質原料熱解系統， • 其包含：一進料裝置；一控制驅動裝置，係用於控制該生H is lacking, and the energy required for JQ^ and the people's livelihood is almost entirely dependent on imports. Therefore, it is important for the development of any form of renewable energy. Renewable energy sources are “green”, “green” and “environmental pollution”. Among them, raw materials are used to call the most suitable liquid fuels and chemicals. Biomass raw materials include various types of organic waste, such as: agricultural or forestry waste, kitchen waste, animal waste, waste tires, etc., which are also known as bio-oil. Further step into a high-value fuel, such as bio-diesel. This process technology for converting raw materials into raw oils not only converts waste into valuable energy, but also achieves the environmental benefits of energy recovery and reuse and the environmental impact of waste reduction. At present, the technology for converting raw materials can be roughly divided into the following: 1_bio/chemical conversion: if gasoline, gasoline, biogas are produced by processes such as fermentation, esterification, etc. Bio-gas) or biodiesel; or a method such as a biological strain to produce a fuel such as hydrogen or sterol. 2. Thermal conversion: If direct combustion (direct 201221635 combustion) ^ ^ ^ (Pyrolysis) ^ ^ ^ b (gasificati〇n); r formula, produce synthetic gas (syngas) or fuel. Among them, pyrolysis technology mainly refers to solid fuel raw materials or waste, which is directly made into liquid fuel by thermal pyr〇lySis. The procedure is also called liquefaction. If properly purified, the calorific value of the liquid fuel can be effectively improved. 'The rapid pyrolysis technology that is currently developing is fast heating the raw material or waste forming gas under high temperature and anoxic conditions. Solid coke, the gas produced is quickly condensed to obtain a raw oil; in addition, the obtained solid coke is further processed to obtain a high value-added chemical. The main operating temperature for rapid pyrolysis is slightly higher than the traditional pyrolysis method 'about 450. 〇 to 6〇〇. Between 〇, the stagnation time is less than 1 second. Due to rapid temperature rise and rapid cooling, secondary cracking can be avoided. Therefore, liquid production of about 6 〇 to 75 wt 〇 / 可 can be obtained. The advantages of using derivative fuels produced by pyrolysis technology are high calorific value and convenient storage. It can be used as an auxiliary fuel for steel furnaces or directly used in generators, in line with the environmental and economic benefits of waste recycling and clean production. The technology of raw material or waste pyrolysis to produce synthetic fuel is not fully commercialized at present, but rapid pyrolysis technology will be the future development trend. The rapid pyrolysis reactors developed abroad include a vortex reactor, an entrained flow reactor, a rotating cone reactor, a vacuum transported bed, and a circulation. A variety of circulating fluid beds and the like. At present, the rapid pyrolysis reaction system can produce 50 to 75 wt% of liquid biomass oil, 15 to 25 wt% of coke, and 10 to 20 wt% of non-condensable gas, but the rapid pyrolysis reaction equipment still has some disadvantages such as energy loss in 201221635. Large, expensive, difficult to expand equipment, heat carrier (sand) and raw materials need to be nitrogened for fluidization, heat carrier and coke (char) separation is not easy, feeding is prone to suspension, hanging material or condensation into a block Blocking and other issues. Therefore, how to develop a biomass raw material pyrolysis system to improve the disadvantages of the prior art, reduce the manufacturing cost of the pyrolysis system, and improve the production efficiency and quality of the raw oil is the disclosure of the present invention. ® [Invention] The inventor felt that the above-mentioned rapid pyrolysis reaction system was not perfected, exhausted his mental research and overcoming, and based on his years of experience in the research and development of this technology, he developed a raw material conversion. It is a rapid pyrolysis system and method for producing raw oil, in order to achieve the purpose of reducing manufacturing cost and improving production efficiency and quality of raw oil. To achieve the above object, the present invention provides a raw material pyrolysis system, which comprises: a feeding device; a control driving device for controlling the raw
I 質原料之送料速率；一熱解反應裝置，係用於快速熱解該 生質原料；一氣體/固體分離裝置，係用於分離該生質原料 熱解後所產生之氣體及固體；一觸媒脫氧裝置，係用於添 加觸媒同步進行生質油之催化反應，以提升生質油之熱 值；以及一冷凝裝置，係用於冷凝該分離後之氣體，以生 成液態生質油及不冷凝氣體。上述之系統，其中，進一步 包含一溫度監控裝置，係用於控制該生質原料之熱解溫度。 上述之系統，其中，該進料裝置係包含一儲料斗、一 201221635 攪拌裝置、一送料裝置。 驅動器 上述之系統，其中，該授掉裝置係包含 撓性元件及一曲柄擺動轴。 上述之系統，其中，該送料裳置係包含一驅動器、一 撓性元件及一送料螺桿。 上述之系統，其中，當生質原料進入該儲料斗時，今 驅動器係以該換性㈣帶動—曲柄擺動軸，同時另= 元件帶動另-送料螺桿，並將生質原料送人熱解反應裝置。 上述之系統，其中’該控制驅動裝置係包含-驅動器、 -撓性7C件、-推拔式平方導螺桿及—控制器。 上述之系統，其巾，該驅動^細該撓性元件談 推^式平方導螺桿進行送料，並㈣控制11控制該驅動器 之轉速。 上述之系統’其中 上述之糸統’其中 上述之系統，其中 上述之系統，其中 該驅動器係一減速機馬達。 該撓性元件係一鏈條。 该控制器係一變頻控制器。 該導螺桿係推拔式平方等節距。 上述之系統其中，該導螺桿進一步包含二陶兗軸承， 用於支撐、固定及傳動。 述之系先《中，該導螺桿之材質係耐高溫、抗氧 化及低熱膨脹係數之球墨鑄鐵。 上述之系統，其中，該熱解反應襄置係包含一燃燒器 及一生成氣體儲存槽。 上述之系統’其中，該燃燒器係以不錄鋼管彎製成圓 201221635 形，且在圓管之每90度位置處鑽孔，並設置爐頭、爐嘴及 連接管。 上述之系統，其中，該氣體/固體分離裝置係一漩風機。 上述之系統，其中，該漩風機之氣體輸出管路係深入 該旋風機内部。 上述之系統，其中，該觸媒脫氧裝置，係用於添加觸 媒同步進行生質油之催化反應。 上述之系統，其中，該冷凝裝置係一液體冷凝器。 本發明另提供一種熱解生質原料以生成液態生質油之 方法，其係使用上述之系統，並控制熱解溫度為460〜600 °C，送料之轉速為15〜30 rpm，冷凝溫度為5°C以下。 藉此，本發明之生質原料熱解系統及方法，藉由整合 控制驅動裝置、熱解反應裝.置、氣體/固體分離裝置及觸媒 脫氧裝置，可達到縮小設備體積、提升生產效率及產品品 質、降低熱解設備製造成本之功效。 【實施方式】 為充分暸解本發明之目的、特徵及功效，茲藉由下述 具體之實施例，並配合所附之圖式，對本發明做一詳細說 明如後： 請參考第1圖，其為本發明較佳具體實施例之示意圖， 顯示一種生質原料快速熱解系統，其包含：一進料裝置1， 係用於連續提供生質原料；一控制驅動裝置2,係用於控制 該生質原料之送料速率；一熱解反應裝置3，係用於熱解該 201221635 生貝原料，—氣體/固體分離裝置4，係用 質原料後羞生之氣體及固體；一觸錢氣用於分離熱解該生 加觸媒同步進行生質油之催化反應，裝f5,係用於添 體。 之孔體以生成液悲生質油及不冷凝氣 /熱解系統進一步包含一不冷凝 以儲存該不冷凝氣體，可供作為合成嫉^收儲筒7,係用 供給裝置8,係用以供給該熱解反應裳置^燃料；一燃料 源’如使用瓦斯作為燃燒之燃料；—3錢時之燃料來 供該冷凝裝置6之冷凝水，如使用冰=欠槽9,係用以提 用馬達將冰水“該冷凝裝置6，_= 水，且利 下’然後冰水再回到該冷凝水槽9内:冷凝溫度為穴以 控裝置7系用於控制該生質原料之熱::；及一溫度監 以下進—步詳細說明，本發明之#^ 皿度。 要元件及功能。 权隹具體實施例的主 掉裝係利用一授 縣置可贱Μ質原料蚊反應裝置3。該授 在傳統•中_筒易形成dn 進料不穩定氣供科停頓等問題。#壁掛料，而導致 控制驗動裂12:請參考 m包含：一驅動m 一驗及^圖，該控制驅動 導螺桿20反一控㈣u = 12、一推拔式平方 8 201221635 拔式平方導螺桿20送料，另以變頻器作為控制器13，以控 制減速機馬達之轉速；而且該推拔式平方導螺桿20可利用 二個陶瓷轴承及防熱墊片，以支撐、固定及傳動，並達到 隔熱與提升氣體防漏之目的。又該推拔式平方導螺桿20的 材質為自行研發之耐高溫、抗氧化及低熱膨脹係數之球墨 每鐵’有利於南溫熱解生質原料時之傳送，並避免向溫麵 曲變形之問題。 熱解反應裝置3 :請參考第1圖及第3圖，該熱解反應 * 裝置3係由數支燃燒器21所組合而成，其中該燃燒器21 係以不鏽鋼管彎製成圓形，並在圓管之每90度位置處鑽 孔，再組裝快速爐頭、爐嘴及連接管所組成之加熱燃燒器， 其優點為高溫加熱均勻及升溫速率快速。 氣體/固體分離裝置4:由於熱解產生的揮發分氣體中 含有少量焦炭(char)及灰分(ash)，若未適當的分離，常會造 成管路系統的阻塞，焦炭與灰分中碳會產生二次熱解現 φ 象，影響了生質油的產量及增加不冷凝氣體的生成。一般 分離的方法是利用漩風機，將揮發分氣體以切線方向吹入 具有錐形底的圓桶23中，將帶有焦炭和灰分拋向外周，與 器壁碰撞後由圓桶23之錐形底下部的出口排出，揮發分氣 體則由圓桶23中心之氣體輸出管路22之開口端排出，該 漩風機之氣體輸出管路22係深入該旋風機内部，以避免焦 炭及灰份進入氣體輸出管路22，請參考第4圖。 觸媒脫氧裝置5:分離後之揮發分氣體，再利用線上添 加觸媒同步進行生質油之催化反應，將揮發分氣體中的氧 201221635 去除，以提升生質油之熱值，請參考第4圖。 冷凝裝置6:熱解產生的揮發分氣體在冷凝條件下，將 快速生成液態生質油及不冷凝氣體。但熱解所產生的揮發 分氣體到冷凝階段的溫度及時間，都直接影響到生質油的 產量和成份，因揮發分氣體與生質油在高溫條件下，易造 成二次熱解的發生，使得不冷凝氣體的生成愈多，大大降 低了生質油的產量。本發明之冷凝裝置6可利用液態冷凝 水，快速冷凝揮發分氣體，其冷凝溫度控制在5°C以下，以 提高液態生質油之產量。 生質原料快速熱解之實施例 以下進一步說明，利用本發明之生質原料轉化為生質 油之快速熱解設備系統，進行生質原料熱解實驗之步驟及 製程參數。 生質原料快速熱解液化成生質油，其製程參數的選取 是影響其反應效率與產能的主要關鍵。一般造成生質油產 能低的最主要因素包含：熱解溫度太高、升溫速率太慢、 揮發分氣體停留時間過長以及冷凝時間太長等，導致揮發 分氣體產生二次熱解之生成物皆為不冷凝氣體。另一方面 生質油成分中含水量和氧量過高時，也是降低熱值、燃燒 點和成分性質不穩定的原因。 1.生質原料粒徑：為了提高加熱速率，獲得更高的產 能，生質原料經粉碎後的顆粒大小就相當重要，當粒徑小 於1 mm時，熱解過程屬於動力學反應機制；當粒徑大於1 mm時，熱解過程即屬於傳熱和傳質控制，所以粒徑大小是 201221635 衫響熱解反應過程的重眷因去 時，並生曾㈣其 當粒#尺寸超過某一範圍 揮發性擴散較慢，氣相產物停留顆粒大時，内部 被熱解為小分子的篆氣。因長’使得更多的生質油 语祖^ 因此，實施例採用樟樹作為生質 原枓’，、粒役參數水準設^ l.Gmm以下。 低導致It料乾燥.當生質油含水量過高時’熱值會降a feed rate of the raw material; a pyrolysis reaction device for rapidly pyrolyzing the raw material; a gas/solid separation device for separating gas and solid generated after pyrolysis of the raw material; The catalyst deoxidizing device is used for adding a catalyst to simultaneously perform a catalytic reaction of the raw oil to increase the calorific value of the raw oil; and a condensing device for condensing the separated gas to form a liquid raw oil And no condensation gas. The above system, further comprising a temperature monitoring device for controlling the pyrolysis temperature of the raw material. The above system, wherein the feeding device comprises a storage hopper, a 201221635 stirring device, and a feeding device. Drive The system described above, wherein the transfer device comprises a flexible member and a crank swing shaft. The system described above, wherein the feed skirt comprises a driver, a flexible member and a feed screw. The above system, wherein when the raw material enters the storage hopper, the actuator is driven by the transducing (four)-cranking shaft, and the other element drives the other-feeding screw, and the raw material is sent to the pyrolysis reaction. Device. The above system, wherein the control drive comprises a driver, a flexible 7C member, a push-pull square lead screw and a controller. In the above system, the towel is driven to feed the flexible member, and (4) the control 11 controls the rotational speed of the driver. The above system, wherein the above system is the system described above, wherein the drive is a reducer motor. The flexible element is a chain. The controller is a variable frequency controller. The lead screw is a push-pull squared pitch. In the above system, the lead screw further comprises two ceramic bearings for supporting, fixing and driving. In the first chapter, the material of the lead screw is a ductile iron with high temperature resistance, oxidation resistance and low coefficient of thermal expansion. The above system, wherein the pyrolysis reaction system comprises a burner and a generating gas storage tank. In the above system, the burner is formed into a round shape of 201221635 by a non-recorded steel pipe, and is bored at every 90 degrees of the circular pipe, and is provided with a burner, a nozzle and a connecting pipe. The above system, wherein the gas/solids separation device is a cyclone. In the above system, the gas output line of the cyclone is deep inside the cyclone. In the above system, the catalyst deoxidizing device is used for adding a catalyst to simultaneously perform a catalytic reaction of a raw oil. The above system, wherein the condensing device is a liquid condenser. The invention further provides a method for pyrolyzing raw material to form liquid raw oil, which uses the above system, and controls the pyrolysis temperature to be 460~600 °C, the feeding speed is 15~30 rpm, and the condensation temperature is Below 5 °C. Thereby, the biomass raw material pyrolysis system and method of the invention can reduce the volume of the device and improve the production efficiency by integrating the control driving device, the pyrolysis reaction device, the gas/solid separation device and the catalytic deoxidation device. Product quality, reducing the cost of pyrolysis equipment manufacturing costs. DETAILED DESCRIPTION OF THE INVENTION In order to fully understand the objects, features and effects of the present invention, the present invention will be described in detail by the following specific embodiments and the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS A schematic diagram of a preferred embodiment of the present invention, showing a rapid pyrolysis system for raw material, comprising: a feeding device 1 for continuously supplying raw material; and a control driving device 2 for controlling the Feeding rate of raw material; a pyrolysis reaction device 3 for pyrolyzing the raw material of 201221635 raw material, gas/solid separation device 4, gas and solid after shampooing with raw materials; Separation pyrolysis The raw catalyst is simultaneously subjected to catalytic reaction of the raw oil, and f5 is used for the addition. The pore body further comprises a non-condensing gas and a non-condensing gas/pyrolysis system to store the non-condensable gas, and is used as a synthetic storage tank 7 and is provided with a supply device 8 for Supplying the pyrolysis reaction to the fuel; a fuel source 'such as using gas as a fuel for combustion; - 3 money for the condensate of the condensing device 6, such as using ice = under-slot 9, for lifting The chilled water "the condensing device 6, _= water, and the profit" is then charged by the motor and then the ice water is returned to the condensing water tank 9: the condensing temperature is the hole control device 7 is used to control the heat of the raw material: The following is a detailed description of the temperature of the present invention. The components of the present invention are used in the main components of the present invention. The grant is in the traditional • medium _ tube easy to form dn feed unstable gas for the company to stop the problem. #壁挂料, resulting in control inspection crack 12: Please refer to m contains: a drive m a test and ^ map, the Control drive lead screw 20 reverse one control (four) u = 12, a push-pull square 8 201221635 pull-type square lead screw 20 send In addition, the frequency converter is used as the controller 13 to control the rotation speed of the speed reducer motor; and the push-type square lead screw 20 can utilize two ceramic bearings and a heat-proof gasket to support, fix and transmit, and achieve heat insulation. The purpose of the push-type square lead screw 20 is that the self-developed high-temperature, anti-oxidation and low thermal expansion coefficient of the spheroidal ink per iron is beneficial to the transfer of the raw material during the south temperature pyrolysis of the raw material. And avoiding the problem of deformation to the warm surface. Pyrolysis reaction device 3: Please refer to Fig. 1 and Fig. 3, the pyrolysis reaction device 3 is composed of a plurality of burners 21, wherein the burner 21 The stainless steel pipe is bent into a circular shape, and the hole is drilled at every 90 degrees of the round pipe, and then the heating burner composed of the quick burner, the nozzle and the connecting pipe is assembled, and the advantages thereof are high temperature heating uniformity and heating rate. Rapid gas/solid separation device 4: The volatile gas generated by pyrolysis contains a small amount of char (char) and ash (ash). If not properly separated, it will often cause blockage of the pipeline system, and carbon in coke and ash will Generate secondary heat The current φ image affects the production of raw oil and increases the formation of non-condensable gas. The general separation method is to use a cyclone to blow the volatile gas into the drum 23 with a conical bottom in a tangential direction. The coke and the ash are thrown to the outer circumference, and are collided with the wall to be discharged from the outlet of the lower portion of the conical bottom of the drum 23, and the volatile gas is discharged from the open end of the gas output line 22 at the center of the drum 23, the gas of the cyclone The output line 22 is deep inside the cyclone to prevent coke and ash from entering the gas output line 22. Please refer to Figure 4. Catalyst deoxidizer 5: Dissociated volatile gas, then add catalyst on the line to synchronize The catalytic reaction of the raw oil is carried out, and the oxygen 201221635 in the volatile gas is removed to increase the calorific value of the raw oil, please refer to Fig. 4. Condensing unit 6: The volatile gas generated by pyrolysis will rapidly form liquid biomass oil and non-condensable gas under condensing conditions. However, the temperature and time of the volatile gas generated by pyrolysis to the condensation stage directly affect the yield and composition of the raw oil, because the volatile gas and the raw oil are liable to cause secondary pyrolysis under high temperature conditions. Therefore, the more non-condensed gas is generated, the production of bio-oil is greatly reduced. The condensing device 6 of the present invention can utilize liquid condensate to rapidly condense volatile gases, and the condensation temperature is controlled below 5 ° C to increase the yield of liquid biomass oil. Examples of Rapid Pyrolysis of Biomass Raw Materials The following further explains the steps and process parameters of the pyrolysis test of the raw material using the raw material of the present invention converted into a rapid pyrolysis equipment system for the raw oil. The raw materials are rapidly pyrolyzed into liquefied oils, and the selection of process parameters is the main key factor affecting their reaction efficiency and productivity. The most important factors causing low productivity of raw oil include: too high pyrolysis temperature, too slow heating rate, too long residence time of volatile gas, and too long condensation time, resulting in secondary pyrolysis of volatile gas. All are non-condensable gases. On the other hand, when the water content and the oxygen content in the raw oil component are too high, the calorific value, the burning point, and the compositional properties are unstable. 1. Particle size of raw material: In order to increase the heating rate and obtain higher productivity, the particle size of the raw material after pulverization is very important. When the particle size is less than 1 mm, the pyrolysis process belongs to the kinetic reaction mechanism; When the particle size is larger than 1 mm, the pyrolysis process belongs to heat transfer and mass transfer control, so the particle size is 201221635. When the heat reaction process of the sizzling reaction is repeated, the granules are more than a certain size. The range of volatile diffusion is slower, and when the gas phase product stays large, the interior is pyrolyzed into small molecules of helium. Because of the long term, more ginseng oil is used. Therefore, the example uses eucalyptus as the raw material 枓', and the granule parameter level is below l.Gmm. Low causes the It material to dry. When the water content of the raw oil is too high, the calorific value will drop.
隼=!:質且會树路及收集器，故必須先將 料乾燥’較佳係將其含水量控财丨"。以 3下；=，實施例採用樟樹作為生質原料，其乾燥時間約 j〜/小時。 3·進料與輸送逮率··進料穩定與輸送速率會影塑執解 反應之生質油產值，而實施例採用樟樹作為生質原：時之 送料轉速設定為15〜3〇 rpm，較佳為2()〜25 rpm。 4·熱解溫度··在低溫慢速熱解溫度低於3贼時，分解 產物大都以焦炭為主；當中溫閃速(l_°C/s)且熱解溫度控 制在460 600 C時’生質原油的生成車交高，可達到％〜75 wt%，當咼溫快速熱解溫度為7〇〇〜12〇〇(5c時，其生成物以 不冷凝氣體居多。實施例採用樟樹作為生質原料，熱解溫 度控制在460〜560。(：之間，測試結果如表！所示。 201221635 表1 :生質原料樟樹在不同熱解溫度之測試結果 生質原料 粒徑 溫度 (°C) 產量（wt%) 液態生質油 焦炭 不冷凝氣體 1.0 mm (Mesh 16) 460 38.8 24.9 36.3 480 42.3 23.8 33.9 500 49.6 23.1 27.3 520 39.5 22.1 38.4 540 38.1 21.0 40.9 560 37.4 19.2 43.4 0.85 mm (Mesh 20) 400 20.0 61.3 18.7 450 50.7 30.2 19.1 470 58.2 24.0 17.8 500 51.6 23.1 25.3 550 48.9 20.4 30.7 0.60 mm (Mesh 28) 400 20.5 58.9 20.6 450 46.7 41.3 12.0 470 60.4 27.2 12.4 500 51.1 26.7 22.2 550 49.8 20.4 29.8 0.425 mm (Mesh 35) 400 14.3 66.1 19.6 450 25.5 53.6 20.9 470 40.9 37.8 21.3 500 50.2 27.6 22.2 550 47.6 23.1 29.8隼=!: Quality and will be used for trees and collectors, so it is necessary to dry the material first, and it is better to control its water content. Taking 3 times; =, the example uses eucalyptus as a raw material for raw materials, and the drying time is about j~/hour. 3. Feeding and conveying rate ·· Feed stability and conveying rate will affect the production value of the raw oil, and the example uses eucalyptus as the raw material: the feeding speed is set to 15~3〇rpm. It is preferably 2 () to 25 rpm. 4. Pyrolysis temperature · When the low temperature slow pyrolysis temperature is lower than 3 thieves, the decomposition products are mostly coke; the intermediate temperature flash (l_°C/s) and the pyrolysis temperature is controlled at 460 600 C' The production of raw crude oil is high, which can reach %~75 wt%. When the rapid pyrolysis temperature is 7〇〇~12〇〇 (5c, the product is mostly non-condensable gas. The example uses eucalyptus as the Raw material, pyrolysis temperature is controlled at 460~560. (:, the test results are shown in the table! 201221635 Table 1: Raw material raw material eucalyptus test results at different pyrolysis temperatures Biomass raw material particle size temperature (° C) Yield (wt%) Liquid Biomass Oil Coke Non-condensable Gas 1.0 mm (Mesh 16) 460 38.8 24.9 36.3 480 42.3 23.8 33.9 500 49.6 23.1 27.3 520 39.5 22.1 38.4 540 38.1 21.0 40.9 560 37.4 19.2 43.4 0.85 mm (Mesh 20 400 20.0 61.3 18.7 450 50.7 30.2 19.1 470 58.2 24.0 17.8 500 51.6 23.1 25.3 550 48.9 20.4 30.7 0.60 mm (Mesh 28) 400 20.5 58.9 20.6 450 46.7 41.3 12.0 470 60.4 27.2 12.4 500 51.1 26.7 22.2 550 49.8 20.4 29.8 0.425 mm ( Mesh 35) 400 14.3 66. 1 19.6 450 25.5 53.6 20.9 470 40.9 37.8 21.3 500 50.2 27.6 22.2 550 47.6 23.1 29.8
本發明藉由整合控制驅動裝置、熱解反應裝置、氣體/ 固體分離裝置及觸媒脫氧裝置，可達到縮小設備體積、提 升生產效率及產品品質、降低熱解設備製造成本之功效； 就產業上的可利用性而言，利用本發明所衍生的產品，當 可充分滿足目前市場的需求。如上所述，本發明完全符合 專利三要件：新穎性、進步性和產業上的可利用性。 本發明在上文中已以較佳實施例揭露，然熟習本項技 術者應理解的是，該實施例僅用於描繪本發明，而不應解 12 201221635 讀為限制本發明之範圍。應注意的是，舉凡與該實施例等 效之變化與置換，均應設為涵蓋於本發明之範疇内。因此， 本發明之保護範圍當以下文之申請專利範圍所界定者為 準。 【圖式簡單說明】 第1圖為本發明較佳具體實施例之示意圖。 第2圖為本發明較佳具體實施例進料裝置之示意圖。 第3圖為本發明較佳具體實施例控制驅動裝置及熱解 反應裝置之示意圖。 第4圖為本發明較佳具體實施例氣體/固體分離裝置及 觸媒脫氧裝置之示意圖。 【主要元件符號說明】 1 進料裝置 2 控制驅動裝置 3 熱解反應裝置 4 氣體/固體分離裝置 5 觸媒脫氧裝置 6 冷凝裝置 7 不冷凝氣體回收儲筒 8 燃料供給裝置 冷凝水槽 溫度監控裝置 13 10 201221635 11 驅動器 12 撓性元件 13 控制器 14 曲柄擺動轴 15 驅動器 16 撓性元件 17 驅動器 18 撓性元件 19 送料螺桿 20 推拔式平方導螺桿 21 燃燒器 22 氣體輸出管路 23 圓桶 14By integrating the control driving device, the pyrolysis reaction device, the gas/solid separation device and the catalytic deoxidizing device, the invention can achieve the effects of reducing the volume of the device, improving the production efficiency and product quality, and reducing the manufacturing cost of the pyrolysis device; In terms of availability, the products derived from the present invention can fully satisfy the needs of the current market. As described above, the present invention fully complies with the three requirements of the patent: novelty, advancement, and industrial applicability. The invention has been described above in terms of preferred embodiments, and it is understood by those skilled in the art that the present invention is only intended to depict the invention and is not intended to be construed as limiting the scope of the invention. It should be noted that variations and permutations that are equivalent to the embodiments are intended to be within the scope of the present invention. Therefore, the scope of the invention is defined by the scope of the following claims. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view of a preferred embodiment of the present invention. Figure 2 is a schematic view of a feeding device in accordance with a preferred embodiment of the present invention. Fig. 3 is a schematic view showing a control driving device and a pyrolysis reaction device according to a preferred embodiment of the present invention. Figure 4 is a schematic view of a gas/solids separation apparatus and a catalyst deoxidation apparatus according to a preferred embodiment of the present invention. [Description of main components] 1 Feeding device 2 Control drive device 3 Pyrolysis reaction device 4 Gas/solids separation device 5 Catalytic deoxidation device 6 Condensing device 7 Non-condensing gas recovery storage tank 8 Fuel supply device Condensation tank temperature monitoring device 13 10 201221635 11 Drive 12 Flexible element 13 Controller 14 Crank pivoting shaft 15 Actuator 16 Flexible element 17 Actuator 18 Flexible element 19 Feed screw 20 Push-out squared lead screw 21 Burner 22 Gas output line 23 Drum 14