200808949 九、發明說明·· 【發明所屬之技術領域】 將生關：種再生能源產生裝置，尤其是指-種 二種：：此：進仃混切循環以加速反應產生生質能源之 種生質柴油提煉裝置。 【先前技術】 用、^ Γί油因具不需修改柴油引擎系統即可直接添加信 去上低 、鬲十六烷值等多項優點，故其提煉技術一i 2源=程重要的研究發展方向。目前生質柴油的製造;$ 程力驗製程、酸製程、酵素製程以及超臨界曱醇靠 而超臨界甲二^ 及抓C以上的高壓二2 = 7需要在46^ 阿，里衣丨兄下反應，且每一抵々姦能的 為5ml，無法大量生產製造。 母批-人產此力 (t⑽tel柴油f提煉方法嶋使用的即為轉酯化技術 化劑不同，細分為強驗、強酸、 5354878)， f產使用，唯-不同的是所採用的原料油因it不:廣： 含量的籽油，美國則是使用癸花油等高油脂 疋使用大丑油來進行反應、日本因地 200808949 • 狹人稠’油脂成本較南’故回收廢油炸油來進行轉醋化反 應。四種轉1旨化製程相較如下所示： 首先是強驗與強酸製程的比較’使用相同比例的催化 劑進行轉酯化反應時發現，強鹼製程花費1小時即可完成 反應，但強酸製程依其所添加的醇類不同，需花費3〜69小 . 時不等的時間；若以油脂與醇類的莫耳比率來看，強驗製 程需要1 · 6莫耳即達到9 0 %以上的轉化率，而強酸製程卻 需要1 : 30莫耳方可達到相同的轉化率，較高的莫耳比率 φ 將提高醇類的使用量，相對的生產成本也將大幅上升。〔β Freedman, Ε· H. Pryde and Τ· L· Mounts, nVariables affecting the yields of fatty esters from transesterified vegetable oils', Journal 〇f American Oil Chemist’s Society, Vol. 61， pp. 1638-1643 1984.] 強鹼製程雖然可以將反應時間縮短至i小時，但僅偈 限於實驗室級的微量樣品製造方可達到，若以相同的添加 φ 比例擴大至工廠大量生產時’即可發現攪拌馬達在量產混 合攪:摔時’常因轉速、層流現象以及檟;摔死角過多，而無 ’ 法上下混合、均勻攪拌反應，為達90%以上的反應率，常 ， 需將反應時間需要拉長3至4小時，此舉將嚴重影響工廠 產能。〔Y· Zhang，M· A· Dube，D· D· McLean, M. Kates， "Biodiesel production from waste cooking • oil:L Process design and technological assessment", ， Bioresource Technology, Vol. 89, pp. 1-16,2003.〕 以酯解酵素當成生物催化劑使用是近幾年來生質柴油 200808949 • 匆展的方向之一 ’其原因不外乎酵素的添加具有增加轉酯 ， 化反應的特性，即使在15%含水量環境下，該混合反應中 仍有90%的轉換率，此外某些特定酵素在水份含量越高的 環k 中’其反應越是激烈〔KaiedaM.，SamukawaT.，Kondo A.，Fukuda Η·，πEffect of methanol and water contents on production of biodiesel fuel from plant oil catalyzed by various lipases in a solvent-free system , Journal of Bioscience and Bioengineering _ V〇1· 91，P12—H 2001·〕，如此的特性很適合運用在水分 含量較高的廢油炸油提煉生質柴油製程中，但由於酵素的 價格過於昂貴’因此目前商業上大多以鹼性及酸性催化劑 為主。 酵素製程雖然有著上述的特性，但因酵素培養不易且 需在特定的環境與條件下方能保持其活性，故轉酯化反應 時’其製程步驟變的相當繁瑣，例如需將反應溫度固定在 35t：，過高或過低的環境溫度都會影響酵素活性，此外製 φ 程進行中需不斷添加醋酸鹽以維持反應環境的Ph值，視反 應率的提升，需再行添加適當的醇類含量，並維持每分鐘 • 150次的振動頻率方可進行反應〔 Ban k.，Kaieda M.， Matsumoto T·，Kondo Α·，Fukuda Η.,"Whole cell biocatalyst for biodiesel fuel production utilizing Rhizopus oryzae cells immobilized within biomass support particles , Biochemical Engineering Journal Vol· 8，p39-43, 2001·〕，種種嚴苛的條件將使得量產製程 相對複雜化，且較令人擔憂的是，隨著使用酵素與方式的 200808949 不同，其反應時間約為6· 3〜72小時不等’相較於驗性催化 - 劑的簡單、快速、轉化率高等優點，這也是目前生質柴油 量產廠未廣泛使用酵素製程的最主要原因。 超臨界曱醇製程，可在不需添加任何催化劑的條件 下，快速的進行轉酯化反應，文獻所示，一個批次循環可 . 在 3 分鐘生產約 5ml 的生質柴油 〔S.Saka/D.Kusdiana,"Biodiesel fuel from rapeseed oil as prepared in supercritical methanol”，Fuel 參 Vol· 80, p225-231，2000〕，正因為超臨界製程不需添加任 何催化劑，因此其反應需添加大量的醇類，其油脂與醇類 的混合比例為1 : 42莫耳，這樣的醇類使用量為強鹼製程 的6倍，為強酸製程的1· 41倍；除此之外，為了快速完成 轉醋化反應，反應時需在45〜65MPa與350°C以上的高壓高 溫環境下才可完成，此舉將增加該製程的危險性與大幅提 局反應成本’除此之外目前超臨界曱醇製程因受限於高壓 高溫的反應容器，故無法配合量產製造，僅能於實驗室進 • 仃微置生產與特性分析，此乃該製程未來欲大量生產時急 需克服的問.題。 綜合上述’因此亟需一種生質柴油提煉裝置，來改善 •習用技術所產生之問題。 發明内容】 驻士本的主要目的是提供—種生f柴油提煉裝置，其 ，1過可進行旋轉混切反應物並產生使反 …衣之均賀反應部，達到縮短生質柴油提煉時之 8 200808949 反應時間，減少反應時所消耗的能量，進而提高產能、降 低成本之目的。 本發明的次要目的是提供一種生質柴油提煉裝置，其 藉由一循環迴路，透過具有複數個分支管路將反應物分流 再進行匯流，使反應物藉由匯流時產生撞擊進而細化反應 物，達到縮短生質柴油提煉時之反應時間，減少反應時所 消耗的能量，進而提高產能、降低成本之目的。 為了達到上述之目的，本發明提供一種生質柴油提煉 裝置，包括：一反應槽體，提供容置至少一反應物；以及 一均質反應部，其係具有一循環空間且以一管路與該反應 槽體形成一循環迴路，該均質反應部更包括有：一轉軸， 其係設置於該循環空間内，該轉軸可藉由一驅動裝置帶動 以進行轉動；以及至少一混切體，其係設置於該轉軸上， 該混切體可隨著該轉軸之轉動以混切該至少一反應物，並 帶動該至少一反應物進行循環。 較佳的是，該反應槽體更具有一加熱器，以提供加熱 該至少一反應物。 較佳的是，該反應槽體更具有一超音波震盪器，以提 供能量振動該至少一反應物，利用其分子間的高頻碰撞， 加速其反應時間。 較佳的是，該混切體更具有：一轉子，其係設置於該 轉軸上，該轉子之一端具有一第一混切齒；以及一定子， 其係具有與該第一混切齒相交錯之一第二混切齒。 為了達到上述之目的，本發明更提供一種生質柴油提 煉裝置，包括：一反應槽體，提供容置至少一反應物；一 200808949 迴：反二二其係以一循%管路與該反應槽體形成-循環 ^路^均質反應部更包括有至少—混切體，其係具有一 弟-官路、複數個分支管路以及一混切管路，該第一管路 該至少—反應物，該複數個分支管路係與該第-管 以分散該至少-反應物，該混切管路係與該複數 刀5路相連通，以接收由該複數個分支管路所匯隼之 =反應物;以及一幫浦，其係設置於該均;反二 ，、该反應槽體之間且與該循環管路相連接。 【實施方式】 為使貴審查委員能對本發明之特徵、目的及功能有 更進-步的認知與瞭解，τ文特將本發明之系統的相關細 部結構以及設計的理念原由進行說明，以使得冑查委員可 以了解本發明之特點，詳細說明陳述如下： 、 請參閱圖一以及圖二Α所示，其中圖一係為本發明生 質柴油提煉裝置之第一較佳實施例示意圖；圖二A ^為本 發明生質柴油提煉裝置之均質反應部較佳實施例剖面示意 圖。該生質柴油提煉裝置丨，包括：一反應槽體1〇以及二 均質反應部11。該反應槽體1〇内具有容置空間可提供容 置至少一反應物。該均質反應部u，其係具有一循環空間 113且以一官路12與該反應槽體1〇形成一循環迴路9〇。 a亥管路12包括有一第一管路12〇以及一第二管路I。。該 第一官路120連接該反應槽體1〇之出口端以及該均質反廡 部11之入口端11丨。該第二管路121則連接該反應槽體】〇 之入口端以及該均質反應部11之出口端Η 2。 200808949 该反應槽體10更具有一加熱器101，以提供加熱該至 少一反應物。除了該加熱器101之外，該反應槽體10更具 有起θ波晨盪為102 ’以提供能量振動該至少一反應物， 進而辅助提供該至少—反應物產生熱量，以增加反應物之 溫度。 邊均負反應部11更包括有一轉軸Η4以及一混切體 115。该轉車由114 ’其係設置於該循環空_ 113 Θ，該轉軸 =可藉由-驅動裝置（圖中未示）帶動以進行轉動。該驅 動衣置可為馬達。該混切體115，其係設置於該轉轴⑴ 风切體115 Tlk著该轉車由114之轉動以混切該至少 一反應物，並帶動該至少一反應物進行循環。 請參關二A與圖二B所示，圖二㈣為本發明均質 2指佳實_之混切體剖片示意圖。該混城115更 子U5G以及^子1152。該轉子115G係設置於 :定子it’該：子1150之—端具有—第-混切齒115卜 定\⑽"係設置於該均質反應部之殼體110上，該 子1152具有與該第一混切齒1151相交錯之一 齒1153。請參閱圖三所示’該；質：：： 裝置之均質反雇邱s 土— ~令心明生貝&油提煉200808949 IX. Inventive description·· 【Technical field to which the invention belongs】 Will be produced: a kind of renewable energy generation device, especially two kinds of species: this: the mixing and cutting cycle to accelerate the reaction to produce biomass energy Quality diesel refining unit. [Prior Art] With ^ Γ 油 oil, you can directly add letters to the low and hexadecane values without modifying the diesel engine system, so its refining technology - i 2 source = important research direction . At present, the manufacture of biodiesel; the process of the process, the acid process, the enzyme process and the supercritical sterol rely on the supercritical A 2 ^ and the high pressure of the C above 2 = 7 = 7 need to be in 46 ^ A, Li Yi brother The next reaction, and each of the smuggling ability is 5ml, which cannot be mass-produced. The mother batch - the human production of this force (t (10) tel diesel f refining method, the use of transesterification technical agent is different, subdivided into strong test, strong acid, 5354878), f production use, only - the difference is the raw material oil used Because it does not: wide: the content of seed oil, the United States is the use of eucalyptus oil and other high-fat oil, the use of large oil to react, Japan's inland 200,808,949 • narrow people's fat cost of the South than the recycling of waste oil To carry out the transacetalization reaction. The four conversion processes are as follows: The first is the comparison between the strong test and the strong acid process. 'When the same ratio of catalyst is used for the transesterification reaction, it is found that the strong alkali process takes 1 hour to complete the reaction, but the strong acid process Depending on the amount of alcohol added, it takes 3 to 69 hours. When the molar ratio of oil to alcohol is used, the strength of the process requires 1 · 6 moles to reach 90% or more. The conversion rate, while the strong acid process requires 1: 30 moles to achieve the same conversion rate, the higher molar ratio φ will increase the amount of alcohol used, and the relative production cost will also increase significantly. [β Freedman, Ε·H. Pryde and Τ·L· Mounts, nVariables affecting the yields of fatty esters from transesterified vegetable oils', Journal Americanf American Oil Chemist's Society, Vol. 61, pp. 1638-1643 1984.] Strong Although the alkali process can shorten the reaction time to i hours, it can only be achieved by limiting the production of micro-samples at the laboratory level. If the same addition φ ratio is extended to the mass production of the factory, the mixing motor can be found in mass production. Stirring: When falling, 'usually due to the speed, laminar flow phenomenon and sputum; too many corners, but no method of mixing up and down, evenly stirring the reaction, to achieve a reaction rate of more than 90%, often, the reaction time needs to be extended by 3 to 4 hours, this will seriously affect the factory capacity. [Y· Zhang, M·A·Dube, D·D· McLean, M. Kates, "Biodiesel production from waste cooking • oil:L Process design and technological assessment", , Bioresource Technology, Vol. 89, pp. 1 -16,2003.] Esterase is used as a biocatalyst in recent years. Biodiesel 2000808949 • One of the directions in a hurry' is due to the fact that the addition of enzymes has the property of increasing transesterification and hydration, even in In the 15% water content environment, there is still a 90% conversion rate in the mixed reaction, and in addition, some specific enzymes are more intense in the ring k with higher moisture content [Kaieda M., Samukawa T., Kondo A. , Fukuda Η·, πEffect of methanol and water contents on production of biodiesel fuel from plant oil catalyzed by various lipases in a solvent-free system , Journal of Bioscience and Bioengineering _ V〇1· 91, P12-H 2001·], The characteristics are very suitable for the use of waste oil with high moisture content to refine the biodiesel process, but because the price of the enzyme is too expensive, so most of the current commercial Mainly alkaline and acidic catalyst. Although the enzyme process has the above characteristics, because the enzyme culture is not easy and needs to maintain its activity under specific circumstances and conditions, the process of the esterification reaction becomes quite complicated, for example, the reaction temperature needs to be fixed at 35t. : Excessive or too low ambient temperature will affect the activity of the enzyme. In addition, the pH of the reaction environment should be continuously added to maintain the Ph value of the reaction environment. According to the increase of the reaction rate, the appropriate alcohol content should be added. And maintain the vibration frequency of 150 times per minute to react [Ban k., Kaieda M., Matsumoto T., Kondo Α·, Fukuda Η., "Whole cell biocatalyst for biodiesel fuel production utilizing Rhizopus oryzae cells immobilized within Biomass support particles, Biochemical Engineering Journal Vol· 8, p39-43, 2001·], all kinds of harsh conditions will make the mass production process relatively complicated, and more worryingly, unlike the use of enzymes and methods of 200808949 , the reaction time is about 6.3 ~ 72 hours, compared to the simple, rapid, conversion of the catalytic catalyst Advantages, which is currently biodiesel production plants are not widely used process is the main reason for the enzyme. The supercritical sterol process allows rapid transesterification without the need to add any catalyst. As shown in the literature, one batch can be recycled. Produce about 5 ml of biodiesel in 3 minutes [S.Saka/ D.Kusdiana, "Biodiesel fuel from rapeseed oil as prepared in supercritical methanol", Fuel, Vol. 80, p225-231, 2000], because the supercritical process does not need to add any catalyst, so the reaction needs to add a large amount of alcohol The ratio of the oil to the alcohol is 1:42 moles. The amount of alcohol used is 6 times that of the strong alkali process, which is 1.41 times that of the strong acid process. In addition, in order to complete the transfer of vinegar quickly The reaction needs to be completed under high pressure and high temperature environment of 45~65MPa and above 350°C, which will increase the risk of the process and greatly increase the reaction cost. In addition, the current supercritical sterol process Due to the high pressure and high temperature of the reaction vessel, it can not be combined with mass production, and it can only be used in the laboratory for micro-production and characteristic analysis. This is an urgent question to be overcome when the process is to be mass-produced in the future. The above-mentioned 'there is a need for a biodiesel refining device to improve the problems caused by the conventional technology. SUMMARY OF THE INVENTION The main purpose of the resident is to provide a kind of raw oil refining device, which can be rotated and mixed The reaction product produces a homogenization reaction unit for shortening the reaction time of 8 200808949 when the biodiesel is refined, thereby reducing the energy consumed during the reaction, thereby increasing the productivity and reducing the cost. The secondary object of the present invention The invention provides a raw material diesel refining device which divides a reactant through a plurality of branch pipes through a circulation loop to recirculate, so that the reactants collide by the confluence to refine the reactants, thereby shortening the biomass. The reaction time of the diesel oil refining reduces the energy consumed during the reaction, thereby increasing the productivity and reducing the cost. In order to achieve the above object, the present invention provides a biodiesel refining device comprising: a reaction tank body for providing accommodation At least one reactant; and a homogeneous reaction portion having a circulation space and a conduit and the reaction vessel The body forms a circulation loop, and the homogeneous reaction portion further includes: a rotating shaft disposed in the circulation space, the rotating shaft can be driven to rotate by a driving device; and at least one mixed body disposed on the rotating body On the rotating shaft, the mixing body can rotate the rotating shaft to mix and cut the at least one reactant, and drive the at least one reactant to circulate. Preferably, the reaction tank body further has a heater to Preferably, the at least one reactant is heated. Preferably, the reaction tank body further has an ultrasonic oscillator to provide energy to vibrate the at least one reactant, and to accelerate the reaction time by using high frequency collision between the molecules. Preferably, the mixed body further has: a rotor disposed on the rotating shaft, one end of the rotor has a first mixed cutting tooth; and a stator having a cross between the first mixed cutting tooth and the first mixed cutting tooth A second mixed cutting tooth. In order to achieve the above object, the present invention further provides a biodiesel refining device, comprising: a reaction tank body for providing at least one reactant; a 200808949 back: anti-two-two system with a one-by-one pipeline and the reaction The tank forming-circulating circuit ^ homogenizing reaction portion further comprises at least a mixed body having a brother-official path, a plurality of branch lines, and a mixed cutting line, the first line of the at least one reaction And the plurality of branch lines are connected to the first tube to disperse the at least one reactant, and the mixed cutting line is in communication with the plurality of paths 5 to receive the plurality of branch lines. a reactant; and a pump disposed in the same; and a second, between the reaction tanks and connected to the circulation line. [Embodiment] In order to enable the reviewing committee to have a more advanced understanding and understanding of the features, objects and functions of the present invention, τVent describes the relevant detailed structure of the system of the present invention and the concept of the design, so that The members of the present invention can understand the characteristics of the present invention. The detailed description is as follows: Please refer to FIG. 1 and FIG. 2, wherein FIG. 1 is a schematic diagram of a first preferred embodiment of the biodiesel refining device of the present invention; A ^ is a schematic cross-sectional view of a preferred embodiment of the homogeneous reaction portion of the biodiesel refining device of the present invention. The biodiesel refining apparatus crucible comprises: a reaction tank body 1〇 and a homogenization reaction unit 11. The reaction tank body 1 has an accommodation space for providing at least one reactant. The homogeneous reaction portion u has a circulation space 113 and forms a circulation loop 9 with the reaction channel body 1 by a common path 12. The ahai line 12 includes a first line 12A and a second line I. . The first official road 120 connects the outlet end of the reaction tank body 1 and the inlet end 11 of the homogeneous reaction portion 11. The second line 121 is connected to the inlet end of the reaction tank body 以及 and the outlet end Η 2 of the homogeneous reaction portion 11. 200808949 The reaction tank 10 further has a heater 101 to provide heating of at least one reactant. In addition to the heater 101, the reaction tank body 10 further has a θ wave morning oscillation of 102 ′ to provide energy to vibrate the at least one reactant, thereby assisting in providing the at least—reactant to generate heat to increase the temperature of the reactant. . The side average negative reaction portion 11 further includes a rotating shaft 4 and a mixed body 115. The transfer is set by 114 ′ in the cycle _ 113 Θ, and the rotation axis = can be driven by a driving device (not shown) for rotation. The drive can be a motor. The mixing body 115 is disposed on the rotating shaft (1). The wind cutting body 115 Tlk rotates the turning wheel 114 to mix the at least one reactant and drives the at least one reactant to circulate. Please refer to Figure 2A and Figure 2B. Figure 2 (4) is a schematic diagram of the cross-section of the mixed body of the homogeneous 2 of the present invention. The mixed city 115 is further divided into U5G and ^1115. The rotor 115G is disposed on the stator: the end of the sub-portion 1150 has a first-mixing-cutting tooth 115, and the (10)" is disposed on the housing 110 of the homogeneous reaction portion, and the sub-1152 has the first The mixing teeth 1151 are interlaced with one of the teeth 1153. Please refer to the figure shown in Figure 3; Quality::: The homogenization of the device is anti-employed Qiu s soil - ~ Xinming Shengbei & oil refining
中僅利用^ : 貫施例剖面示意圖。在圖二A 中僅利用飞切體115，而在圖三之 個混切體116套設在轉軸114上 ]中_用了二 果。上以乓加混切反應物之效 接卜采說明本發明之生質柴油提煉 施例之操作方式。首弈楹彳 、置之弟車乂 卞F力式百先棱供如圖一之裝置1並g己人夂 —A所不。然後，量取一定 Λ 口 > 斗比卞的油脂與醇類。接 200808949 ..量取試量之驗性催化割。隨後先將鹼性催化咖溶於醇類 .之中。皆下來將油脂倒人該反應槽體1G内，開啟加執哭 101將油脂預熱至適當溫度，同時啟動超音波震蘆器 加速油脂預熱。持續使用超音波震盡，待油脂加熱至 溫度時’將催化劑/醇類混合溶液倒人該反應槽體ί〇中: ' 將溫度持續加熱至適當溫度以進行轉醋化反應。在本實施 - 例中忒油脂可為動、植物油及回收之廢油炸油。 接著啟動該均質反應部u，使該轉轴114轉動以帶動 _ 該混切體m進行轉動，此時由於該混切體115之轉動會 產生類似幫浦之效應，以產生吸力將反應物由該反應样體 ίο内抽取進到該循環空間113内，透過轉子115〇盥^子 1152上之混切齒115卜1153,交錯的運動，以擾動以及剪 切反應物，以增加反應物分子間碰撞之機會，進而達到均 質與加，反應之效果。藉由上述之生質柴油提煉裴置i產 生之循裱以混切反應物，產生轉酯化之反應，進而產生生 質柴油（脂肪酸酯類）以及副產品甘油。 鲁在轉酯化反應之後可以對反應之生成物’亦即，生質 柴油（脂肪酸酯類）以及副產品甘油進行後處理之程序。該 後處理的程序包括有下列步驟，首先添加適當莫耳比例= 酸性或者是鹼性催化劑，中和生質柴油與甘油的ph值。然 後，利用油水分離器，將不同比重之生質柴油、甘油以^ 不純的皂化物迅速分離，此舉可得到純淨的粗製生質柴 油；油水分離利用如靜置、重力、離心力...等原理之裴置，這二 裝置為習用之技術，在此不做贅述。接著，可將分離之產物再 置放在本發明之裝置之反應槽體10内，然後添加適當之有 12 200808949 機溶劑（如醚類、醇類、烷類、烯類、酮類···等化學物質）， 使用超音波震盪的方式重複將非酯類之不純物析出。最後 添加適量的水分（如蒸餾水、飽和食鹽水、二次去離子水、 純水...等），使用超音波震盪重複水洗至適當次數，將親 水性之不純物析出。最後啟動反應槽體10之加熱器101並 持續使用超音波震盪，將生質柴油加熱至適當溫度，回收 殘留之醇類、有機溶劑以及水分後，即可完成精緻之生質 柴油。 請參閱圖四所示，該圖係為本發明生質柴油提煉裝置 之第二較佳實施例示意圖。該生質柴油提煉裝置2，包括： 一反應槽體20、一均質反應部22以及一幫浦21。該反應 槽體20，提供容置至少一反應物。該反應槽體20更具有 一加熱器201，以提供加熱該至少一反應物。除了該加熱 器201之外，該反應槽體20更具有一超音波震盪器202， 以提供能量振動該至少一反應物，進而輔助提供該至少一 反應物產生熱量，以增加溫度。 該均質反應部22，其係以一循環管路23與該反應槽 體20形成一循環迴路90。如圖五所示，該均質反應部22 更包括有至少一混切體，本實施例係用兩個混切體220、 221所串連而成。混切體220、221，其係具有一第一管路. 2201、2211、複數個分支管路2202、2212以及一混切管路 2203、2213。該第一管路2201可接收該至少一反應物，該 複數個分支管路2202係與該第一管路2201相連通以分散 該至少一反應物，該混切管路2203係與該複數個分支管路 2202相連通，以接收由該複數個分支管路2202所匯集之 200808949 5亥至少—反應物。然後該混切管路2203與另一混切體221 之第一官路2211相連接以接收該混切管路2203之反應 物，然後再透過分支管路2212之分流再匯流至混切管ς 2213進而達到混切反應物之目的。Only use ^: a schematic diagram of the cross section of the application. In Fig. 2A, only the flying body 115 is used, and in Fig. 3, the mixed body 116 is sleeved on the rotating shaft 114. The effect of the puncture and mixing reaction is illustrated in the operation mode of the biodiesel refining embodiment of the present invention. The first game 楹彳 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 、 Then, measure the amount of oil and alcohol in a certain mouth > Connected to 200808949 .. to measure the amount of test catalytic cut. The alkaline catalyzed coffee is then dissolved in the alcohol. All the oil will be poured into the reaction tank 1G, open and cry, 101 preheat the grease to the appropriate temperature, and start the ultrasonic vibration device to accelerate the oil preheating. Continuous use of ultrasonic shock, when the grease is heated to temperature, 'pour the catalyst/alcohol mixture solution into the reaction tank. ': 'Continue the temperature to a suitable temperature for the transacetification reaction. In the present embodiment - the cockroach oil may be an animal or vegetable oil and a recovered waste frying oil. Then, the homogeneous reaction portion u is started, and the rotating shaft 114 is rotated to drive the mixed cutting body m to rotate. At this time, due to the rotation of the mixed cutting body 115, a pump-like effect is generated to generate suction to generate reactants. The reaction sample ίο is drawn into the circulation space 113, and passes through the mixed cutting teeth 115 1153 on the rotor 115 1115, staggered motion to disturb and shear the reactants to increase the intermolecular collision of the reactants. The opportunity to achieve homogenization and addition, the effect of the reaction. The raw material produced by the above-mentioned raw diesel refining unit i is mixed to cut the reactants to produce a transesterification reaction, thereby producing biodiesel (fatty acid esters) and by-product glycerin. After the transesterification reaction, Lu can be used to post-treat the reaction product, i.e., biodiesel (fatty acid ester) and by-product glycerin. The post-treatment procedure includes the following steps of first adding the appropriate molar ratio = acidic or basic catalyst to neutralize the pH of the biomass diesel and glycerol. Then, using the oil-water separator, the biodiesel and glycerin of different specific gravity are quickly separated by the impure saponification, which can obtain pure crude biomass diesel; the separation of oil and water such as standing, gravity, centrifugal force, etc. The principle is that the two devices are conventional technologies and will not be described here. Next, the separated product can be placed in the reaction tank body 10 of the apparatus of the present invention, and then the appropriate solvent of 12 200808949 (such as ethers, alcohols, alkanes, alkenes, ketones, etc.) can be added. (Chemical substances), the non-ester impurities are repeatedly precipitated by means of ultrasonic vibration. Finally, add an appropriate amount of water (such as distilled water, saturated brine, secondary deionized water, pure water, etc.), and repeat washing with ultrasonic waves to the appropriate number of times to precipitate the hydrophilic impurities. Finally, the heater 101 of the reaction tank body 10 is started and the ultrasonic diesel is continuously heated to heat the raw diesel oil to an appropriate temperature to recover the residual alcohol, the organic solvent and the water, thereby completing the refined biomass diesel oil. Referring to Figure 4, there is shown a schematic view of a second preferred embodiment of the biodiesel refining apparatus of the present invention. The biodiesel refining device 2 includes: a reaction tank body 20, a homogeneous reaction portion 22, and a pump 21. The reaction tank 20 provides for accommodating at least one reactant. The reaction tank body 20 further has a heater 201 to provide heating of the at least one reactant. In addition to the heater 201, the reaction vessel 20 further includes an ultrasonic oscillator 202 to provide energy to vibrate the at least one reactant to assist in providing heat to the at least one reactant to increase temperature. The homogeneous reaction portion 22 forms a circulation loop 90 with the reaction tank body 20 in a circulation line 23. As shown in FIG. 5, the homogeneous reaction portion 22 further includes at least one mixed body. In this embodiment, two mixed bodies 220 and 221 are connected in series. The mixed body 220, 221 has a first pipeline. 2201, 2211, a plurality of branch pipelines 2202, 2212, and a mixed pipeline 2203, 2213. The first conduit 2201 can receive the at least one reactant, and the plurality of branch conduits 2202 are in communication with the first conduit 2201 to disperse the at least one reactant, and the mixed conduit 2203 is associated with the plurality of reactants The branch line 2202 is in communication to receive at least 200,808,949 5 at least the reactants collected by the plurality of branch lines 2202. Then, the mixed cutting line 2203 is connected with the first official road 2211 of the other mixed body 221 to receive the reactant of the mixed cutting line 2203, and then branched and then merged to the mixed cutting tube through the branching line 2212. 2213 further achieves the purpose of mixing the reactants.
為了增加混切的效果可由複數個混切體相串連而成， 圖五中僅顯示兩個，但可依此類推。該幫浦Μ ,其係設置 5玄均貝反應部22與該反應槽體20之間且與該循環管路23 相連接/該循環管路23包括有管路23〇、管路231、管路 232。官路230連接該反應槽體20之出口端以及該幫浦21 ，入口端。管路231連接該幫浦21之出口端與該均質反應 =22之該第一管路22(Π。管路咖則連接該 :In order to increase the effect of the mixed cut, a plurality of mixed cut bodies may be connected in series, and only two are shown in FIG. 5, but the like. The pump raft is provided between the 5 Xuanbei reaction portion 22 and the reaction tank body 20 and is connected to the circulation line 23. The circulation line 23 includes a pipeline 23, a pipeline 231, and a pipe. Road 232. The official road 230 connects the outlet end of the reaction tank body 20 and the pump 21 and the inlet end. The line 231 is connected to the outlet end of the pump 21 and the first line 22 of the homogeneous reaction = 22 (Π.
Μ之混抑路2213。該幫浦21可提供反應物循環的動γ 本貫施例之運作方式基本上與圖一類似，其主要的目 Ϊ是藉^使反應物產生剪切混和的仙，㈣加均質的 當該反應物透過㈣21的動力進人到該第一管路 空1時^透過該複數個分支管路2202分流，然後再匯流 二：匕切官路2203 ’於匯流的過程中反應物液體分子間备 擊，然後產生剪切混和的效果，使反應物細化，i ^加歧應之絲。至於其他反應的雜 在此不做贅述。 之Fp f以上所者，僅為本發明之較佳實施例，當不能以 均^本發明範圍。即大凡依本發明申請專利範圍所做之 及修飾’仍料失本發明之要義所在，故都應視 ”、、务明的進一步實施狀況。 ‘合上述’本發明提供之生質柴油提煉裝置，可有效 14 200808949 縮短生質柴油提煉時之反應時間，減少反應時所消耗的能 量，進而提高產能、降低成本，並可在任何溫度、壓力下 快速反應，減少人員操作上之危險性等多項優點。足以滿 足業界之需求，進而提高該產業之競爭力，誠已符合發明 專利法所規定申請發明所需具備之要件，故爰依法呈提發 明專利之申請，謹請貴審查委員允撥時間惠予審視，並 賜準專利為禱。 【圖式簡單說明】 圖一係為本發明生質柴油提煉裝置之第一較佳實施例示意 圖。 圖二A係為本發明生質柴油提煉裝置之均質反應部較佳實 施例剖面示意圖。 圖二B係為本發明均質反應部較佳實施例之混切體剖片示 意圖。 圖三係為本發明生質柴油提煉裝置之均質反應部另一較佳 實施例剖面示意圖。 圖四係為本發明生質柴油提煉裝置之第二較佳實施例示意 圖。 圖五係為本發明生質柴油提煉裝置之均質反應部又一較佳 貫施例不意圖。 【主要元件符號說明】 1-生質柴油提煉裝置 15 200808949 ίο-反應槽體 101-加熱器 102-超音波震盪器 11- 均質反應部 110-殼體 111 -入口端 112- 出口端混 混 混 2222. The pump 21 can provide a dynamic gamma of the reactant cycle. The mode of operation of the present embodiment is basically similar to that of Figure 1. The main objective is to cause the reactant to produce shear-mixed cents, and (4) to add homogenization. When the reactants pass through the power of (4) 21 into the first pipeline, the air is diverted through the plurality of branch conduits 2202, and then merges two: the cut channel 2203' during the process of the reactants Strike, then produce the effect of shear mixing, refine the reactants, i ^ add the silk. As for the other reactions, we will not repeat them here. The above Fp f is only a preferred embodiment of the present invention, and the scope of the present invention cannot be used. That is to say, the modification and the modification of the scope of the patent application of the present invention are still in the meaning of the invention, and therefore should be regarded as further implementation status of the invention. The above-mentioned biodiesel refining device provided by the invention , can be effective 14 200808949 shorten the reaction time of biodiesel refining, reduce the energy consumed in the reaction, thereby increasing productivity, reducing costs, and can react quickly under any temperature and pressure, reducing the risk of personnel operation, etc. Advantages. Sufficient to meet the needs of the industry, and thus improve the competitiveness of the industry, Cheng has already met the requirements for applying for inventions as stipulated in the invention patent law. Therefore, the application for invention patents is required according to law. Please ask the review committee to allow time. It is a schematic diagram of the first preferred embodiment of the biodiesel refining device of the present invention. Fig. 2A is a biodiesel refining device of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 2B is a schematic view of a cross-section of a mixed body of a preferred embodiment of the homogeneous reaction unit of the present invention. 3 is a schematic cross-sectional view showing another preferred embodiment of the homogeneous reaction unit of the biodiesel refining device of the present invention. FIG. 4 is a schematic view showing a second preferred embodiment of the biodiesel refining device of the present invention. A further preferred embodiment of the homogenization reaction unit of the biodiesel refining device is not intended. [Main component symbol description] 1-Biomass diesel refining device 15 200808949 ίο-Reaction tank body 101-Heater 102-Ultrasonic oscillator 11 - homogeneous reaction section 110 - housing 111 - inlet end 112 - outlet end
113- 循環空間 114 -轉轴 115 -混切體 1150- 轉子 1151- 第一混切齒 1152- 定子 1153- 第一混切齒 Π6-混切體 12- 管路 120- 第一管路 121- 第二管路 2-生質柴油提煉裝置 20-反應槽體 201-加熱器 202-超音波震盪器 200808949 21- 幫浦 22- 均質反應部 220、221-混切體 2201、 2211-第一管路 2202、 2212-分支管路 2203、 2213-混切管路 23- 循環管路 230、231、232-管路 9 0 -循環迴路113- Circulation space 114 - Shaft 115 - Mixed body 1150 - Rotor 1151 - First mixed cutting tooth 1152 - Stator 1153 - First mixed cutting Π 6 - Mixed body 12 - Line 120 - First line 121 - Second Pipeline 2 - Biomass Diesel Refining Device 20 - Reaction Tank Body 201 - Heater 202 - Ultrasonic Oscillator 200208949 21 - Pump 22 - Homogeneous Reaction Section 220, 221 - Mixed Cylinder 2201, 2211 - First Pipeline 2202 2212-branch line 2203, 2213-mixing line 23- circulation line 230, 231, 232-line 9 0 - circulation circuit