201024402 九、發明說明： 【發明所屬之技術領域】 本發明係關於生質柴油生產系統，且#別是關於一種 連續型之生質柴油生產系統與生產方法。 【先前技#?】 生質柴油（Biodiesel)係由植物油脂及動物脂肪經過 • 轉酯化程序而形成，屬於再生能源的一種，其具有生物 可分解性和無毒性等優點，且其使用後所排放廢氣污染 較使用石化柴油的排放廢氣污染相對為低，屬為環境友 善型燃料。 近來，隨著國際原油的價格上漲、石油來源受限及 環保意識抬頭以及石油使用量的持續增加等因素，為了 避免空氣污染及全球溫室效應現象的持續擴大，生質柴 油便受到重視以作為替代燃料之用。另外，傳統生質柴 φ 油之生產方式係採大規模批次型量產方式，其需要進行 原料收集以及成品輸送，因而於收集與輸送等過程中仍 然會造成如二氧化碳之溫室氣體的排放。 請參照第1圖之示意情形，以解說習知生質柴油之 批次型生產流程。如第1圖所示，於步驟S101中，首先 將收集來如植物油脂及動物脂肪之廢油脂混入曱醇與觸 媒後以形成含油脂、曱醇與觸媒之一反應物。於步驟S103 中，接著將前述反應物置入於一批次反應器中，以於50°C 〜60°C之溫度下以及不同形式旋轉攪拌翼之機械攪拌狀 201024402 轉醋化反應約兩個小時以形成生成物，生成物 匕甘，甴與生質柴油。於步驟S105中’接著將由轉 醋化反應所制之生成物導人於—儲射並靜置約3〜4 二夺之時@以刀離生成物内甘油與生質柴油，並於步 驟SU)7中除去經靜置分離後得到之甘油並留下生質柴 油。於步驟S109中’則針對經除去甘油後而留下之生質 柴油進行水洗程序，以進—步除去其内之不純物並經再201024402 IX. Description of the invention: [Technical field to which the invention pertains] The present invention relates to a biodiesel production system, and relates to a continuous type of biodiesel production system and production method. [Previous technology #?] Biodiesel is formed by the process of transesterification of vegetable oils and animal fats. It is a kind of renewable energy, which has the advantages of biodegradability and non-toxicity. The emission of exhaust gas is relatively low compared to the pollution of exhaust gas using petrochemical diesel, and it is an environmentally friendly fuel. Recently, with the rise of international crude oil prices, limited oil sources and rising awareness of environmental protection and the continued increase in oil use, in order to avoid air pollution and the global greenhouse effect continues to expand, biodiesel is valued as an alternative. For fuel use. In addition, the production method of traditional biomass diesel oil is a large-scale batch type mass production method, which requires raw material collection and finished product transportation, so that greenhouse gas emissions such as carbon dioxide are still generated during collection and transportation. Please refer to the schematic diagram in Figure 1 to illustrate the batch production process of conventional biodiesel. As shown in Fig. 1, in step S101, waste oils such as vegetable fats and animal fats are first mixed into a sterol and a catalyst to form a reactant containing a fat, a sterol and a catalyst. In step S103, the reactants are then placed in a batch of reactors for about two hours at a temperature of 50 ° C to 60 ° C and a mechanical stirring of the different types of rotating stirring wings of 201024402. In order to form a product, the product is produced, and the raw material is diesel. In step S105, 'the product produced by the transacetation reaction is then guided to the reservoir and left to stand for about 3 to 4 times. @刀出出物内的glycerin and biodiesel, and in step SU In 7), the glycerin obtained after standing separation is removed and the biomass diesel is left. In step S109, a water washing process is performed on the biodiesel left after the glycerin is removed, to further remove the impurities therein and further
- 人靜置分離後而得到含有不純物之廢水以及較為純化之 生質柴油。隸由步驟SU1除去分離得狀廢水後，進 而得到較為純狀生質柴油。於㈣SU3中，則針對上 述較為純化之生質柴油施行—蒸餾程序，以更進一步除 去其内殘存水分，以得到最終之生質柴油成品，如步驟 S115所示。 參照上述習知生質柴油之生產流程，由於係屬於批 次型操作’於轉自旨化過程中f要加熱、溫度與攪摔等控 制裝置以控制其轉自旨化反應，此些額外之控制裝置亦提 升了生貝柴油生產成本。另外，於精練轉酯化得到之生 質柴油時需要進行水洗及蒸料麟程序，上述程序將 額外地，費大量熱能、產生了高濃度污染廢水且需要額 外設置蒸餾設備以及污水處理設備的設置，因而更不利 於生質柴油生產成本的降低。再者，上述生質柴油生產 流程極為耗時，不利於生質柴油產率的提升。 【發明内容】 有鑑於此，本發明提供了一種生質柴油之生產系統與 7 201024402 生產方法，以降低生質柴油之生產成本與提升生質柴油之 產率。 依據一實施例，本發明提供了一種生質柴油之生產系 統，包括： 一反應物供應單元，用以提供包括油脂、醇類化合物 與觸媒之一液態反應物；一傳輸單元，連結於該反應物供 應單元；一靜態攪拌單元，連結於該傳輸單元；一微波反 應單元，連結於該靜態攪拌單元；以及一生成物分離單元， 連結於該微波反應單元，其中該反應物供應單元所提供之 該液態反應物經該傳輸單元輸送流經該攪拌單元與該微波 反應單元後形成一生成物，且該生成物為該生成物分離單 元所接收並分離形成一生質柴油與一甘油。 依據另一實施例，本發明提供了一種生質柴油之生產 方法： 提供包括油脂、醇類化合物與觸媒之一液態反應物； 使該液態反應物流通一靜態攪拌單元，應用其内之一固定 式擾拌元件以攪拌並混合該液態反應物内之該油脂、醇類 化合物與觸媒；混合完成之該液態反應物應用微波催化反 應’以得到一生成物’其中該生成物包括生質柴油與甘油； 以及移除該生成物内之甘油而留下生質柴油。 為了讓本發明之上述和其他目的、特徵、和優點能更 明顯易懂，下文特舉一較佳實施例，並配合所附圖示，作 詳細說明如下： 【實施方式】 201024402 本發明之實施方式將藉由下文配合第2圖與第3圖等 附圖而加以解說。 清參照第2圖’綠示了依據本發明-實施例之生質柴 油生產系統200。 如第2圖所示之生質柴油生產系統200主要包括： ^應物供應單元210、連結於反應物供應單元210之 傳輸皁tl 220、連結於傳輸單元之靜錢拌單元2,連結 讀態授拌單元230之微波反應單元24〇、連結於微波反 f早70 之生成物切單元25〇以及相於生成物分離 早7G25G之反應物儲存單元27G。經由生成物分離單元25〇 所刀離得到之粗生質柴油，則可經由栗浦说輸送至纯化 單元260，並藉由其内之乾式純化裝置262 it行純化處理。 上述各生產單元之間可依照其輸送流體之流量斑特性而採 用適當尺寸與材質之管路而形成連結，故在料詳細描述 連結於各生產單元間所使用之管路尺寸與材質，惟通過微 波反應單元240之管路的材質需為可為微波穿透之材質， 例如為陶瓷、鐵氟隆、破璃或塑膠。 請繼續參照第2圖，反應物供應單元2ι〇内包括油脂 儲槽212以及添加物儲槽214，其中油脂儲槽212内可儲 存經使用過而回收或未經使用之植物油脂及動物脂肪，而 添加物儲槽2H則可儲存有包括醇類化合物朗媒之混 合物。反應物供應單元210係用於供應包括油脂、醇類化 合物與觸媒之液悲反應物之用，藉以生產出生質柴油。 醇類化合物例如為甲醇，而觸媒則例如為氫氧化鈉或氫 201024402 氧化鉀等鹼金屬物質。於分別連結於油脂儲槽以及添 加物儲槽214之管線上則分別設置有一閥件^丨與^ 以開啟或關閉上述油脂儲槽212以及添加物儲槽Μ内^ 儲存流體的輸出。 9 另外’傳輪單元220内則設置有如系浦功之傳輸裝 置’藉以傳輸由反應物供應單元210與反應物分離單元25〇 所供應之流體(例如為反應物、生質柴油或甘油）。- The human is allowed to stand for separation to obtain waste water containing impurities and relatively purified biomass diesel. After the separated wastewater is removed by the step SU1, the relatively pure biomass diesel is obtained. In (4) SU3, the above-mentioned relatively purified biomass diesel is subjected to a distillation process to further remove residual moisture therein to obtain a final finished diesel product, as shown in step S115. Referring to the above-mentioned conventional production process of raw diesel, since it is a batch type operation, in the process of transferring from the process of heating, temperature and stirring, etc., to control the transfer of the control, these additional control devices are also Increased production costs of raw shell diesel. In addition, the water washing and steaming process are required for the scouring of the biodiesel obtained by the esterification. The above procedure will additionally require a large amount of heat energy, generate a high concentration of polluted wastewater and require additional distillation equipment and sewage treatment equipment. Therefore, it is more detrimental to the reduction of production cost of biodiesel. Moreover, the above-mentioned biodiesel production process is extremely time consuming and is not conducive to the increase in the yield of biodiesel. SUMMARY OF THE INVENTION In view of the above, the present invention provides a production system of biodiesel and a production method of 7 201024402 to reduce the production cost of biodiesel and increase the yield of biodiesel. According to an embodiment, the present invention provides a biodiesel production system, comprising: a reactant supply unit for providing a liquid reactant including a grease, an alcohol compound and a catalyst; and a transport unit coupled to the reactant a reactant supply unit; a static agitation unit coupled to the transfer unit; a microwave reaction unit coupled to the static agitation unit; and a product separation unit coupled to the microwave reaction unit, wherein the reactant supply unit provides The liquid reactant is transported through the transfer unit and flows through the stirring unit and the microwave reaction unit to form a product, and the product is received by the product separation unit and separated to form a biomass diesel and a glycerin. According to another embodiment, the present invention provides a method for producing biodiesel: providing a liquid reactant comprising a grease, an alcohol compound and a catalyst; and passing the liquid reactant stream through a static stirring unit, applying one of the liquid reactants a fixed scramble component for agitating and mixing the grease, the alcohol compound and the catalyst in the liquid reactant; the liquid reactant is mixed and subjected to a microwave catalytic reaction to obtain a product, wherein the product includes the biomass Diesel and glycerin; and removing glycerin from the product leaving biodiesel. The above and other objects, features, and advantages of the present invention will become more apparent and understood. The manner will be explained below with reference to the drawings of Figs. 2 and 3 and the like. The green diesel fuel production system 200 according to the present invention is described with reference to Fig. 2'. The biodiesel production system 200 as shown in FIG. 2 mainly includes: an reactant supply unit 210, a transfer soap ttl 220 connected to the reactant supply unit 210, and a static money mixing unit 2 connected to the transfer unit. The microwave reaction unit 24 of the mixing unit 230, the product cutting unit 25A connected to the microwave reverse f early 70, and the reactant storage unit 27G separated from the product by 7G25G. The crude biomass diesel oil obtained by the separation of the product separation unit 25 can be transported to the purification unit 260 via Lipu, and purified by the dry purification apparatus 262 therein. The above-mentioned production units can be connected according to the flow spot characteristics of the fluid to be transported by using pipes of appropriate size and material. Therefore, the dimensions and materials of the pipes used in connection between the production units are described in detail. The material of the pipeline of the microwave reaction unit 240 needs to be a material that can be microwave-transparent, such as ceramic, Teflon, broken glass or plastic. Referring to FIG. 2 , the reactant supply unit 2 ι includes a grease reservoir 212 and an additive reservoir 214 , wherein the grease reservoir 212 can store the vegetable oil and animal fat recovered or used without being used. The additive storage tank 2H can store a mixture comprising an alcohol compound. The reactant supply unit 210 is for supplying a liquid reaction product including a fat, an alcohol compound, and a catalyst to produce a biomass diesel. The alcohol compound is, for example, methanol, and the catalyst is, for example, an alkali metal substance such as sodium hydroxide or hydrogen 201024402 potassium oxide. On the pipelines respectively connected to the grease reservoir and the additive reservoir 214, a valve member is provided to open or close the grease reservoir 212 and the output of the storage fluid in the additive reservoir. Further, the 'transmission unit 220 is provided with a transfer device such as a transfer device' to transfer the fluid (e.g., reactant, biomass diesel or glycerin) supplied from the reactant supply unit 210 and the reactant separation unit 25A.
再者’於靜態授拌單元230内則設置有―固定式㈣ ，件232，例如為-靜態授掉管_ie ，且經由傳輸 單元220之傳輸，來自於反應物供應單元21〇之定量反應 物於流經靜態攪拌單元230後便可使得其内之油脂、醇類 化合物與觸媒得到混合與均勻攪拌。於靜態攪拌單元 内更設置有-閥件V3’以控制為傳輸單a 22〇所傳輸之流 體輸送量。 而微波反應單元240内則設置有-微波反應裝置 242。熟習此技藝者可視生f柴油生產系統之生產規模 而採用適當形態之微波反應裝置。於一實施例中，當生質 柴油生產系統200之生產規模可依實際規劃處理量，經由 商業化設備所設計最適合功率規模之微波源以促進轉醋化 反應。上述經過靜態授拌單元23〇所混合與均勾擾摔之反 應物則可於通過微波反應單元時藉㈣内之微波反 應而完成轉醋化反應，進而得到包括生質柴油與甘油之 生成物。於一貫施例中’微波反應單元24〇内所施行之 微波反應係於適當功率下以及介於3〇〇MHz〜3〇〇GHz 10 201024402 之適當微波頻率下連續地反應流經此微波反應單元240之 反應物而達成，而上述微波反應係連續地施行了約5〜10 分鐘之時間。實際之微波反應之功率、頻率以及操作時間 亦可參照實際處理量以及微波反應單元之微波功率而適度 調整，而不以上述反應條件限制本發明。 另外，生成物分離單元250内則包括數個生成物分離 槽252與254，藉以接收、儲存與分離來自於微波反應單 元240之生成物，以進行生產條件調整。此些生成物分離 • 槽内設置有如傾斜板、整流板等分離構件或上述分離構件 之組合，使得所得到之生成物於生成物分離槽252與254 之一内經連續分離成其内之生質柴油與甘油等液體。如第 2圖所示，可接著移除生成物分離單元250之生成物分離 單元252與254内如甘油之副產品，並使得經分離之生質 柴油流經純化單元260而進行後續純化處理，以及使得經 分離之如甘油之副產品可被副產品儲存槽272所接收。在 此，於生成物分離槽252與254與連接管路間更分別設置 有一閥件V4與V5，藉以控制其進入副產品儲存槽272之 流通情形。純化單元260應用泵浦264將經分離之生質柴 油輸送並通過乾式純化裝置262以去除其内殘留之觸媒、 未反應完全之油脂、醇類化合物等原料以及其他不纯物等 物質，進而達到純化生質柴油之目的。在此，乾式純化裝 置262例如為包括矽酸鎂或離子交換樹脂等材質之分離管 柱。於一實施例中，於乾式純化裝置262内所使用之矽酸 鎂材質例如為Dallas Gr〇up公司所產製 201024402 之”MAGNESOLtm” ’其約佔乾式純化裝置262内材質約 30%之重量份，藉以得到經純化之生質柴油成品並提升其 内之酯含量。於另一實施例中，於乾式純化裝置262内所 使用之離子交換樹脂例如為r〇hm HAAS公司產製 之”AMBERLITE™ BD丨0DRY” ’其約佔乾式純化裝置262 内材質約10〜20 %之空間。 再者，於生成物儲存單元27〇則包括了生質柴油儲存 槽274以及副產品儲储272，上賴存槽與連接管路間 更分別設置有一閥件V7與V8，藉以控制進入生質柴油儲 存槽274以及副產品儲存槽272之流通與否。副產品儲 槽272係用以接收來自於生成物分離單元25q而分離得= 如甘油=副產品’而生質柴油儲存槽274則用以接收來 於純化早元260之經純化之生質柴油。 … 請參照第3圖之示意圖，以解說依據本發明一 之生質柴油之生產方法’其係採用如第2圖所== 統所達成。 〈主產系 如第3圖所示，於步驟S3〇1中首先將收集來之 =如醇類化合物與觸料添加物分別儲存於反應^ 應早70 210内之儲槽内。於步驟33〇3中接著藉 單 儿220傳輸由反應物供應單元21〇所提供一定比 油，、醇類化合物賴媒之液態反應物且於流經靜離二 拌早兀23G後藉由其内之固定式攪拌元件而得到^ :勾，拌。於步驟·中’經混合與均句授拌之物 接者流經微波反應單元305而連續地進行轉酯化反ς， 201024402 2進生成物。於步驟咖7中，採用生成物分離單元 而連續地分離得到生質柴油與甘油。於步驟S3〇9中 之甘油移除，經移除之甘油則可為生成物锦 Γί^内之副產品儲存槽奶所接收^步驟則Further, in the static mixing unit 230, a "fixed type (4), a member 232, for example, a static transfer tube _ie, and a quantitative reaction from the reactant supply unit 21 is transmitted through the transfer unit 220. After flowing through the static stirring unit 230, the oil, the alcohol compound and the catalyst in the mixture can be mixed and uniformly stirred. A valve member V3' is further provided in the static agitation unit to control the amount of fluid transported for transporting the single a 22 。. The microwave reaction unit 240 is provided with a microwave reaction device 242. Those skilled in the art will be able to use a microwave reaction apparatus of a suitable form in view of the production scale of the diesel production system. In one embodiment, when the production scale of the biodiesel production system 200 can be planned according to actual conditions, a microwave source most suitable for power scale is designed via commercial equipment to promote the transacetification reaction. The above-mentioned reactants mixed and uniformly smashed by the static mixing unit 23 can complete the transacetalization reaction by the microwave reaction in (4) when passing through the microwave reaction unit, thereby obtaining the product including the biomass diesel and the glycerin. . In a consistent example, the microwave reaction carried out in the microwave reaction unit 24 连续 is continuously reacted through the microwave reaction unit at an appropriate power and at a suitable microwave frequency of 3 〇〇 MHz to 3 〇〇 GHz 10 2010 24402. The reaction of 240 is achieved, and the microwave reaction is continuously carried out for about 5 to 10 minutes. The power, frequency and operating time of the actual microwave reaction can also be adjusted moderately with reference to the actual throughput and the microwave power of the microwave reaction unit, without limiting the invention to the above reaction conditions. Further, the product separation unit 250 includes a plurality of product separation grooves 252 and 254 for receiving, storing, and separating the product from the microwave reaction unit 240 to adjust the production conditions. Such a product separation/slot is provided with a separation member such as an inclined plate or a rectifying plate or a combination of the above-described separation members, so that the resultant product is continuously separated into one of the product separation grooves 252 and 254. Liquid diesel and glycerin. As shown in FIG. 2, the by-products such as glycerin in the product separation units 252 and 254 of the product separation unit 250 may be removed, and the separated biomass diesel may be passed through the purification unit 260 for subsequent purification treatment, and The separated by-product such as glycerin can be received by the by-product storage tank 272. Here, a valve member V4 and V5 are further disposed between the product separating grooves 252 and 254 and the connecting pipe, thereby controlling the flow of the product into the by-product storage tank 272. The purification unit 260 uses the pump 264 to transport the separated raw diesel oil and pass through the dry purification device 262 to remove the residual catalyst, the unreacted oil, the alcohol compound, and other impurities, and the like. To achieve the purpose of purifying biodiesel. Here, the dry purification device 262 is, for example, a separation column comprising a material such as magnesium niobate or an ion exchange resin. In one embodiment, the magnesium ruthenate material used in the dry purification device 262 is, for example, "MAGNESOLtm" manufactured by Dallas Gr〇up Co., Ltd. 201024402, which accounts for about 30% by weight of the material in the dry purification device 262. In order to obtain the purified biodiesel finished product and increase the ester content therein. In another embodiment, the ion exchange resin used in the dry purification device 262 is, for example, "AMBERLITETM BD丨0DRY" manufactured by r〇hm HAAS, which is about 10 to 20 in the dry purification device 262. % space. Furthermore, the product storage unit 27 includes a biodiesel storage tank 274 and a by-product storage 272, and a valve member V7 and V8 are respectively disposed between the upper storage tank and the connecting pipeline to control the entry into the raw diesel fuel. Whether the storage tank 274 and the by-product storage tank 272 are circulated or not. The byproduct storage tank 272 is for receiving the separated product from the product separation unit 25q = glycerol = by-products and the raw diesel storage tank 274 for receiving the purified biomass diesel for the purification of the early element 260. ... Please refer to the schematic diagram of Fig. 3 to explain the production method of the biodiesel according to the present invention, which is achieved by using the == system shown in Fig. 2. <Main Production Line As shown in Fig. 3, in the step S3〇1, the collected alcohol, such as the alcohol compound and the contact additive, are separately stored in the storage tank in the reaction 70 210. In step 33〇3, the liquid reactants provided by the reactant supply unit 21〇 are supplied by the reactant supply unit 21, and the liquid reactant of the alcohol compound is used, and after flowing through the static separation, 23G is used. The fixed stirring element inside is obtained by ^: hook and mixing. In the step, the mixture of the mixed and the uniform sample flows through the microwave reaction unit 305 to continuously carry out the transesterification reaction, and the product is introduced in 201024402. In the step coffee 7, the raw material separation unit is continuously separated to obtain biodiesel and glycerin. The glycerin removed in step S3〇9, the removed glycerin can be received by the byproduct storage tank milk in the product ^^^
Li:將初步製備之生質柴油傳輸並流通純化單元 Φ，妓1到純化目的並提升其内之醋含量。於步驟S313 =將、’查過純化之生質柴油傳輸為生成物儲存單元 =之生質柴油儲存槽274所接收，進而得到—生質柴油 成口口，如步驟S315所示。 實施例： 波反^如第2圖所示之生質柴油生產系統200，其中微 242係為一微波爐（大同公司產製’型號為 、）。於本實施例之微波爐中之後壁鑽有兩孔以 ’、&，進出，並應用直徑〇.8公分鐵福龍（Teflon)管並 • 1之：微波爐内盤繞成直徑約20公分盤管12 ®，以增加 t留時間及擾動目的。接著藉由生成物供應單元210將混 ^有油月日、甲醇以及氫氧㈣(觸媒)之液態反應物(混合比 例為100 .10:0.3)，並經由泵浦222輸送而流經靜態攪拌單 元230混合後經上述微波爐採用6〇〇w功率、2450MHz之 頻率等操作條件之微波催化，以針對上述液態反應物達到 連續式轉酯化作用。接著經由生成物分離單元25〇而分離 侍未純化之生質柴油並使之流經純化單元260而得到了經 純化之生質柴油。本實施例中之生質柴油生產系統之處理 201024402 為j〇#72公升/小時，而於生成物分離單元處得到之未 ^ 由經檢驗(採用CNS15051氣相層析法)得到 之酯含量約90%，且於苴續 m + , /、心經含有陽離子樹脂或矽酸鎂等 材料之乾式純化管之後，八 刀別得到具有95%以及94.5%之 酯含量之經純化之生質柴油 則述Λ施例所本發明之生質柴油生產系統與生 產方法具有以下優點： 1·藉由如靜攪拌f之靜態授拌單元的使用，可較習 知批次製，中所使用之桶槽搜拌葉片及權板混合之授拌方 式具有較高之油脂與曱醇混合效率。 2. 採用了微波催化之轉酯化反應，可較習知採用之電 熱反應或療氣加熱反應具有較為縮短之反應時間，可於數 分鐘内達到習知方法1_2小時反應時間之相同轉換率，因 φ 而可節省操作成本及生產設備空間 3. 採用了含離子交換樹脂或碎酸鎮等材質之淨化單 元’其具有吸附生質柴油内所殘存之鹼金屬離子以及如甘 油、甲醇及皂化物等未反應物或副產物之功效，可進一步 純化生質柴油與提升所得到之生質柴油内的酯含量，進而 提升油品品質。 4. 採用可連續式分離甘油及生質柴油設施，經由連續 式分離，提升設備處理效率及降低設備所需空間及生產成 本。 201024402 5.相較於傳統批次生產系統，本發明之生質柴油生產 系統中不需要額外設置加熱、溫度與攪拌等控制裝置以及 如蒸餾設備與污水處理設備等處理設備，因而具有簡化製 程，縮減生產系統空間，生產自動化及不產生廢水等技術 特徵。且由於本發明之生產方法及生產系統較為精簡，因 此也適用於生質柴油之移動式生產應用。 基於上述優點，本發明之生質柴油生產系統與生產方 • 法之可以應用於區域為中心之分散式能源發展型式，藉以 作為小型及高效率之生質柴油生產設施，並配合如閥件操 作與流體流量控制等適當之自動化作業情形，便能達成油 脂回收或油脂就地生產與應用，因而兼具初設成本低及自 動化生產等技術功效，且同時可達到降低油脂運送過程所 造成之二氧化碳溫室氣體排放之技術功效。 雖然本發明已以較佳實施例揭露如上，然其並非用以 限定本發明，任何熟習此技藝者，在不脫離本發明之精神 — 和範圍内，當可作各種之更動與潤飾，因此本發明之保護 範圍當視後附之申請專利範圍所界定者為準。 15 201024402 【圖式簡單說明】 第1圖為一示意圖，顯示了習知生質柴油之生產方法； 第2圖為一示意圖，繪示了依據本發明一實施例之生 質柴油之生產系統；以及 第3圖為一示意圖，顯示了依據本發明一實施例之生 質柴油之生產方法。 【主要元件符號說明】 200〜生質柴油生產系統； 210〜反應物供應單元； 212〜油脂儲槽； 214〜添加物儲槽； 220〜傳輸單元； 222〜泵浦； 230〜靜態攪拌單元； 232〜固定式攪拌元件； 240〜微波反應單元； 242〜微波反應裝置； 250〜生成物分離單元； 252、254〜生成物分離槽； 260〜純化單元； 262〜乾式純化管； 264〜泵浦； 270〜生成物儲存單元； 16 201024402 272〜副產物儲存槽； 274〜生質柴油儲存槽； VI、V2、V3、V4、V5、V7、V8 〜閥件Li: The preliminary prepared biodiesel is transported and passed through the purification unit Φ, 妓1 to the purpose of purification and the vinegar content therein is increased. In step S313, the biodiesel storage tank 274, which has been inspected and transferred to the product storage unit, is received, and the raw diesel fuel port is obtained, as shown in step S315. EXAMPLES: The reverse generation of the biodiesel production system 200 shown in Fig. 2, wherein the micro 242 is a microwave oven (manufactured by Datong Co., Ltd.). In the microwave oven of this embodiment, the wall drill has two holes for ', &, in and out, and a diameter of 8.8 cm Teflon tube is used and • 1 is: the microwave is coiled into a coil of about 20 cm in diameter. 12 ® to increase t retention time and disturbance purpose. Then, the liquid reactant (mixing ratio of 100.10:0.3) of the oily day, methanol, and hydrogen (4) (catalyst) is mixed by the product supply unit 210, and is transported through the pump 222 to pass through the static state. The mixing unit 230 is mixed and subjected to microwave catalysis using operating conditions of 6 〇〇w power and 2450 MHz frequency in the above microwave oven to achieve continuous transesterification for the liquid reactant. The unpurified raw diesel oil is then separated and passed through a purification unit 260 via a product separation unit 25 to obtain purified biomass diesel. The treatment of the biodiesel production system in the present embodiment 201024402 is j〇#72 liter/hour, and the ester obtained at the product separation unit is not tested by the CNS15051 gas chromatography. After 90%, and after the dry purification tube containing the cationic resin or magnesium citrate, the purified bio-diesel with 95% and 94.5% ester content is obtained. The biodiesel production system and the production method of the present invention have the following advantages: 1. By using the static mixing unit such as static stirring f, the batch system can be used in comparison with the conventional batch system. The blending method of the blade and the weight plate has a high mixing efficiency of the oil and the sterol. 2. The microwave-catalyzed transesterification reaction can shorten the reaction time compared with the conventional electrothermal reaction or the therapeutic gas heating reaction, and can reach the same conversion rate of the conventional method 1 to 2 hours reaction time in a few minutes. Saving operation cost and production equipment space due to φ 3. Purification unit containing ion exchange resin or crushed acid town, which has alkali metal ions remaining in adsorbed raw diesel oil such as glycerin, methanol and saponified product The effect of the unreacted materials or by-products can further purify the biodiesel and enhance the ester content in the raw diesel oil, thereby improving the quality of the oil. 4. Continuous separation of glycerin and biodiesel facilities for continuous separation, improved equipment processing efficiency and reduced equipment space and production costs. 201024402 5. Compared with the conventional batch production system, the biodiesel production system of the present invention does not require additional control devices such as heating, temperature and agitation, and processing equipment such as distillation equipment and sewage treatment equipment, thereby simplifying the process. Reduce the technical characteristics of production system space, production automation and no waste water. Moreover, since the production method and production system of the present invention are relatively simple, it is also suitable for mobile production applications of biodiesel. Based on the above advantages, the biodiesel production system and the production method of the present invention can be applied to a regionally-centered decentralized energy development model, thereby serving as a small and high-efficiency biomass diesel production facility, and operating as a valve member. With proper automation in fluid flow control, oil recovery or grease production and application can be achieved, resulting in low initial cost and automated production, while reducing carbon dioxide emissions from the grease delivery process. Technical efficacy of greenhouse gas emissions. While the present invention has been described above in terms of the preferred embodiments thereof, it is not intended to limit the invention, and the present invention may be modified and modified without departing from the spirit and scope of the invention. The scope of the invention is defined by the scope of the appended claims. 15 201024402 [Simple description of the drawings] Fig. 1 is a schematic view showing a production method of a conventional biodiesel; Fig. 2 is a schematic view showing a production system of a biodiesel according to an embodiment of the present invention; Fig. 3 is a schematic view showing a method of producing biodiesel according to an embodiment of the present invention. [Main component symbol description] 200~ biodiesel production system; 210~reactant supply unit; 212~ grease storage tank; 214~ additive storage tank; 220~transport unit; 222~pump; 230~ static stirring unit; 232~fixed stirring element; 240~microwave reaction unit; 242~microwave reaction unit; 250~product separation unit; 252, 254~product separation tank; 260~purification unit; 262~dry purification tube; 264~pump 270~product storage unit; 16 201024402 272~ byproduct storage tank; 274~ biodiesel storage tank; VI, V2, V3, V4, V5, V7, V8 ~ valve parts
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