201122092 六、發明說明： 【發明所屬之技術領域】 本發明係有關於一種連續萃取裝置，且㈣關於__種 藻類萃取裝置及其方法。 【先前技術】 由於全球石油資源短缺’價格居高不下，加上「京都 議定書」對溫室氣體排放的全球性管制，因此積極尋找替 代能源，是刻不容缓的課題。生質燃料已經證明具有能源 及環保之雙重效益。藻類物質與其他能作為生質燃料的農 作物，例如棕櫚、甘蔗、玉米、黃豆等相比，擁有更令人 矚目的優勢。舉例來說，根據國際創價學會（Synthetic Genomics Inc.; SGI)與 EMRE (Exxon Mobile Research Engineering)的資料，以種植每一英故能產生的燃料年產量 來比較，棕櫊、甘蔗、玉米與黃豆的燃料產量分別為650、 450、250與50加侖，而藻類卻高達2,000加侖，遠超過上 述四種農作物的總和產量。因此，油脂利用性高的微藻生 物著實為相當具有潛力的一種替代能源。 由於微藻生物的油脂係被包覆在藻體細胞壁當中，因 此若要使油脂的使用效率大幅提升，就必須破裂藻體細胞 壁。此外，由於微藻生物係在水環境中生長，因此當從水 環境中取出時，其會含有大量的水分’而富含水分的微藻 的細胞壁較難被破壞，因此油脂的取用較困難。由上述内 容可知，要提高從微藻生物中取得油脂的效率，關鍵在於 降低微藻含水量，並提高微藻細胞壁的破裂程度。 201122092 目前最廣泛使用的破壁方法是高壓均質（Homogenizer) 和珠磨（Ball mill)破裂法，然而其作用過程中產生的大量熱 能’會提高待萃物的溫度（70。(：以上），而使微藻生物中同 樣極具商業價值如色素或具生物活性等物質亦遭受破裂。 此外’能同時去除水分並破裂藻體細胞壁的乾燥法，其激 烈的高溫手段也容易使色素或具生物活性等物質產生變 質。其他例如滲透壓衝擊法或凍結-融解法的非機械式方 法，則有無法應用在大規模或破裂效率低的問題。再者， 上述方法大多是批次萃取，產率低且能耗高。 【發明内容】 .本發明提供一種連續式微藻萃取裝置，包括：一脫水 ^裝置’其係用以將被導人的濕藻泥物料脫水且破壁， 2該脫水破裂裝置包括—第—擠出機及喷嘴；—第-八 -^體1二分離槽；以及—流體供應器，其係用以提二 濕物供—種連續萃取的方法，包括：將-第-脫水破裂裝置中進行脫水 脫水破裂裝置包括一第一擠出機及喷嘴。 其中該 本發明還提供一種脫水 出機，包括一嘖喈^备 包括.k供一擠 機的第二端位1位在該擠出機的第-端，其中該擠出 ;5亥第一端的相反侧；將—流胃 入該擠出機，苴士 训·锻興濕物料導 -端的方Μ、、、中’該濕物料在該擠出機中由第二端往兹 ，。送的過程中，受擠壓或剪切力而被破裂，且 201122092 壓力逐漸增加以提升該喷嘴内、外側之間的壓力差，而該 流體則在該擠出機中，由第一端往第二端的方向傳送而與 該濕物料逆向而流，藉此提高與該濕物料的接觸效率，而 達到脫水目的；以及使用該喷嘴，將該流體與脫水且破裂 的物料從該擠出機喷出，藉此進一步地破裂該物料。 本發明更提供一種脫水破裂的方法，包括：提供一高 壓儲槽、喷嘴、擠出機與分離槽，其中該喷嘴位於該高壓 儲槽的底部；將一流體與濕物料導入該高壓儲槽；使用該 • 喷嘴，將該高壓儲槽中的該流體與濕物料喷出，藉此破裂 該物料；將從該喷嘴喷出的該流體與破裂的物料導入該擠 出機，並使用該擠出機更進一步地破裂該破裂的濕物料； 以及從該擠出機將該流體與破裂的濕物料導入該分離槽， 並使用該分離槽將該流體與濕物料分離成油脂與該流體以 及水分與殘潰。 【實施方式】 ® 第1圖顯示根據本發明概念的連續式微藻萃取裝置。 第2圖為一實施例之擠出機的内部構造示意圖。須注意圖 中所示者為本發明所選用之實施例結構，此僅供說明之 用’在專利申請上並不受此種結構之限制。 請參考第1圖，連續式萃取裝置包括擠出機10、喷嘴 11、擠出機30、分離槽20、分離槽22、萃取槽40與流體 供應器4卜擠出機10、喷嘴11與分離槽20可建構成脫水 破裂裝置，之後會詳細說明。擠出機10的第二部分(左部 201122092 分）具有入料口 25。喷嘴11位於擠出機10的第一端（右端）。 雖然第1圖所示的擠出機10為水平式擠出機，其中入料口 25是位於擠出機10的左部分（第二部分），且喷嘴11是位 於擠出機10右端（第一端），然而其也可為垂直式擠出機（未 顯示），此時喷嘴會位於擠出機的底部，入料口則位於喷嘴 的上方，因此換言之，在此所述的擠出機的“第一’’、“第二’’ 端（方、部分）同時也可分別表示擠出機的“右”、“左”端（方、 部分）或“下”、“上”端（方、部分），且為求簡潔，以下不再 贅述此概念。擠出機30具有入料口 26。 請參考第1圖，管線3與分離槽22連接，並與通往入 料口 25的管線13連接。管線1也與管線13連接。管線4 的兩端分別連接在擠出機10不同的橫向位置。管線8連接 萃取槽40與擠出機10。管線9連接喷嘴11與分離槽20。 管線15連接擠出機10與分離槽22。管線2連接流體供應 器41、分離槽20與萃取槽40。管線42與萃取槽40連接， 並通往裝置的外部。通往裝置外部的管線33與擠出機30 連接。管線31通往擠出機30的入料口 26。管線5與分離 槽20連接，並通往入料口 26。管線21與分離槽20連接， 並通往裝置的外部。管線6連接分離槽22與管線21。管 線7連接擠出機30與萃取槽40。 以下以第1圖與第2圖說明本發明一實施例的方法。 首先，從裝置的外部，藉由管線1與13，將富含水分的濕 藻泥物料傳輸至入料口 25而進入擠出機10的第二部分 中。同時，來自流體供應器41的流體，例如利用溫度控制 在-56.6°C至31.1°C的範圍内，且壓力控制在大於5_18 201122092201122092 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a continuous extraction apparatus, and (4) to an apparatus for extracting algae and a method therefor. [Prior Art] Due to the high global oil resource shortage, and the “Kyoto Protocol” global regulation of greenhouse gas emissions, it is an urgent task to actively seek alternative energy sources. Biomass fuel has proven to be a dual benefit of energy and environmental protection. Algae has a more compelling advantage than other crops that can be used as biofuels, such as palm, sugar cane, corn, and soy. For example, according to the data of Synthetic Genomics Inc. (SGI) and EMRE (Exxon Mobile Research Engineering), comparing the annual production of fuel produced by each age, palm stalks, sugar cane, corn and Soybean fuel production is 650, 450, 250 and 50 gallons, respectively, while algae is as high as 2,000 gallons, far exceeding the combined yield of the four crops mentioned above. Therefore, microalgae organisms with high oil availability are indeed an alternative energy source with considerable potential. Since the oil of the microalgae organism is coated in the cell wall of the algae, it is necessary to break the cell wall of the algae in order to greatly increase the efficiency of the use of the oil. In addition, since the microalgae organism grows in an aquatic environment, it will contain a large amount of water when taken out from the water environment, and the cell wall of the water-rich microalgae is hard to be destroyed, so that it is difficult to obtain the oil. . From the above, it is known that to increase the efficiency of obtaining fats and oils from microalgae organisms, the key is to reduce the water content of the microalgae and to increase the degree of rupture of the microalgae cell wall. 201122092 The most widely used method of breaking the wall is the high pressure homogenizer (Homogenizer) and the bead mill (Ball mill) rupture method. However, the large amount of thermal energy generated during the action will increase the temperature of the extract (70. (:)). The microalgae organisms are also commercially viable, such as pigments or biologically active substances. In addition, the drying method, which can simultaneously remove water and break the cell wall of algae, is also prone to pigments or organisms. Substances such as activity are deteriorated. Other non-mechanical methods such as osmotic pressure or freeze-thaw method cannot be applied to large-scale or low-efficiency problems. Moreover, most of the above methods are batch extraction, yield. The invention provides a continuous microalgae extraction device, comprising: a dehydration device for dehydrating and breaking a guided wet algae material, 2 the dehydration rupture The device comprises: a first extruder and a nozzle; a first-eight-body 1 two separation tank; and a fluid supply device for extracting two wet materials for continuous extraction The method comprises: dehydrating and dehydrating the rupture device in the first-dehydration rupture device, comprising a first extruder and a nozzle. The invention also provides a dewatering machine, comprising a 包括The second end of the machine is at the first end of the extruder, wherein the extrusion; the opposite side of the first end of the 5 hai; the flow-flow into the extruder, the gentleman training, the forging wet material The guide-end of the square, the middle, the 'wet material in the extruder from the second end toward the line. During the process of being sent, it is broken by the extrusion or shearing force, and the pressure of 201122092 is gradually increased to enhance a pressure difference between the inside and the outside of the nozzle, and the fluid is conveyed in the extruder from the first end to the second end to flow backward with the wet material, thereby increasing contact with the wet material Efficiency, to achieve the purpose of dewatering; and using the nozzle, the fluid and the dehydrated and ruptured material are ejected from the extruder, thereby further breaking the material. The present invention further provides a method for dehydration cracking, comprising: providing a high pressure storage tank, nozzle, extruder and separation tank, The nozzle is located at the bottom of the high pressure storage tank; a fluid and wet material is introduced into the high pressure storage tank; the nozzle is used to spray the fluid and the wet material in the high pressure storage tank, thereby breaking the material; The fluid ejected from the nozzle and the ruptured material are introduced into the extruder, and the ruptured wet material is further broken using the extruder; and the fluid and the ruptured wet material are introduced into the extruder from the extruder The separation tank is used to separate the fluid from the wet material into grease and the fluid and moisture and residue. [Embodiment] ® Fig. 1 shows a continuous microalgae extraction device according to the concept of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS The internal configuration of an extruder of an embodiment is to be taken as an illustration of the structure of the embodiment selected for the present invention, which is for illustrative purposes only and is not limited by such structure. Referring to FIG. 1, the continuous extraction apparatus includes an extruder 10, a nozzle 11, an extruder 30, a separation tank 20, a separation tank 22, an extraction tank 40, a fluid supply device 4, an extruder 10, and a nozzle 11 and separation. The tank 20 can be constructed as a dewatering rupture device, which will be described in detail later. The second portion of the extruder 10 (left part 201122092 points) has a feed port 25. The nozzle 11 is located at the first end (right end) of the extruder 10. Although the extruder 10 shown in Fig. 1 is a horizontal extruder in which the inlet port 25 is located at the left portion (second portion) of the extruder 10, and the nozzle 11 is located at the right end of the extruder 10 (the One end), however it can also be a vertical extruder (not shown), where the nozzle will be located at the bottom of the extruder and the feed port will be above the nozzle, so in other words, the extruder described herein The "first" and "second" ends (squares, parts) can also represent the "right", "left" end (square, partial) or "lower" and "upper" ends of the extruder, respectively. Fang, part), and for the sake of simplicity, the concept will not be repeated below. The extruder 30 has a feed port 26. Referring to Fig. 1, line 3 is connected to separation tank 22 and to line 13 leading to inlet port 25. Line 1 is also connected to line 13. Both ends of the line 4 are connected to different lateral positions of the extruder 10, respectively. Line 8 connects extraction tank 40 to extruder 10. The line 9 connects the nozzle 11 and the separation tank 20. Line 15 connects extruder 10 to separation tank 22. The line 2 connects the fluid supply 41, the separation tank 20 and the extraction tank 40. Line 42 is connected to extraction tank 40 and to the exterior of the unit. A line 33 leading to the outside of the apparatus is connected to the extruder 30. Line 31 leads to the feed port 26 of the extruder 30. The line 5 is connected to the separation tank 20 and leads to the feed port 26. Line 21 is connected to separation tank 20 and to the exterior of the unit. Line 6 connects separation tank 22 to line 21. The line 7 is connected to the extruder 30 and the extraction tank 40. Hereinafter, a method of an embodiment of the present invention will be described with reference to Figs. 1 and 2. First, moisture-rich wet algal mud material is transferred from the outside of the apparatus to the feed port 25 through lines 1 and 13 into the second portion of the extruder 10. At the same time, the fluid from the fluid supply 41 is controlled, for example, by a temperature in the range of -56.6 ° C to 31.1 ° C, and the pressure is controlled to be greater than 5_18 201122092.
Bar(> 5.18 Bar)的液態二氧化碳壓縮流體，則通過管線管線 2與8而傳至擠出機10的第一部分中。於其他實施例中， 二氧化碳流體也可為超臨界流體，此時的操作溫度則控制 在高於31.1°C(>31.rc)，且壓力控制在大於73 Bar(>73 Bar)。於實施例中，流體供應器41也具有壓縮冷凝流體的 作用。在擠出機10中，濕藻泥物料會隨著擠出機中轉 動的元件由第二端往第一端的方向移動，二氧化碳流體則 由第二端往第一端的方向移動。此外，流動至擠出機10第 • 二部分的二氧化碳流體可藉由管線4回流到第一部分中而 再次地被使用，因此能提高二氧化碳流體的利用率。 於一實施例中，擠出機10為單元式交錯型同向雙螺桿 機，且内部構造可如第2圖所示，包括JE向螺紋段45、47 與反向螺紋段46。濕藻泥物料係在導程間距較大的正向螺 紋段45，流順地進入雙螺桿擠出機1〇的第二部分中，然 後隨著同向共軛旋轉的螺紋逐步地向第，端的方向輸送， 而傳送至導程間距較小的正向螺紋段47及反向螺紋段 • 46，此時’濕藻泥物料與正向螺紋段47、反向螺紋段46 會在雙螺桿擠出機10中產生建壓作用，造成壓力會往第— 端的方向逐漸增大，使得在臨接噴嘴11的第一部分具有最 大壓力值，而藉此提高噴嘴11内、外側之間的壓力差。上 述喷嘴11内、外側之間的壓力差係大於1 Bar，較佳介於 1 Bar 至 1，000 Bar 之間（1 Barg ΔΡ$ 1,〇〇〇 Bar)。 在擠出機10中，由於逆向而流的二氧化碳流體與濕藻 泥物料能夠充分地混合接觸’因此二氧化碳流體能夠有效 率地帶走濕藻泥物料中的水分’而其中愈接近喷嘴1 1處的 201122092 濕藻泥物料具有愈高的脫水程度。含水量愈少的藻泥愈容 易受到外力的影響而被破裂。再者，藻泥在擠出機10中混 合的過程中，少部分藻泥的藻體細胞壁已受到螺紋元件的 擠壓或剪切力而被破裂。此外，藻泥在藉由喷嘴11膨脹喷 出時，大部分藻體細胞壁會更進一步地被破裂。換句話說， 在經過擠出機10、喷嘴11與流向相反的二氧化碳流體的 作用之下，藻泥内的藻體細胞壁結構會大幅度地被破裂， 因而能釋出藻體内大量的油脂，因此在接下來的流程中， 能夠充分地利用藻泥内含有的油脂。要注意的是，本發明 使用液態二氧化碳的壓縮流體的好處在於，不需要使用高 溫’二氧化碳流體就能夠有效率地擴散及滲透至濕藻泥物 料之中，而達到優異的脫水效果，同時能避免高溫環境破 裂掉微藻生物具有商業價值的結構。 另外，須注意的是，在能夠提高喷嘴11内、外側之間 的壓力差的前提之下’本發明擠出機10的構造並不限定於 第2圖所示的結構’而可視情況使用其他未顯示在圖中的 單元部件，例如·動力密封段(dynamic seal)(設置在擠出機10 第一端，以避免流體直接在喷嘴11處逸出）、捏合塊 (kneading block)及齒形塊(tooth block)(用來增強破裂藻體 細胞壁之剪切力）’並可使用其他任意的排列組合。另外， 本發明僅以第2圖所示的結構簡單地說明概念，為求簡 泳，其他有關於擠出過程的參數及部件，例如擾伴凸輪、 控溫迴路、抽真空迴路、蒸氣鎖或中空螺桿及改變流體黏 度之複合添加劑（compounding)加料口之設計則省略而未 詳述。 201122092 部分藻泥與水分會藉由管線15，從擠出機10流入分 離槽22中並進行分離，接著，部分藻泥會流至管線3中， 並藉由管線13回流至第一擠出機10中，而水分會流至管 線6中。 二氧化碳流體、脫水且破壁的大部分藻體與油脂會藉 由管線9，從喷嘴11處流入分離槽20中並進行分離，接 著，二氧化碳流體會流至管線2中，大部分的油脂與更進 一步去除水分的脫水且破壁的藻體會流至管線5中，而水 • 分與另一部分的油脂則會流至管線21中。 管線5中的脫水且破壁的大部分藻體與油脂會流至擠 出機30的入料口 26而進入擠出機30中。醇類物質可藉由 管線31傳入擠出機30中。於一實施例中，擠出機30為雙 螺桿擠出機。擠出機30的構造可類似、但不限定於第1圖 所示的擠出機10的構造，且也同樣地可視情況使用其他未 顯示在圖中的單元部件，例如動力密封段、捏合塊(kneading block)及齒形塊(tooth block)，並可使用其他任意的排列組 • 合，另外，為求簡潔，其他有關於擠出過程的參數及部件， 例如攪伴凸輪、控溫迴路、抽真空迴路、蒸氣鎖或中空螺 桿及改變流體黏度之複合添加劑（compounding)加料口之 設計則省略而未詳述。 透過雙螺桿擠出機30的混合作用，油脂能有效率地與 醇類物質進行酯化反應而變成酯類物質。上述醇類物質包 括碳數低於5的醇類物質，例如曱醇、乙醇或其他具有高 極性的醇類溶劑。舉例來說，當油脂是與曱醇進行酯化反 應時，會得到曱基酯。於一實施例中，除了醇類物質之外， 201122092 觸媒也能同時藉由管線31傳入擠出機30中，藉此更進一 步地提升酯化反應的效率。上述觸媒較佳為固體粉末，包 括氫氧化鈉、氫氧化鉀或氧化鎂，但不限於此，其也可以 係具有其他型態的物質，例如曱醇鈉。酯類物質與藻渣會 藉由管線7，從擠出機30流入萃取槽40中。未反應的曱 醇或經反應後曱醇則可藉由管線33從裝置排除回收或再 使用掉，觸媒則可由萃取槽40回收使用。 管線7中的藻渣與酯類物質，與管線2中的二氧化碳 流體，在流入萃取槽40中作用之後，藻渣會流入收集管線 籲 42中，二氧化碳流體與酯類物質則會流入管線8中。萃取 槽40可包括槽式或高壓爸式反應器。萃取槽40可具有壓 力表、安全洩壓膜片（rupture disc)、安全汽壓閥（relief valve) 等裝置（未顯示）。本發明也發現，相對於典型的先對油脂 進行萃取然後再進行酯化反應的方法，本發明先將油脂進 行酯化反應，然後再對得到的酯類物質（利用萃取槽）進行 萃取的方法，能夠得到更佳的萃取效果。 要注意的是，流入管線8中的二氧化碳流體與酯類物 · 質會進入擠出機10中，而再次地依循上述途徑，與從入料 口 25流入擠出機10中的濕藻泥物料相互混合。之後，在 管線9中流往分離槽20的物質除了二氧化碳流體、脫水且 破壁的藻體與油脂之外，更包括酯類物質，且在分離槽20 分離之後，二氧化碳流體會流至管線2中，部分的油脂與 脫水且破壁的藻體會流至管線5中，而酯類物質、水分與 另一部分的油脂則會流至管線21中。裝置其他部分的運作 則大致上與先前的說明相同，因此在此不再贅述以求簡潔。 10 201122092 裝置須的另-個連續式微藻萃取 喷嘴78、擠出機54、卒取裝置了匕括4儲槽2、 60。噴嘴刀離槽56、分離槽％與流體供應器 ，壓儲槽52的底部。高壓_、噴嘴 會詳細說明。管線^離槽可建構成脫水破裂裝置，之後 嘴78與擠出機& ;4二：=槽52連接。管線64連接噴 管_分離槽56連1菩 機54與分離槽56。 槽mm分=5°Λ線7G連接分離槽56與分離 與流體供應H 60。f/76、= ° #線74連接分離槽％ 52。 綠76連接流體供應器60與高壓儲槽 的方沐。、本&明根據第3圖所示裝置進行連續式萃取 將_含水分的濕藻泥物料與流體同向地傳 至尚壓儲槽52。卜诂占人& \ 私_ ^ 3水为的濕藻泥物料與流體可藉由 高壓儲槽52中。或者，富含水分的濕 蕤由法鞅i 9由官線62傳送至高壓儲槽52中，而流體則 二机體供應器60提供至高壓儲槽52中。於實施例中， 體供應60也具有壓縮冷凝流體的作用。上述流體可為 溫度控制在_56.6t：至31儿的範_，且壓力控制在大於 5.18 Bar(>5.18 Bar)的液態二氧化碳壓縮流體，或者，也 可為溫度則控制在高於31.代（>31⑻，且壓力控制在大 ，73 Bar(>73 Bar)的超臨界二氧化碳流體。持續流入的二 氧化碳流體會在高壓儲槽52中建立壓力，藉此提高喷嘴 201122092 78内、外側之間的壓力差，使得當高壓儲槽52中的二氧 化碳流體與濕藻泥物料藉由喷嘴78膨脹喷出時’藻泥的藻 體細胞壁會被破裂。上述噴嘴78内、外側之間的壓力差係 大於1 Bar，較佳介於1 Bar至1，〇〇〇 Bar之間u Bar S ΔΡ S 1，000 Bar)。 然後，從喷嘴78喷出的二氧化碳流體與破壁濕藻泥物 料可藉由管線64傳至擠出機54。於一實施例中，擠出機 54為單元式交錯型同向雙螺桿機。擠出機54的構造可類 似、但不限定於第1圖所示的擠出機的構造’且也同樣 地可視情況使用其他未顯示在圖中的單元部件，例如動力 密封段、捏合塊(kneading block)及齒形塊(tooth block)，並 可使用其他任意的排列組合，另外，為求簡潔，其他有關 於擠出過程的參數及部件，例如攪伴凸輪、控溫迴路、抽 真空迴路、蒸氣鎖或中空螺桿及改變流體黏度之複合添加 劑（compounding)加料口之設計則省略而未詳述。 在擠出機54中，轉動的螺紋元件可幫助二氧化碟流體 與破壁濕藻泥物料的混合。此外’藻泥在在擠出機54中混 合的過程中，藻泥的藻壁會受到螺紋元件的擠壓或剪切力 而被進一步地破裂。根據上述，濕藻泥物料在高壓儲槽52、 喷嘴78與擠出機54的作用之下’藻泥内的藻體細胞壁結 構會大幅度地被破裂，而釋出大量的油脂。因此，二氧化 碳流體在擠出機54的攪拌混合過程中，能夠充分地萃取油 脂。 接著，藉由管路66從擠出機54將二氧化碳流體與破 壁濕藻泥物料導入分離槽56，然後經由分離槽56分離出 201122092The liquid carbon dioxide compressed fluid of Bar (> 5.18 Bar) is passed through line lines 2 and 8 to the first portion of extruder 10. In other embodiments, the carbon dioxide fluid may also be a supercritical fluid, at which time the operating temperature is controlled above 31.1 ° C (> 31. rc) and the pressure is controlled to be greater than 73 Bar (> 73 Bar). In the embodiment, the fluid supply 41 also has the function of compressing the condensed fluid. In the extruder 10, the wet algae material moves as the element rotating in the extruder moves from the second end toward the first end, and the carbon dioxide fluid moves from the second end toward the first end. In addition, the carbon dioxide fluid flowing to the second part of the extruder 10 can be reused by returning the line 4 to the first portion, thereby increasing the utilization of the carbon dioxide fluid. In one embodiment, the extruder 10 is a unitary staggered co-rotating twin screw machine and the internal configuration can be as shown in Fig. 2, including the JE threaded sections 45, 47 and the reverse threaded section 46. The wet algae mud material is in the forward thread section 45 with a large lead spacing, smoothly enters the second part of the twin-screw extruder 1〇, and then gradually moves toward the first step with the thread of the same conjugate rotation. The direction of the end is conveyed to the forward thread section 47 and the reverse thread section 46 with a small lead pitch. At this time, the 'wet algae material and the forward thread section 47 and the reverse thread section 46 are squeezed in the twin screw. The build-up action is generated in the outlet 10, causing the pressure to gradually increase toward the first end, so that the first portion of the adjoining nozzle 11 has a maximum pressure value, thereby increasing the pressure difference between the inside and the outside of the nozzle 11. The pressure difference between the inside and the outside of the nozzle 11 is greater than 1 Bar, preferably between 1 Bar and 1,000 Bar (1 Barg ΔΡ$ 1, 〇〇〇 Bar). In the extruder 10, the carbon dioxide fluid flowing in the reverse direction and the wet algae material can be sufficiently mixed to contact 'so the carbon dioxide fluid can efficiently remove the moisture in the wet algae material', and the closer to the nozzle 1 1 201122092 The wet algae mud material has a higher degree of dehydration. The less the algae mud with less water content, the more susceptible it is to being broken by the influence of external forces. Further, during the mixing of the algal mud in the extruder 10, a small portion of the algal body cell wall of the algal mud has been broken by the pressing or shearing force of the threaded member. Further, when the algal mud is ejected by the nozzle 11, most of the algal body cell walls are further broken. In other words, under the action of the extruder 10, the nozzle 11 and the oppositely flowing carbon dioxide fluid, the cell wall structure of the algae in the algae mud is greatly broken, thereby releasing a large amount of oil in the algae body. Therefore, in the following flow, the oil and fat contained in the algae can be fully utilized. It should be noted that the advantage of the compressed fluid using liquid carbon dioxide of the present invention is that it can efficiently diffuse and penetrate into the wet algae mud material without using a high temperature 'carbon dioxide fluid, thereby achieving excellent dehydration effect while avoiding The high temperature environment ruptures the structure of microalgae organisms with commercial value. In addition, it is to be noted that the structure of the extruder 10 of the present invention is not limited to the structure shown in FIG. 2, and the other configuration may be used as appropriate, provided that the pressure difference between the inside and the outside of the nozzle 11 can be increased. Unit components not shown in the figure, such as a dynamic seal (provided at the first end of the extruder 10 to prevent fluid from escaping directly at the nozzle 11), kneading block and tooth profile A block of teeth (used to enhance the shear of the cell wall of the ruptured algae) can be used in any other permutation combination. In addition, the present invention simply illustrates the concept with the structure shown in FIG. 2, and for the sake of simple stroke, other parameters and components related to the extrusion process, such as a disturbance cam, a temperature control loop, a vacuum circuit, a vapor lock, or The design of the hollow screw and the compounding feed port for changing the viscosity of the fluid is omitted and not described in detail. 201122092 Part of the algae and moisture will flow from the extruder 10 into the separation tank 22 by means of the line 15, and will be separated. Then, part of the algae will flow into the line 3 and return to the first extruder by the line 13. 10, and moisture will flow into line 6. Most of the carbon dioxide fluid, dehydrated and broken wall of algae and oil will flow from the nozzle 11 into the separation tank 20 through the line 9, and will be separated, and then the carbon dioxide fluid will flow into the pipeline 2, most of the grease and more The dehydrated and further broken algae which are further removed by the water will flow into the line 5, and the water and the other part of the oil will flow into the line 21. Most of the dehydrated and broken walls of the line 5 will flow to the feed port 26 of the extruder 30 and into the extruder 30. The alcohol material can be introduced into the extruder 30 via line 31. In one embodiment, extruder 30 is a twin screw extruder. The configuration of the extruder 30 can be similar, but not limited to, the configuration of the extruder 10 shown in Fig. 1, and similarly, other unit components not shown in the drawings, such as a power sealing section and a kneading block, can be used as appropriate. (kneading block) and tooth block, and can use any other arrangement and combination. In addition, for the sake of simplicity, other parameters and components related to the extrusion process, such as stirring cam, temperature control loop, The design of the vacuuming circuit, the vapor lock or the hollow screw, and the compounding feed port for changing the viscosity of the fluid are omitted and not described in detail. Through the mixing action of the twin-screw extruder 30, the fat and oil can be efficiently esterified with the alcohol to become an ester. The above alcohols include alcohols having a carbon number of less than 5, such as decyl alcohol, ethanol or other alcohol solvents having a high polarity. For example, when the oil is esterified with sterol, a mercapto ester is obtained. In one embodiment, in addition to the alcohol species, the 201122092 catalyst can also be introduced into the extruder 30 via line 31, thereby further enhancing the efficiency of the esterification reaction. The above catalyst is preferably a solid powder, including sodium hydroxide, potassium hydroxide or magnesium oxide, but is not limited thereto, and it may be a substance having other types such as sodium decylate. The ester material and the algae residue flow from the extruder 30 into the extraction tank 40 via the line 7. The unreacted sterol or the reacted sterol can be recovered or reused from the apparatus by line 33, and the catalyst can be recovered from the extraction tank 40. The algae and esters in line 7 and the carbon dioxide fluid in line 2, after flowing into the extraction tank 40, will flow into the collection line 42 and the carbon dioxide fluid and ester will flow into line 8. . Extraction tank 40 can include a trough or high pressure dad reactor. The extraction tank 40 may have a pressure gauge, a rupture disc, a relief valve, and the like (not shown). The present invention also finds that the method for extracting the oil and fat, and then extracting the obtained ester substance (using the extraction tank) is compared with the typical method of extracting the oil and then performing the esterification reaction. , can get better extraction results. It is to be noted that the carbon dioxide fluid and the ester material flowing into the line 8 will enter the extruder 10, and again follow the above route, and the wet algae material flowing into the extruder 10 from the inlet port 25. Mix with each other. Thereafter, the substance flowing in the separation tank 20 in the line 9 includes an ester substance in addition to the carbon dioxide fluid, the dehydrated and broken algae body and the fat, and the carbon dioxide fluid flows into the line 2 after the separation tank 20 is separated. Some of the oil and fat and dehydrated and broken algae will flow into the line 5, and the ester substance, moisture and another part of the oil will flow into the line 21. The operation of the rest of the device is generally the same as the previous description, and therefore will not be repeated here for brevity. 10 201122092 Another continuous microalgae extraction required for the device Nozzle 78, extruder 54, and stroke device include 4 reservoirs 2, 60. The nozzle knife is spaced from the groove 56, the separation tank %, and the fluid supply, and the bottom of the pressure storage tank 52. High pressure _, nozzle will be described in detail. The line can be constructed to form a dewatering rupture device, after which the nozzle 78 is connected to the extruder & 4:= slot 52. The line 64 is connected to the nozzle _ separation tank 56 to connect the bottling machine 54 and the separation tank 56. The groove mm = 5° Λ line 7G connects the separation groove 56 with the separation and fluid supply H 60 . f/76, = ° #线74 is connected to the separation tank % 52. Green 76 connects the fluid supply 60 to the high pressure reservoir. The present & Ming is continuously extracted according to the apparatus shown in Fig. 3. The moisture-containing wet algae material is transferred to the pressurized storage tank 52 in the same direction as the fluid. The wet algae material and fluid of the Buddhism & \ private_ ^ 3 water can be used in the high pressure storage tank 52. Alternatively, the moisture-rich wet raft is transferred from the official line 62 to the high pressure storage tank 52, and the fluid second body supply 60 is supplied to the high pressure storage tank 52. In an embodiment, the body supply 60 also has the function of compressing the condensed fluid. The above fluid may be a liquid carbon dioxide compressed fluid whose temperature is controlled at _56.6t: to 31, and whose pressure is controlled to be greater than 5.18 Bar (> 5.18 Bar), or the temperature may be controlled to be higher than 31. Generation (>31(8), and the pressure is controlled at a large, 73 Bar (>73 Bar) supercritical carbon dioxide fluid. The continuously flowing carbon dioxide fluid will build up pressure in the high pressure reservoir 52, thereby increasing the inside and outside of the nozzle 201122092 78 The pressure difference between them causes the algal body cell wall of the algae to be broken when the carbon dioxide fluid and the wet algae material in the high pressure reservoir 52 are expanded and ejected by the nozzle 78. The pressure between the inside and the outside of the nozzle 78 The difference is greater than 1 Bar, preferably between 1 Bar and 1, and BarBar between u Bar S ΔΡ S 1,000 Bar). The carbon dioxide fluid ejected from the nozzle 78 and the broken wall wet algae mud material can then be passed to the extruder 54 via line 64. In one embodiment, extruder 54 is a unitary staggered co-rotating twin screw machine. The configuration of the extruder 54 can be similar, but not limited to the configuration of the extruder shown in Fig. 1 and similarly other unit components not shown in the drawings, such as a dynamic seal section, a kneading block, can be used as appropriate ( Kneading block) and tooth block, and can use any other arrangement and combination. In addition, for the sake of simplicity, other parameters and components related to the extrusion process, such as stirring cam, temperature control loop, vacuum circuit The design of the vapor lock or hollow screw and the compounding feed port for changing the viscosity of the fluid is omitted and not described in detail. In the extruder 54, the rotating threaded element assists in the mixing of the dioxide dish fluid with the broken wall wet algae material. Further, during the mixing of the algal mud in the extruder 54, the algal wall of the algal mud is further broken by the pressing or shearing force of the threaded member. According to the above, the wet algal mud material is under the action of the high pressure storage tank 52, the nozzle 78 and the extruder 54. The algal body cell wall structure in the algae mud is largely broken, and a large amount of oil is released. Therefore, the carbon dioxide fluid can sufficiently extract the grease during the agitation and mixing of the extruder 54. Next, the carbon dioxide fluid and the broken wet algae material are introduced into the separation tank 56 from the extruder 54 by the line 66, and then separated through the separation tank 56. 201122092
油脂與二氧化碳流體至管路70，以及水分與藻渣至管路 68。流入管路70的油脂與二氧化碳流體會進入分離槽％， 然後經由分離槽58分離出油脂至管路72，以及二氧化碳 流體至管路74。於實施例中，分離槽58可為多數個並聯 的分離槽（未顯示），以將油脂進一步地分離成DHA、EpAGrease and carbon dioxide fluid to line 70, as well as moisture and algae to line 68. The grease and carbon dioxide fluid flowing into line 70 will enter the separation tank %, and then the grease will be separated to line 72 via the separation tank 58 and the carbon dioxide fluid to line 74. In an embodiment, the separation tank 58 may be a plurality of parallel separation tanks (not shown) to further separate the grease into DHA, EpA.
等局單價產物。流入至管路74的二氧化碳流體可流入流體 供應器60進行壓縮與冷凝，而再次轉變成壓縮二氧化碳流 體，然後經由管路76傳至高壓儲槽52重複使用。上述壓 縮二氧化碳流體包括溫度控制在_ 5 6.6它至3丨.丨它的範圍 内，且壓力控制在大於5.18 Bar(>5.18 Bar)的液態二氧化 碳壓縮流體，或者，溫度則控制在高於3i rc(>3i丨它 :壓於73 Bar(>73 Ba__界二氧化破流 例方法不需要使用任何的有機溶劑即可有效率 本發明的優點在於，連鲭或 用原料並具有極高的產率。再：$置能充分地利 質)。再者，本二::二m他具生物活性物 r::;避“二== 用萃取槽)進行萃取，能(利 的、特徵、和優點能更明 ’作詳細說明如下： 為讓本發明之上述和其他目 顯易懂’下文特舉出較佳實施例 201122092 【實施例1:以超臨界二氧化碳流體萃取破壁藻粉】 將破壁藻粉10 g放入高壓萃取槽中，在壓力為4,500 psi、溫度為60°C的條件下，以超臨界二氧化碳流體進行萃 取7小時’而得到微藻粗脂肪1.8g。換算粗脂肪的萃取率 為18.0 wt%。接著，取出〇.5g微藻粗脂肪加入1〇 ml濃度 為〇·5 N的氫氧化鉀/曱醇溶液中，然後加熱至1〇〇。〇進行 皂化反應10分鐘。接著加入1〇 ml濃度為〇 7 N的鹽酸/ 曱醇’及14wt%三氟化硼/甲醇溶液，並在溫度為i〇〇〇c的 條件下進行酯化反應10分鐘。以氣相層析儀定量分析得到 的微藻脂肪酸甲酯（Fatty Acid Methyl Esters; FAME)為 〇.436g。以數學式:(〇 436/〇.5)xl8 wt%，換算出以破壁藻粉 為分母下的微藻脂肪酸曱酯萃取率為157wt〇/〇。 【比較例1 :以超臨界二氧化碳流體萃取未破壁藻粉】 將未破壁藻粉1〇 g放入高壓萃取槽中，在壓力為4,5〇〇 psi、溫度為60°C的條件下，以超臨界二氧化碳流體進行萃 取7小時’而得到微藻粗脂肪1.0 g。換算粗脂肪的萃取率 為 10.0 wt%。 接著，取出0.5g微藻粗脂肪加入10 ml濃度為〇 5 N 的氫氧化鉀/曱醇溶液中，然後加熱至100。〇進行皂化反應 10分鐘。接著加入1〇 ml濃度為0.7 N的鹽酸/甲醇，^ 14wt%三氟化硼/甲醇溶液’並在溫度為loot的條件下進 行酯化反應10分鐘。以氣相層析儀定量分析得到的微藻月t 肪酸甲酯（Fatty Acid Methyl Esters, FAME)為 0.27g 〇 LV 备 & 从數 201122092 學式:(0.27/0.5)xl0 wt%，換算出以未破壁藻粉為分母下的 微藻脂肪酸曱酯萃取率為5.4 wt%。 【貫施例2 ·以超臨界二氧化碳_流體卒取澡粉的自旨化 溶液】 將10 g未破壁藻粉加入10 ml濃度為0.5 N的氫氧化 鉀/曱醇溶液中，然後加熱至l〇〇°C進行皂化反應10分鐘。 接著加入10 ml濃度為0.7 N的鹽酸/曱醇，及14wt%三氟 • 化硼/曱醇溶液，並在溫度為100°C的條件下進行酯化反應 10分鐘。然後將得到的溶液放入高壓萃取槽中，在壓力為 4,500 psi、溫度為60°C的條件下，以超臨界二氧化碳流體 進行萃取1.5小時，接著以氣相層析儀定量分析，得到微 藻脂肪酸曱酯的重量為1.26g。換算脂肪酸曱酯的萃取率為 12.6 wt%。 【比較例2 :以溶劑萃取藻粉的酯化溶液】 • 將10 g未破壁藻粉加入10 ml濃度為0.5 N的氫氧化 鉀/曱醇溶液中，然後加熱至l〇〇°C進行皂化反應10分鐘。 接著加入10 ml濃度為0.7 N的鹽酸/曱醇，及14wt%三氟 化硼/曱醇溶液，並在溫度為100°C的條件下進行酯化反應 10分鐘。然後以庚烷對得到的溶液進行萃取，共計5次並 費時5小時，接著以氣相層析儀定量分析，得到微藻脂肪 酸甲酯的重量為〇.7g。換算脂肪酸曱酯的萃取率為7.0 Wt% 0 15 201122092 【實施例3 :以液態二氧化碳流體乾燥（或脫水)並萃取 破壁藻泥】 將250g的未破壁藻粉置入珠磨機中’並持續地研磨 10分鐘以得到破壁藻液。然後將破壁藻液置於局速離心機 中，於8,000 rpm的轉速下離心10分鐘，而得到離心物_ 含水率為82.4wt%的破壁藻泥。取20g破壁議泥（内含3.52g 藻體；其粗脂肪有20 wt% ’亦即是此藻體含有0·704 g粗 脂肪）置於萃取槽内，在壓力為4,700 psi、溫度為30.8°C的 條件下，以液態二氧化碳流體進行萃取12小時’而得到微 藻粗脂肪0.5 g。以數學式子：（0.5/0.704)*1〇〇 wt% ’換算粗 脂肪的萃取率為71.0 wt%。此外，在萃取過後所取出的萃 餘物為粉狀物，而非濕泥狀’其含水率僅剩10.0wt%。 【比較例3:以液態二氧化碳流體乾燥（或脫水)並萃取 未破壁藻泥】 將50g未破壁藻粉加入10〇g蒸餾水中，經連續攪拌 12個小時之後，得到含水率為72.6wt%的未破壁藻泥。取 25g未破壁藻泥（内含6.85g藻體；其粗脂肪有20 wt%，亦 即是此藻體含有1.37 g粗脂肪）置於萃取槽内，在壓力為 4,700 psi、溫度為30.8°C的條件下，以液態二氧化碳流體 進行萃取13小時，僅得到微藻粗脂肪0.2 g。以數學式: (0.2Λ·37)*1〇〇 wt%，換算得粗脂肪的萃取率為14.6 wt%。 此外，在萃取過後所取出的萃餘物為沙狀物，而非濕泥狀’ 其含水率尚達50.0wt%。 201122092 【實施例4:以雙螺桿擠出機進行藻泥脫水】 利用螺旋幫浦，以12.5 kg/cm2的出料壓力將將含水率 為71.5wt%的未破壁藻泥打入雙螺桿擠出機中，接著雙螺 桿擠出機的螺桿以600rpm的轉速將藻泥擠壓而往前運 送，約1分鐘左右，藻泥即被推送至壓力達到14 kg/cm2 的出口處，然後，受到高壓的藻泥在經過出口之兩片孔徑 為200 mesh過濾片之後，會被分離成藻體與水分。得到的 藻體為表面乾燥的藻塊，並測其含水率為60.4wt%，換算 • (((71.5-60.4)/71.5)* 100 %)可得到雙螺桿擠出機對藻泥的脫 水率達15.5%。 雖然本發明已以數個較佳實施例揭露如上，然其並非 用以限定本發明，任何所屬技術領域中具有通常知識者， 在不脫離本發明之精神和範圍内，當可作任意之更動與潤 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。 17 201122092 【圖式簡單說明】 第1圖顯示本發明的連續式萃取裝置。 t 一-之擠出機的内部構造示意圖。 裝置 第3圖顯讀據本發明概念㈣—個連續式微藻萃取 【主要元件符號說明】 1〜管線；2〜管線；3〜管線；4〜管線；5〜管線；6〜管線；# 7〜管線；8〜管線；9〜管線；10〜掩出機；u〜喷嘴；13〜管 線；15〜管線；20〜分離槽；21〜管線；22〜分離槽；25〜入料 口； 26〜入料口； 30〜撥出機；31〜管線』〜管線；40〜萃取 槽；41〜流體供應器；42〜管線；4S〜段；46〜 47〜螺紋段；52高壓儲槽；54擠出機；％分離槽；％分離 槽’ 60流體供應益；62管路；64管路；66管路；68管路； 70管路；72管路；74管路；76管路；78喷嘴。 18Equal unit price product. The carbon dioxide fluid flowing into line 74 can flow into fluid supply 60 for compression and condensation, and again into a compressed carbon dioxide stream, which is then passed via line 76 to high pressure storage tank 52 for reuse. The above compressed carbon dioxide fluid comprises a liquid carbon dioxide compressed fluid whose temperature is controlled within a range of _ 5 6.6 to 3 丨. 且, and whose pressure is controlled to be greater than 5.18 Bar (> 5.18 Bar), or the temperature is controlled above 3i Rc(>3i丨 it: pressed at 73 Bar (>73 Ba__ boundary dioxide oxidation flow method does not require any organic solvent to be effective. The advantage of the present invention is that the crucible or the raw material has a pole High yield. Again: $ fully capable of quality.) Again, this two:: two m he has bioactive substance r::; avoid "two == with extraction tank" for extraction, can (profit, The features and advantages of the present invention will be described in detail as follows: To make the above and other aspects of the present invention readily apparent, the following is a detailed description of the preferred embodiment 201122092. [Example 1: Extraction of broken algae powder by supercritical carbon dioxide fluid 】 10 g of broken algae powder was placed in a high-pressure extraction tank, and extracted with supercritical carbon dioxide fluid at a pressure of 4,500 psi and a temperature of 60 ° C for 7 hours to obtain a microalgae crude fat of 1.8 g. The extraction rate of crude fat was 18.0 wt%. Then, 〇.5g micro was taken out. The crude fat of the algae was added to a 氢氧化·5 N potassium hydroxide/decanol solution, and then heated to 1 Torr. The saponification reaction was carried out for 10 minutes, followed by the addition of 1 〇ml of 〇7 N hydrochloric acid/曱l' and 14wt% boron trifluoride/methanol solution, and esterification reaction at a temperature of i〇〇〇c for 10 minutes. Quantitative analysis of microalgae fatty acid methyl ester by gas chromatography (Fatty Acid Methyl Esters; FAME) is 436.436g. The mathematical formula: (〇436/〇.5)xl8 wt%, the extraction rate of microalgae fatty acid oxime ester under the dehydration of the broken algae powder is 157wt〇/〇. [Comparative Example 1: Extraction of unbroken algal flour by supercritical carbon dioxide fluid] 1 〇g of unbroken algal flour was placed in a high pressure extraction tank at a pressure of 4,5 psi and a temperature of 60 ° C. Under the condition, extraction with supercritical carbon dioxide fluid for 7 hours' gives microalgae crude fat 1.0 g. The extraction ratio of crude fat is 10.0 wt%. Next, 0.5 g of microalgae crude fat is taken out and added to 10 ml of concentration 〇5 N In a potassium hydroxide/decanol solution, then heated to 100. The saponification reaction was carried out for 10 minutes. 1 〇ml concentration of 0.7 N hydrochloric acid/methanol, 14 wt% boron trifluoride/methanol solution' and esterification reaction at a temperature of loot for 10 minutes. Quantitative analysis of the microalgae by gas chromatography Fatty Acid Methyl Esters (FAME) is 0.27g 〇LV 备& From 201122092 Formula: (0.27/0.5)xl0 wt%, converted to the denominator of unbroken algae powder The algae fatty acid oxime ester extraction rate was 5.4 wt%. [Example 2] Self-directed solution of supercritical carbon dioxide_fluid bath powder] 10 g of unbroken algae powder was added to 10 ml of a 0.5 N potassium hydroxide/decanol solution, and then heated to The saponification reaction was carried out for 10 minutes at 10 °C. Next, 10 ml of a 0.7 N hydrochloric acid/nonanol solution and a 14 wt% boron trifluoride/decanol solution were added, and the esterification reaction was carried out at a temperature of 100 ° C for 10 minutes. Then, the obtained solution was placed in a high-pressure extraction tank, and extracted with a supercritical carbon dioxide fluid at a pressure of 4,500 psi and a temperature of 60 ° C for 1.5 hours, followed by quantitative analysis by gas chromatography to obtain microalgae. The weight of the fatty acid oxime ester was 1.26 g. The extraction ratio of the fatty acid oxime ester was 12.6 wt%. [Comparative Example 2: Extraction of an esterified solution of algal flour by solvent] • Add 10 g of unbroken algal flour to 10 ml of a 0.5 N potassium hydroxide/nonanol solution, and then heat to l ° ° C The saponification reaction was carried out for 10 minutes. Next, 10 ml of a 0.7 N hydrochloric acid/nonanol solution and a 14 wt% boron trifluoride/decanol solution were added, and the esterification reaction was carried out at a temperature of 100 ° C for 10 minutes. Then, the obtained solution was extracted with heptane for 5 times and took 5 hours, and then quantitatively analyzed by a gas chromatograph to obtain a microalgae fatty acid methyl ester having a weight of 〇.7 g. The extraction ratio of the converted fatty acid oxime ester is 7.0 Wt% 0 15 201122092 [Example 3: Drying (or dehydrating) with liquid carbon dioxide fluid and extracting the broken algae mud] Putting 250 g of unbroken algal flour into the bead mill' It was continuously ground for 10 minutes to obtain a broken algae solution. Then, the broken seaweed liquid was placed in a local speed centrifuge, and centrifuged at 8,000 rpm for 10 minutes to obtain a centrifuged diatom mud having a water content of 82.4% by weight. Take 20g of broken mud (containing 3.52g of algae; its crude fat is 20wt% 'that is, this algae contains 0.704g of crude fat) placed in the extraction tank at a pressure of 4,700 psi, at a temperature of Under the condition of 30.8 ° C, the extraction was carried out with a liquid carbon dioxide fluid for 12 hours to obtain 0.5 g of microalgae crude fat. The extraction ratio of the crude fat in the mathematical formula: (0.5/0.704) *1 〇〇 wt% ' was 71.0 wt%. Further, the raffinate taken out after the extraction was a powder, not a wet mud, which had a moisture content of only 10.0% by weight. [Comparative Example 3: drying (or dehydrating) with liquid carbon dioxide fluid and extracting unbroken algal mud] 50 g of unbroken algal flour was added to 10 g of distilled water, and after continuously stirring for 12 hours, a water content of 72.6 wt was obtained. % of unbroken algae mud. Take 25g of unbroken algae mud (containing 6.85g algae; its crude fat is 20wt%, that is, the algae contains 1.37g of crude fat) placed in the extraction tank at a pressure of 4,700 psi and a temperature of 30.8 Under the condition of °C, extraction with liquid carbon dioxide fluid for 13 hours, only 0.2 g of microalgae crude fat was obtained. In the mathematical formula: (0.2Λ·37)*1〇〇 wt%, the extraction ratio of the crude fat was 14.6 wt%. Further, the raffinate taken after the extraction was a sand, not a wet mud, which had a moisture content of 50.0% by weight. 201122092 [Example 4: Dehydration of algae sludge by twin-screw extruder] Using a screw pump, the unbroken algal mud with a water content of 71.5 wt% was driven into a twin-screw extrusion at a discharge pressure of 12.5 kg/cm2. In the machine, the screw of the twin-screw extruder is then squeezed at 600 rpm to carry forward the slurry. About 1 minute later, the algae is pushed to the outlet at a pressure of 14 kg/cm2, and then subjected to The high-pressure algae will be separated into algae and moisture after passing through two outlets with a 200 mesh filter. The obtained algae is a dry algae block, and the water content is 60.4 wt%, and the dehydration rate of the algae is obtained by the twin-screw extruder by (((71.5-60.4)/71.5)* 100%). Up to 15.5%. While the invention has been described above in terms of several preferred embodiments, it is not intended to limit the scope of the present invention, and it is possible to make any changes without departing from the spirit and scope of the invention. And the scope of the present invention is defined by the scope of the appended claims. 17 201122092 [Simple description of the drawings] Fig. 1 shows a continuous extraction apparatus of the present invention. t--The schematic diagram of the internal structure of the extruder. Figure 3 of the device is read according to the concept of the present invention (four) - a continuous microalgae extraction [main component symbol description] 1 ~ pipeline; 2 ~ pipeline; 3 ~ pipeline; 4 ~ pipeline; 5 ~ pipeline; 6 ~ pipeline; # 7 ~ Pipeline; 8~ pipeline; 9~ pipeline; 10~ masking machine; u~ nozzle; 13~ pipeline; 15~ pipeline; 20~ separation tank; 21~ pipeline; 22~ separation tank; 25~ inlet port; Feed port; 30~ dialing machine; 31~ pipeline 』~ pipeline; 40~ extraction tank; 41~ fluid supply; 42~ pipeline; 4S~ section; 46~47~ threaded section; 52 high pressure storage tank; Exit; % separation tank; % separation tank '60 fluid supply benefit; 62 pipeline; 64 pipeline; 66 pipeline; 68 pipeline; 70 pipeline; 72 pipeline; 74 pipeline; 76 pipeline; . 18