201237162 -六、發明說明： 【發明所屬之技術領域】 本發明係_於—種具雜及多魏自動化生麵以微生物固 態發酵反齡統’尤指—種充份麵自然能源、有效節省能源，及培 養基質之發酵、乾燥及殺菌一貫化作業的技術。 【先前技術】 按固態發酵技術具有節水、節能的優勢，近年來固態發酵技術已 逐漸成為研究的新熱點。固態發酵是微生物培養的一種方式使用固 態物質當作培養基質，讓微生物生長在上面。在固態發酵令，固體培 養基質是不溶於水的聚合物，不僅提供微生物所需營養，還作為細胞 的固定物，能提供微生物所需—切營養的培養基質被認為是理想培養 基質。培養基質在固態發酵中具有獨特的作用，它影響微生物發酵過 程的質傳、熱傳及微生_代謝魏^近幾年，_發酵越來越受 到研究者_注。研究顯示，關發酵有很多伽，其中最大的優點 是培養基質材料成本低、利用率高。由於農產品加工殘渣數量大，碳 水化合物等營養素豐富，非常適合於絲狀真菌的生長，所以固態發酵 是農產品加工固態廢料的良好利用途徑，且對環境污染小，可能會成 為代替深層發酵生產發酵食品、酶及其他特殊細胞代謝產物的-種有 效技術。然而，固態發酵過程存在培養基質成分不均、缺乏自由水及 固體顆粒細卿_，目崎細㈣爾、帅、溫度 和濕度等培養參數馳娜度鼓，械賴生物生_學及熱質 量傳遞數學模型研究較少，限制了固態發酵生物反應器的可控操作， 201237162 -阻礙了賴發酵製程朗和擴大，如參考文獻⑴。 國内外對於氩能替代石化燃料的前景抱持著相當的_，氣經濟 社會的基礎可由再生資源，如生質原料，做為氣氣生產的主要來源， 而不需再依賴高污染的化石燃料。氫氣的生產方法有3種，分別是熱 化學法、電化學法及生物法。利用生物法產氫可在常溫常壓下進行’，’、 也可應驗廢水與廢棄滅理來麟統，_有乾淨、節能、不消 耗資源等伽，是-觀合賴發展的方法，因㈣起各國的重視。 以微生物生產氫氣，可分為光合作用和非光合作用兩種。其中光合作 用微生物需要歧來累積生長所需的能量，並以水或有機物產氮。在 光合作用微生物中，有許多可在厭氧情況下產氫，其中以紫色不含硫 細菌效率最佳’它以光為能量來源，把有機物質如有舰、醣類等^ 全分解’並產生氫氣，這種反應稱作光發酵反應。非光合微生物則藉 由有機質厭氧發酵生產氫氣，因不需光源，所以稱作暗發酵反應。因 此，暗發酵產氫是指厭氧微生物使有機質發酵時所伴隨的產氣作用， 常被仙的厭氧產氫菌有梭抱桿菌屬、腸道菌屬等。在產氣發酵過程 中，通常會伴隨乙酸、丁酸、乳酸、乙醇等產物。由於暗發酵產氮與 光發酵產氫的作用縣相，但有先後_，因此若能先暗發酵 把巨大分子的多酶類分解而快速產氫，在這過程中生成的有機酸及醇 類’再經由光發酵繼續分解，進行第二階段產氫。如此，不但可降低 末端排放的有機物含量，也可減少廢核理成本並增加氫氣獲取量: 應是最佳的生物產氫策略。 隨著能源危機與環境問題的日益嚴重，固態發酵技術以其特有的 201237162 —優點引起人們極大的興趣。m態發酵領域的研究及其在資源環境中的 應用取得了進展’主要表現在生物燃料、生物農藥、生物轉化、生物 解毒及生物修復等方面的應用，如參考文獻u，2]。 (-）生物燃料(biQ-fuel):係彻玉農業紐進拥態發酵所生 產生物燃料(biofuel)主要為乙醇。乙醇是產量最大的發酵工業產品， 是清潔燃料工細代表，主要轉為各種可再生性糖類物#(如天然纖 維素）。當前地球上“溫室效應，，的罪魁禍首是c〇2，人們迫切需要一 種不產生0)2 __料^目前能滿足這種需要的就是燃料乙醇。乙 醇疋可再生性麟。_固態發酵技術生產乙醇有許多優點：可消除糖 的萃取過程’節省成本;由於發酵過程減少用水量，而降低發酵罐體積 無廢水，降低能耗等。這是一個有潛力的生產乙醇方法，國外對其研 九相虽多’大多利用酵母菌發酵，也有研究用代謝葡萄糖的細菌菌株 °纖維素原料是地球上最豐富的，並且是每年可再生的有機物質，充 >利用生物技術把再生資源轉化為有高價值物f可以減輕人類面臨的 能源、環境危機。 (一)生物農藥(bi〇-pesticide):生物農藥是一種既不污染環境， 又可殺死害蟲的辦法。大量的文獻表明，最近人們越來越重視利用昆 蟲病原體真菌及寄生真菌來控制害蟲的方法。Despande利用固態發酵 生產真菌殺蟲綱方法（如參考文獻[3])，與賴發酵相比，不僅生 產成本大大降低’而且藥物對害蟲的毒力也提高了。筛選具有殺蟲能 力的真菌疋開發可感染繁殖體(像分生抱子、牙粉抱子、衣原體抱子、 印孢子、受精_子等）的第—步，對真菌與害蟲作用機理理解是生產 201237162 -有=物農_主要研究賴碎考讀[3]。有益真料铜 其重要性。㈣_生咖崎可H真較量產具有 (1)生物轉細〇-加牆围如）：_發酵其中—個 領域就是利用微生物轉化農作物及其廢潰，以提 … 糾對環_污染4物轉化利用的菌株—般為白腐菌二 亞洲及南美洲地區人民最重要的食物之一。但它的蛋白質、維生素 礦物質含量低，也缺乏含硫氨基酸。雜是可食用絲狀真奸分血型 :代表’擁有可把許多不能仙的植物或其麵物降解轉化為有食用 價值的食物的能力。可伽雜麵繁多，目奸㈣大約有讀 多種’其中約8〇種已實現實驗室培育，約2〇種已利用固態發酵技術 進行商業化生| n纖維素作物的剩餘物是動物飼料具有潛力的源 泉’主要由纖維素、半纖維素及部分木質素組成，其蛋白含量低、難 消化、味道差等特點限制它們作為理想飼料的應用； ⑵生物解毒(bioiogicai detoxification广某些工農業殘渣含 有對人體有害的化合物，如咖啡因、氰化氫、聚苯化合物、縣酸等， 對这些殘潰有效糊十分聊。由於它們可導致嚴重環境問題，所以 對匕們的處珊加工錄說是十分必要的事。最近，_發酵已成為 木薯皮、油菜籽粉、㈣皮、咖啡漿等殘潰有效的解毒方法；及 (3)生物修復(Bi〇-remediati〇n):生物修復是利用微生物及其代 謝過程（其產物消除或在體内富集有毒物質）來修復被人類長期生活和 生產所污染和破壞的局部環境，使之重現生機的過程。由於目前環境 201237162 π染日益嚴重’國外學者對生物修復研究相當投人。贿發酵生物技 術是有毒化合物生物降解與環境生物修復的有益工具。 關於微生物固態發酵反應器的設計，已有許多不同形式的反應器 應用在固態發酵過程，包括填充床反應n、轉鼓反應器、氣固相流體 化床反應H 拌式生物反應^，如參考文獻⑷。熱的移除是固態 發酵反應器設計闕考4的主制題，細在職的液態深層發酵系 統，氧氣的供給通常是必須克服的主要關鍵。最近，固態發酵反應器 的重要發展’轉是在量化賴放大财面，如錄現㈣數學模式 、質傳與熱傳的現象等。固態發酵反應II中所發生的現象可大致上分 為大規模現轉小賴現Ua)®紐_纖現象(micn)Scopic) .建立固態發酵中小規模現象的模式有兩個理由，一是需要描述固態 發酵中真菌的生長狀況，另—則是想知道固態發酵中的小規模現象會 如何限制生長。由於複_空間異質性，大部分反應H的模式都使用 較簡單的表示法來描述生長機制，而小規模的傳送現象則被忽略，如 參考文獻[5]。 (b)菌絲生長與死亡的動力模式：雖然已有固態發酵的linear、 exponentia卜l0gistic生長機制的研究，大部分的反應器依然使用 簡單的logistic equation來描述生長機制。這避免無限制的生長， 也避免使贿送絲方程式。財驗性的研究贿生長機制可合理的 預測生物反應器的效率。使用1〇gistic equati〇n描述生長反應器 的操作模式通常不把比生長速率(speeifie grQwth rate)與最大菌體 濃度(maximum biomass concentration)設為常數，而把它們表示為局 201237162 -部溫度的函數。最近有研究將培養的溫度轉變模擬短暫的溫度變化， 因為比生長速率不只是當時溫度的函數，而是與整個培養期間的溫度 變化有關。Arrhenius-type relationships可用來描述死亡速率隨溫 度增加而增加。最近有另一研究指出假設菌體的呼吸速率在發酵培養 的末期會下降’此過程稱為失活（inactivation)，類似於因本質老化 過程造成的死亡。失活的速率被表示為Arrhenius_type equati〇n中 溫度的函數。 (c)建立菌絲生長、擴散、粒子尺寸減小的模式：近十年來，在小 規模現象影響固態發酵生長的研究有很重要的進展。這魏象包括微 生物的生長行為’藉由擴散的部分質傳與培養基質粒子的縮小。 Mitchell卿麟#作碳源，指出培養基質巾灿咖咖％ _散 會限制生長。大部分的gluc_ylase會釋放在表面附近，所以表面 附近驗粉會很快的被水解·，因此較深區域的生長會受葡萄糖釋 放速率的關。氧氣的_在固態發酵祕巾是—個不可避免的問題 嚴重的氧限制會存在單—細胞的biQfilm巾。在真菌隨發酵系統 二位於培養基質表_穿透性_'將會遭遇氧氣限制的問題。而且， 就時間與位置而言，生長會受到可溶性營養物短缺的限制特別是菌 體的卜層區域與發酵的末期。另一個小規模的重要現象就是培養基質 =的縮小。粒子縮小最秘的模錢假設整錄子(培養基質粒子加 尺寸是保持不變的，而培養基質只在菌體_培養基質界面被 而〔耗速率破▼獲得的氧職制。但實驗絲顯稍式並不對 因‘、、、模式_培養基質粒子最後會完全被雜，細實驗顯示發酵 201237162 -末期還有麵的培養基餘子，這可解釋為培養基子巾的水解酵 素擴散速率低，造成内部的大粒子較難接近酵素。 生物反應器工程(Bioreactor Engineering)是生物工程領域中一 個十分重要和非常活躍的分支，是近十幾年來孕育的年輕學科。近年 來由於固態發酵再次的被重視，對於關發酵生物反應器的研究也越 來越多’而且不只是著重在傳統生物反應器的設計，更添加了生物學 的概念，真正將生物學的現代知識與工程學的現代知識融合成一體， 發展出更接近微生物真正生長環境的固態發酵生物反應器，如參考文 獻[5，6]。近十年來，有許多不同形式的生物反應器使用在固態發酵 系統中。可依授拌與通氣分為六類。依撥拌可分為三類：培養基質床 可靜止，也可減職㈣勝，或是_摘麟。依通氣可分為 兩類：空氣可在培養基質床循環，也可強制通氣通過培養基質。 Mitchell et al如參考文獻.[7]將固態發酵反應器分類如圖丨所示： (1) 實驗至等級·如 Petri dishes，jars，widemouthErlenmeyer flasks，Roux bottles and roller bottles 等型式。其構造簡單， 大多無強制通氣或攪拌’僅調節培養溫度。代表性系統有：〇RST〇M team bioreactor ; INRA team bioreactor ;幾種 drum bi〇react〇r。 (2) 試量產與工業生產等級（固態培養基質重量在幾公斤至幾公嘲 範圍）：在將產量放大時，設計上會有下列問題產生，如：1.熱移除困 難，2.菌絲易受機械授拌破壞；3.必須減少人為汙染，品質才可以標 準化，可量化生產；4·人力成本考量。由於試量產與工業生產等級固 態發酵槽構造複雜’大多因通氣不足，造成熱傳與質傳上的問題。通 201237162 _常有兩種設計··丨.在鱗顧附近通氣；2·穿過培養基質臟又分成 無混合、間歇或連續混合床）。 控制固態發酵反應器最重要的操作參數有床溫、邱、固態培養基 質的水含量，因為_只能在此小範_操作參數中生長。培養基質 床⑴_cbed)的册與通氣也是重要的因素。最後，養分的濃度與 代謝的氣齡彡響了生物量(biQraass)與代觸產生速率，_，這些參 數很難控制，如參考文獻[8]。 一 固態發酵系統之賴放大（scale_up)不健是把小系統轉變成 大系統的-種方法，也是將實驗室規模轉換成商業化規模的重要關鍵 ，提供大量誠物量’所以可能需㈣評估產物和有毒物f。規模放 大牵涉__如參考文獻[9]所餘括：（1)g量生成的變化：微生 物的培養，在生長上料產生變化，在較大的發_裡，異種(如恤） 的數量將會更高。⑵大規模接種體的生長：在大規模發賴中，較大 量的接種體生產，形細顯的單位操作系統，向來是由數個接菌體發 酵槽來增加其容量。s«要在生長鱗基和轉參數上做—些必要 的改變。⑶培養基滅菌：在大雌的培養基滅菌會引起許多問題，如 溫度分佈、培養基的物化轉變、營養物質的熱退化、有毒物質的形成 。⑷通氣：在實驗室中’通氣是在培養瓶中授拌，然而在域模發酵 裡，則是使用強迫通氣(forces aerati〇n)。⑸搜拌：在好氣發酵裡 ’授拌是個很重要_素，它確保了系_均勻，包含溫度、氣體環 境。間歇性的攪拌通常都會比連續性的攪拌要來的好，因為降低了菌 體的傷害和打斷菌絲的機會。（6)熱移除：在發酵的過程中會產生大量 201237162 的代謝熱’它的速度正比於系統中的代謝活性。此外，機械熱也會因 會攪拌和通氣的注入而產生’所以在靜態固態發酵系統所產生的機械 熱會比動態固態發酵系統還低許多。在較大的反應器會額外的使用熱 交換器。蒸發冷卻(Evaporativecooling)常被拿來使用，它的熱移除 效果都比熱傳導和熱對流好，且能夠移除約80 %的熱。（7)固體的濕 度：水對固體的物化性質有深深的影響，甚至影響到它的產率。在發 酵槽内，培養基濕度和相對濕度最重要的因子，使用高濕度的培養基 和空氣約90-98%，能夠有效的維持固體的濕度。（8)pH控制：在固態 發酵系統中，雖然pH電極能夠測量濕潤固體的pH值，但在缺乏自 由水的情況下，要偵測pH值是非常困難的。最好的pH控制方法是， 酸和驗在想要喊度下融人水中’然射人發賴内，這種技術能克 服規模放大上的問題。⑼污染控制：一般而言，預防措施如果沒有做 好，在賴放大的過程中容易發生污染問題。因此採取高比率的接種 體來控制污染f此外，低濕度、pH值的培養基也_很有用的降低 污染物的成長。 如參考文獻[10]之研究顯示，成功的大規模商業化固態發酵過程 的發展受到了未知的質傳與熱傳現象的_。然而，在建立模式的進 展上，對規模放大的固態發酵過程做了許多合理的量化(卿^恤㈣ 研究。⑴規模放大的數學模式：對於傳_填充床生物反應器而言， 在發酵過程中’右有一溫度不超過反應器任何時間的任一溫度時則 =不:填充床生物反應器高度的限制。增加進口氣體的表面流速與管 的高度，可除去溫度限制塔高的因子，但可能導致過高的壓降與流 201237162 -體化。對於Zymotis填充床生物反應器而言，若熱量傳送板保持5cm 的間隔，將使得隨塔増加的溫度達到最小值，而不需要過高的進口氣 體表面流速。因此溫度不再是限制塔高的因子，幾公尺的塔高似乎可 行，但須考量過高的塔高是否會造成過高的壓降。對於任何規模轉鼓 反應器而言’成功的溫度控制需要通氣速率大於2 vvm (v〇lumes 〇f air per total volume of bioreactor per minute)，使用相對的乾 空氣(e.g. 15%RH)，來促進headspace的空氣氣化。但須注意隨時 補充水分，藉由間歇性的喷灌水氣到移動床(m〇vingbed)上。（2)規模 放大之dimensionless number的研究：對於填充床生物反應器與轉 鼓反應器，能量平衡中的熱產生與熱移除項被提出來，而將比值當成 一個無因次參數(dimensionless number)。無因次參數可用來建構操 作圖，指出控制床溫所需的操作變數。近年來規模放大的技術：近 年來對於固態發酵規模放大問題的了解增加許多，因此有一些策略 被提出’然而有-些還沒經過實際的證明，管如此，數學模式所描 述的固L發酵生物反應⑽傳送現象將是—俯旨導規模放大過程的有 力工具。 如附件1圖表所示為近五年_有關微生物發酵與乾燥研究之石員 士’文。另-方面，依據目前所知習用的固體發酵技術大致可分為下 列幾種方式： ⑴太空包：其係為目前最廣為普及的培養技術，但是其仍然以人 —培養方式為主’不但耗費人力，生產量也受到—定限制太空包的 容量為視袋體大小而定，袋子愈大通氣量愈差，產量約為lkg，產量若 12 201237162 為2公斤以上則會因為厚度的關係而無法生長。太空包攪拌方式則是以 人工翻動（-天約-次)為主。濕度控制方面則利用出口處排出多餘水 分，因此，愈大包裳排水愈不易。太空包滅菌方式則是以人工分裝至 太空包後滅菌培養溫度，且1公斤以上容易產生發酵熱。而接種方式則 是採用搖動均勻的方式來接種真菌。 上述習用結構雖然具有於生產過程較不易污染，且施以小包裝接 種較易均勻之優點，惟，仍然具有生產過程較耗費人力、生產量受到 限制以及大量生產散熱勿易等缺失的產生。 (2) 直立式發酵槽：其產量約1〇〇吆(受限於培養基質厚度），攪拌 方式為機器上下翻堆的方式，濕度控制則以喷霧加水來控制，且底層 具有排水裝置，因而水分較易流失〜朗方式則以蒸氣濕式滅菌由 财分不會堆積，所峨賴培養基質含水量低。培養溫度係以冷空 氣注入方式來控溫，於接種真菌時會使邊緣較不易均句的現象產生。 代表性專利刖案如本國專利第M35G554號『通濕氣怪溫固態發酵槽』、 第M313678號『非固定式固態發酵裝置』以及中國大陸新型專利第 «_19Υ 式生物深層固態發酵反應裝置』，該等習用結構雖 然具有恒濕、溫等自_節設備、具有排水設備⑽免滅狀培養過 程中培養基質糊化以及可以降低發酵溫度等優點 ，惟，其仍然有水份 谷易散失培養過程需補充水分、且接不易均句以及大量培養受 到培養基質厚度的限制等諸多缺失的產生。 (3) 队式發賴：其產量職祕斤，無齡賴培養後期會因 太過潮屬而無去產抱方式為度旋轉式齡翻堆，濕度控制則 13 201237162 -以喷霧加水控财式紅，由於鱗捕置的緣故，所财分不易排 出，滅菌方式則是以蒸氣濕式來滅菌，所以水分易留在槽體内，因此， 滅菌時注意培養基質糊化情形，培養溫度則以冷空氣注入方式來杵 溫，於接種真菌時會使邊緣較不易均勻的現象產生。代表性專利前案 如本國專利第M364709號『微生物培養設備』，該習用結構雖然具有怪 濕、溫等之自動控制設備及360度旋轉式機器翻堆等功能，因而具有水 分不易散失、攪拌較為均勻以及原地滅菌等優點，惟，其並無排水設 備’所以培養基質會在滅菌及培養過程中糊化，而且槽體因為無法排 水而產生積水的情事。再者，該習用結構雖然設備比較成熟，在發酵 過程中，滅菌、溫控、通氣、攪拌、加濕等操作相對容易，可以進行 連續的工廠化生產’發酵原料體積最大可達到百啼級，但是卻不利於 木黴菌產孢。 ' (4)盤式發酵：其容量視盤子大小而定，產量每盤約2公斤（盤子愈 大產量愈同，解決厚度的問題，但較耗人力），其培養基質厚度為薄層 故不需翻動，濕度控制則以覆蓋塑膠袋或紗布防止水分散失，培養後 期以人工輸方絲排水。關方姻是培養基縣關，之後在無 菌操作臺以人工方式將培養基質平舖在盤子上，且薄層發酵熱較易散 失，其接種方式則以搖動均勻方式來接種真菌。代表性專利前案如本 國專利第M532G7號『量產固態發酵盤』所示，其係為目前所知最佳的 木黴菌生產方法’係湘盤式的方式培養，不但可以克服培養基厚度 所造成的發育問題’同時克服太空包生產產量受限的瓶頸，因而具有 薄層不需要翻動、熱較易散失以及接種較為均勻等優點。惟，盤式發 201237162 酵法仍有耗費人賴_受到_，而且無法原地滅菌，而且盤式發 酵法大多未使用自動化生產監測監㈣統，造成工人勞義度大滅 菌困難、容易雜、難於控制溫度以及濕度等製程上的諸多缺失產生。 【發明内容】 本發明主要目的’在於提供—種可以放大生產的具節能及多功能 自動化生產模組之微錄固態發酵反應器系統，不僅具有自態發酵與乾 燥-貫化製程，而且可以多組串聯献單—操作使用，藉以大幅節省 電能的耗費，並降低操作^備的購置成本，以符合環保節能與綠色製 造的需求，並可改善產熱與培養基質厚度的問題，藉以達到節能與原 地滅菌之功效，因而具有改善微生物的發酵品質與良率、模組化串接、 放大生產、自動化以及改善人力需求問題等諸多的特點。 為達上述功效本發明採用之技術手段係包括至少一反應器、一廢 熱回收模組、一太陽能熱汽供應殺菌模組及一太陽能光電手段，反應 器包括一具有腔室的箱體，腔室内供置入至少一容器，容器裝填一預 定量之接種有微生物菌種的培養基質，廢熱回收模組包括一第一冷媒 導f、一第一冷媒導管、一壓縮機、一水槽、一入水管、一出水管、 一儲水筒、一膨脹閥及一預定量冷媒；第一冷媒導管設置於反應器内 部’第二冷媒導管與第一冷媒導管連接形成一循環迴路，壓縮機及膨 脹閥設置在循環迴路上，壓縮機用以驅使冷媒於循環迴路流動；入水 管及出水管一端分別與水槽連接，入水管另一端與一冷水源連接，出 水管另一端與儲水筒連接；太陽能熱汽供應殺菌模組包括一太陽能集 熱手段、一水源供應組件及一空氣源’太陽能集熱手段利用太陽熱能 15 201237162 -而使水源供應組件之水與空氣源之空氣形成高溫水汽；太陽能光電手 段將電能儲存於電力供應手段，以供應系統所需電源。 【實施方式】 壹.本發明之構想 請參看第-至三圖所示，本發明是—種可以放大生產的具節能及 多功此自動化生產模組之微生物固態發酵反應系統，不僅具有固態發酵 與乾燥-體化功能，而且可以多組串聯操作使用，或是單組獨立操作 使用，藉以大幅節省電能的耗#，並降低操作設備購置成本，藉以符 合環保節能與綠色製造的需求，並可改善產熱與培養基質厚度的問 題’藉以達到節能與原地滅菌之功效，因而具有可改善良率、模組化 設計、放大生產、自動化職改善人力需求問題等諸多的特點。 貳•本發明之基本具體實施例 請參看第-至三圖及第五圖所示，基於前述目的，本發明所設計 的系統確實可達成發酵、升溫乾燥及殺菌一貫化。其一種具體 基本實施例係包括至少一反應器（10)、一乾燥模組(2)、一太陽能熱 汽供應殺_組(3〇)及-太陽能光電手段⑷）。此反應器⑽）包括一 具有腔室⑽）的箱體⑽，此腔室⑽）内可供置入至少一容器 (50) ’該容器⑽)可以裝填-預定量之接種有微生物g種的培養基質 (51) 。乾燥模組⑵包括一太陽能熱氣供應模組⑽)及一廢熱回收模 組(20)太陽熱氣供應模組(2〇〇)包括一太陽能集熱手段(2〇1)及一 空氣源供餘件⑽2)，於乾糾，域源供應組件⑽)供應空氣， 由太陽月b集熱手段(201)加熱形成高溫乾燥空氣，並供應至腔室（11〇) 201237162 -内以配合進行乾燥。至於廢熱回收模組(20)則包括一第一冷媒導管 (21)、一第二冷媒導管（22)、一壓縮機(23)、一水槽(24)、一入水管 (25)、一出水管(26)、一儲水筒（27)、一膨脹閥（28)、一預定量冷媒 及一排水手段（13)。第一冷媒導管（21)設置於反應器（1〇)内部，第二 冷媒導管（22)則與第一冷媒導管(21)連接形成一裝填有冷媒的循環迴 路’上述壓縮機(23)及膨脹閥（28)設置在該循環迴路上。具體的連結 方式為’入水管(25)與出水管(26)—端分別與水槽(24)連接，入水管 (25)另一端則與一冷水源連接’出水管（26)另一端與儲水筒（27)連 接。當啟動乾燥時’ 一方面太陽能熱氣供應模組(2〇〇)之空氣源供應組 件(202)供應空氣，由太陽能集熱手段(2〇1)加熱形成高溫乾燥空氣， 並將高溫乾燥空氣供應至腔室（11〇)内部以配合進行升溫乾燥，另一方 面壓縮機（23)驅使冷媒於循環迴路流動，腔室（11 〇)内水份凝結在第一 冷媒導管（21) ’滴落在腔室（11〇)底部，由設置在腔室（11〇)底部的排 水手段(13)排除。其中，高溫乾燥空氣的熱量高於廢熱回收模組(2〇) 在配合乾燥時所收走的熱量，故仍能達成升溫乾燥的目的。 太陽能熱汽供應殺菌模組(30)包括一太陽能集熱手段(31)及一水 源供應組件(32)，其中，太陽能熱汽供應殺菌模組(30)之太陽能集熱 手段(31)可與太陽能熱氣供應模組(2〇〇)之太陽能集熱手段(2〇1)同一 個，如第四圖所示。太陽能集熱手段(31)係利用太陽熱能使水源供應 組件(32)之水形成高溫水汽，送入腔室（11〇)内部以進行殺菌。此外， 太陽能光電手段(41)將電能經一電源處理電路(42)轉換處理後儲存於 電力供應手段(40)，藉以供應系統所需的電源。當培養基質（51)發酵 201237162 ‘及乾燥完成時’即可將各容器（50)自反應器（10)内逐一取出，以供 粉碎及包裝’進而達到精密監控以提升培養基質（51)的發酵品質。 冷媒於第一冷媒導管（21)時，吸收培養基質（51)所排放的廢熱而 成為氣化的冷媒，進而將腔室（110)内的溼氣冷凝結為水，以達到冷卻 與乾燥的作用。另一方面，冷媒經過水槽（24)之前則受到壓縮機（23) 壓縮而成為高溫高壓的氣化冷媒，當高溫高壓的氣化冷媒進入水槽（24 ) 時’則可將熱能排出以對水槽(24)的冷水進行加熱作用，此時，廢熱 回收模組(20)再將熱水輸送至儲水筒（27)中。當高壓氣化冷媒通過膨 脹閥（28)時’則可膨脹還原成低溫低壓的液態冷媒，如此重覆循環作 用，即可調節腔室（11〇)内的溫度與濕度。 參·本發明各組件之具體實施例 3.1反應器 «青參看第至二圖及第八圖所示，本發明反應器（1〇)内的腔室 (110)可供裝填有培養基質（51)的容器（50)置放，讓培養基質（51)得以 實行一貫化發酵與乾燥製程，於一種較為具體的實施例中，可以依據 使用需求輪歧應n⑽的數量，使反應H⑽達到多組串聯操作 使用，藉以節省電能的耗費，並降低操作設備購置成本等諸多目的， 基於前述功效’反應n⑽的數量為複數個，且各反絲（⑻係分別 與乾燥模組(2)之太陽能熱氣供應模組⑽）、廢熱回枚模組(2〇)及太 陽能熱汽供應殺菌模組(30)組接。當培養基質⑸）於發酵階段時，可 透過廢熱回收模組(20) ’或是太陽能熱汽供應殺菌模組(3〇)使腔室 (110)内的溫度維持在攝氏25〜32度，濕度則維持在79〜98%。當培養 201237162 -基質（51)於乾燥階段時，乾賴組⑵之太陽能熱氣供應模組(腦)及 廢熱回收模組（20)配合運作而使腔室（110)内的溫度維持在攝氏38 度，濕度則維持在13~10%的範圍。再者，可於每一腔室（HQ)設置一 置放架（12)，此置放架（12)具有複數呈上下排列可供容器（2〇)置放的 置放槽（120)’如第一、二圖所示，第一冷媒導管(21)係沿著置放槽（12〇) 而彎繞設置，以獲得較佳且溫、溼度調節較為均勻的效果。 3. 2環境條件控制手段 請參看第一、二、五圖及第六圖所示，本發明環境條件控制手段 (60)主要用以感測各反應器（1〇)之腔室（no)的溫度、澄度、空氣流 量等環境狀態’並可依據監測及比對結果來控制乾燥模組(2)之太陽能 熱氣供應模組(200)及廢熱回收模組(20)的運轉。環境條件控制手段 (60)係包含至少一用以感測腔室（110)溫度狀態的溫度感測器（61)、至 少一用以感測腔室（110)溼度狀態的濕度感測器（62)、至少一用以感測 腔室（110)空氣流量狀態的空氣流量感測器（63),及一整合控制器 (64)，其可對溫度狀態、濕度狀態及空氣流量狀態進行監測，並分別 與溫度預設值、濕度預設值及空氣流量預設值進行比對，再依據比對 結果輸出至少一控制訊號’藉以控制太陽能熱氣供應模組(2〇〇)及廢熱 回收模組(20)的運轉，進而調節腔室（11〇)内的溫、渥度以及空氣流 量。 凊參看第一、二圖及第六圖所示，於一種更為具體的實施例中， 環境條件控制手段(60)更包含至少一用以感測腔室（11〇)光照狀態的 光源感測器（65)及至少一用以感測腔室（11〇)氣體成份的氣體分析儀 201237162 -(66)。並於腔室（11_設有至少—光源組件⑽，独整合控制器⑽ 對腔至（110)内的光照狀態進行監測，並與光照預設值進行比對，再依 據比對結果控制光源組件(68)的光源亮度。光源組件⑽)的具體實施 例疋複數組LED燈具，此複數组led燈具可以分別架設在置放架（a) 之複數個置放槽（120)的上方，如第一、二圖所示。 再者’氣體分析儀(65)用以分析腔室（no)内氣體成份而得知基 質的pH值狀態，以供了解基質的發酵狀況，俾供做相應處理之參考 或是進行腔室（110)内部溫度、濕度之調節控制。 3. 3溫度與溼度的調控實施 請參看第一、二圖及第四圖所示，本發明腔室（11〇)内的溫、溼 度調節是由廢熱回收模組⑽）或是太陽能熱氣供應模組(_來加以 實現。儲水筒（27)具有一用以輸出熱氣的第一氣口（27〇)，此第一氣口 (270)與-第-熱氣輸送手段⑽-端連接。太陽能熱汽供應殺菌模組 (30)之太陽能集熱手段(31)則與一第二熱氣輸送手段(71) 一端連接， 此第一熱氣輸送手段(70)另端及第二熱氣輸送手段(71)另端分別與一 第-控f1!閥(72)之二個入口連接，第一控制閥(π)的出口則連接一第 三熱氣輸送手段⑽，第-控侧⑽可受觀條件控制手段⑽的 觸發選擇由太陽能熱汽供應殺菌模組(3〇)或是儲水筒（27)來供應第三 熱氣輸送手段(75)内的熱氣；另-方面，第三熱氣輸送手段(75)另端 及太熱氣供應模組(200)之太陽能集熱手段(2〇1)分別與一第二控 制閥（76)之二個入口連接，第二控制閥（76)的出口則與反應器（1〇)之 腔室（110)連接’第二控制閥（76)可受環境條件控制手段(6〇)的觸發選 20 201237162 擇由第三熱氣輸送手段(75)或是太陽能熱氣供應模組（200)來供應腔 室（110)的熱氣。 一般而言，在發酵與乾燥的階段是由儲水筒（27)來供應腔室（11〇) 大約攝氏50〜65度的高溼度熱氣，以對腔室（11〇)的溫、溼度進行調 節。當培養基質（51)完成發酵乾燥製程而被取出時，則是由太陽能熱 汽供應殺菌模組(30)來供應腔室（110)大約攝氏1〇〇〜125度的高溼度 熱氣，以對腔室（110)内部進行原地滅菌的步驟。 進一步來說，第一熱氣輸送手段(70)與第二熱氣輸送手段(71)各 自包含有一氣管（73)及一送風機(74)，此送風機(74)可受環境條件控 制手段(60)的控制將各氣管（73)内的熱氣導引至反應器（1〇)的腔室 (110)内，且環境條件控制手段(6〇)包含至少二壓力感測單元(69)，當 氣管（73)的壓力超過預設值時，環境條件控制手段(6〇)則關閉送風機 (74)，以調節各氣管(73)的氣壓；又，為將第一冷媒導管（21)的冷凝 水排至腔室（110)外，係於反應器（10)底部設有一排水手段（13)，可利 用一電磁閥來控制排水手段(13)作動時機。於另一種可行實施例中壓 力感測單元⑽亦可裝設在第三減輸送手段㈤巾，以監控及調節 第二熱氡輸送手段(75)内的熱氣壓力，如第一、二圖所示。 請參看第-、二圖及第四圖所示，太陽能集熱手段(31)包含至少 -用以吸收太陽光之幅雛的餘管（⑽）。水驗應組件⑽包含至 少一第一管體⑽)及泵浦⑽），上述太陽能熱汽供應賴模組⑽ 則包含至少-第二管體(33)及-儲熱槽(35)，第一管體⑽)一端與儲 水筒⑽之出水口（271)連接，另端則與縫f (剔)—端連接，且第 21 201237162 -一管體(320)另端接設泵浦（37)，用以將儲水筒（27)内之熱水輸送至集 熱管（310)進行再加溫’藉以避免儲水筒（27)内的熱水排放所致的資源 浪費，並可大幅縮短太陽能集熱手段(31)製造熱氣的時間。 又，第二管體(33)—端與集熱管（310)另端連接，其另端則與儲熱 槽(35)連接’且儲熱槽(35)頂部具有一第二氣口（350)，第二氣口（35〇) 與第二熱氣輸送手段(71)—端連接，第三熱氣輸送手段(75)另端及太 陽能熱氣供應模組(200)之太陽能集熱手段(2〇1)分別與一第二控制閥 (76)的一個入口連接，第二控制閥（76)的出口則與腔室（1丨〇)連通，而 且第二控制閥（76)可受環境條件控制手段(6〇)的觸發而選擇由第三熱 氣輸送手段（75)或是太陽能熱氣供應模組（2〇〇)之太陽能集熱手段 (201)來供應腔室（11〇)内的熱氣。 肆·本發明具體實施例的運作 4· 1微生物接種實施 請參看第七圖所示，本發明微生物菌種的具體實施例可以是 -般的有益真g(如木黴g、白僵g、黑僵g、麵、紅槽菌或是 冬蟲夏草）、光合微生物或是非光合微生物，並將有微生物之菌苗 及基質（例如米）置入在液態發酵槽⑽）中，以進行初步的發酵， 再將稻穀放入-壓力鋼⑽中進行蒸煮，再經發泡機⑽冷卻 後送至混合裝置⑽中，崎上苗及基質與稻榖做—混合接 種，以生蚊量的培養基質⑸），如此即可將培養基質⑸）裝填 至合器⑽）内，再將裝填有培養基f (51)的容細)制反應器⑽ 内進行發酵與乾燥製程。 22 201237162 4. 2具體的培養製程運作 凊參看第一、二圖所示，舉有益真菌為例，於培養基質（21)置 入腔室（110)的前三天為發賴，在此細腔室⑴G)的溫度必須控 制在攝氏25〜32度左右’至於濕賴需测在百分之79〜観左右， 由於培養基質⑸）在發酵過程巾會散發出代謝的熱量，所以須對腔 至（110)内的溫度進行瓣’本發娜狀手段係由環麟件控制手 段(60)驅動廢熱回收模組⑽來調降腔室⑽）内的溫度。由於第一 冷媒導管(21)係沿著腔室（11〇)_置放架⑽雜設置，且位於第 -冷媒導管(21)_賴冷_由吸收培養基f⑸）所排放的廢熱而 成為氣化的冷媒，所以可將腔室（11g)_m舒以冷凝為水，並對腔 至（110)的室溫進行冷卻侧，如此即可調降各容器⑽)的床溫。 、另一方面，經過水槽（24)之前的冷媒則受到壓縮機（23)的壓縮而 成為高溫高壓的氣化冷媒’ t高溫高壓的氣化冷舰人水槽⑽時， 高溫高壓化冷_可將減翻⑽水槽⑽的冷舒以加熱成 為熱水’廢熱晚餘⑽)再將齡魏雜水筒(27)進行儲存及保 /里此時第-控fi陳72)受到環境條件控制手段⑽）的觸發而使儲水 筒（27)的熱減由第—熱氣輸送手段⑽)經第三熱氣輸送手段⑺)供 應至腔室（11G)内，進而使腔室⑴〇)的溫度轉在攝氏25〜32度濕 度則維持在79〜類左;έ· ’當高魏化冷縣娜關(28)時，則可膨 脹還原成液態冷媒’如此重覆循環伽，即可制調_室⑴〇)内的 概度與濕度。在此同時，魏條件_手段⑽驅使統組件(⑻將 腔室（110)内的照度調節在25Glux、12GD/N左右，藉以營造出有利 23 201237162 •於培養基質（51)發酵的環境空間。 於培養基質（51)置入的後三天為乾燥期，在此期間腔室〇⑻的 濕度必須控制在百分之13〜1〇%的範圍内，由於位於第一冷媒導管（21) 内的冷媒可以吸收培養基質⑻所排放的廢熱而成為氣化的冷媒所 以將腔室⑽）内的戰蒸發而冷凝成為水，同時關閉第—控制闕 (72) ’並啟動乾燥模組⑵之太陽能熱氣供應模組⑽)及廢熱回收模 組(20)配合運作，而使腔室⑴〇)内的溫度維持在攝氏35 4〇度，濕度 則維持在13〜1_，如此即可相魏作用。其中，若培養基質 ⑼進入乾燥階段，腔室（的溫度低於預設溫度（如攝氏38度） 時’本，可反轉控制電路讓壓縮機⑽輸送冷媒的方向反 之’第-冷媒導管⑵）内的冷媒受到壓縮機⑽壓縮而成為 间脈回墨的乱化冷媒，當高溫高壓的氣化冷媒進入反應器⑽之腔室 (110)時’則可將熱能排出以對腔室（11〇)内的空氣進行加溫，如此 可達到腔室（110)加熱乾燥的運作。 大約少於10天左右即可完成培養基質（21)的發酵與乾燥製 ί依ίΓΓ"架⑽上之容器⑽以如第九圖所示的取送手段⑽ ’再將裝財培養基f⑸）的㈣（5 粉碎及包裝喻，在_，第—酬瞻 == 段⑽的觸發而使太陽能集熱手卿以約攝氏1。 氣對腔室⑽）内部進行_，持續運作約2G分鐘 室⑴〇)__作業。 卩K成腔 4·3攬拌手段的實施 24 201237162 請參看第八圖所示，為達到攪拌培養基質（51)目的，本發明更 匕3用以對各谷器（50)上之培養基質（51)進行擾掉的授摔手段 (77) ’此攪拌手段（77)可受環境條件控制手段（⑼）的控制而對容器 (50)進行攪拌，至於攪拌手段（77)的具體實施例可以是一種裝設在 容器（50)上的震動馬達或是超音波震動器，如此即可藉由震動馬達 或是超音波震動器使容器（50)震動，以達到適時翻動培養基質（51) 的功效。 4.4取送手段的實施 凊參看第九圖所示，本發明經模組化串聯的複數個反應器（1 〇)是 沿著一運送路徑而排列設置，並於每一腔室（110)設置一置放架（12)， 並於置放架⑽設置包括複S呈上下排列供容器（50)置放的置放槽 (120)，及複數個樞設於置放架（12)底部的導輪（14)，並沿著上述之運 送路徑設置二條平行並置以供一台車（9〇)滑行其上的導軌（15)，於本 實施例中，第-冷媒導管(21)並非裝設在置放架（⑵上，而是繞設於 腔室⑽）内的局部空間，以利置放架⑽被—抓取手段取出及置入， 為達到自動化取送置放架（12)及容器（50)之目的，此台車(9〇)具有一 平台（91)，可藉由上述抓取手段(本圖式例未示）將置放架（12)由腔室 (110)取出後置放在平台（91)上，並於平台⑻設有複數個供複數個 導輪(14)1合定位的紐⑽，t置放架⑽的導輪(⑷喪合定位在 嵌槽(92)時，即可一縱移手段(本圖式例未示）驅動台車（9〇)沿著二導 執（15)滑行移動至包裝區，以進行包裝與粉碎的製程。具體言之抓 取手段的實施例可以是-般的機械手臂，至於縱移手段可以包含一可 25 201237162 絲力源軸的動力傳遞機構，並以動 力傳遞機構錄糾車(1_賴(相_未示)轉動。 伍•結論 因此藉由上述技術特徵喊置’本伽確實具有以下特點： 1.本發明可以I業化而放大生產，不僅具有_發酵與乾燥一貫 化程而且可以多組串聯或是單一操作使用，藉以大幅節省電能的 耗費、’並咖__谢，谢卿繼色製造的需 求，並可改善產熱與培養基f厚度的問題，藉以達卿能與原地滅菌 之功效，因而具有改善微生物的㈣品質與良率、模減組接、放大 生產、自動化以及改善人力需求問題等諸多的特點。 2.本發明由於採用自動化監測監控量產模式，所以可以減少人 汗染、可提高產量、加速發酵過程及減少人力成本，並可依據客戶需 求而批次產。 、·^所述僅為本發明之一可行實施例，並非用以限定本發明 專利範圍，凡舉依據下列請求項所狀内容、雜錢其精神而 為之其他變化的等效實施，皆應包含於本發明之專職圍内。本發 斤八體界狀結構触，未驗醜物品，且具實用性 與進步性，已符合發明專利要件，爰依法具文提出申請，謹請鲜 局依法核予柄，轉護本”人合法之權益。 【圖式簡單說明】 第圖係係本發明反應器的監控調節實施示意圖。 第二圖係本發明反應賴組化串聯實施的示意圖。 201237162 -第二圖係本發明反應器模組化串聯實施的外觀示意圖。 第四圖係本發明廢熱回收模組的連結控制方塊示意圖。 第五圖係本發明反應器模組化串聯實施的控制方塊示意圖。 第六圖係本發明環境條件控制手段的連結控制示意圖。 第七圖係本發明培養基質接種的流程示意圖。 第八圖係本發明反應器内的具體實施示意圖。 第九圖係本發明取送手段的具體實施示意圖。 附件1:圖表係近五年國内有關微生物發酵與乾燥研究之碩士論文。 附件2 :係參考文獻。 【主要元件符號說明】 (10)反應器 (11)箱體 (110)腔室 (12)置放架 (120)置放槽 (13)排水手段 (14)導輪 (15)導軌 (2)乾燥模組 (200)太陽能熱氣供應模組 (201)太陽能集熱手段 (202)空氣源供應組件 (21)第一冷媒導管 (22)第二冷媒導管 (23)壓縮機 (24)水槽 (25)入水管 (26)出水管 (27)儲水筒 (270)第一氣口 (28)膨脹閥 (30)太陽能熱汽簡殺菌模組 (31)太陽能集熱手段 (310)集熱管 27 201237162 .(32)水源供應組件 (321)泵浦 (35)儲熱槽 (40)電力供應手段 (42)電源處理電路 (51)培養基質 (61)溫度感測器 (63)空氣流量感測器 (65)光源感測器 (68)光源組件 (70)第一熱氣輸送手段 (72)第一控制閥 (74)送風機 (76)第二控制閥 (80)液態發酵槽 (82)發泡機 (90)台車 (92)嵌槽 (320)第一管體 (33)第二管體 (350)第二氣孔 (41)太陽能光電手段 (50)容器 (60)環境條件控制手段 (62)濕度感測器 (64)整合控制器 (66)氣體分析儀 (69)壓力感測單元 (71)第二熱氣輸送手段 (73)氣管 (75)第三熱氣輸送手段 (77)攪拌手段 (81)壓力鍋 (83)混合裝置 (91)平台 28201237162 - VI, invention description: [Technical field of invention] The present invention is based on a kind of heterogeneous and multi-wei automatic noodles, microbial solid state fermentation, anti-age system, especially a kind of natural energy, effective energy saving And the technology of fermentation, drying and sterilization of the culture medium. [Prior Art] According to the solid-state fermentation technology, it has the advantages of water saving and energy saving. In recent years, solid-state fermentation technology has gradually become a new hot spot of research. Solid-state fermentation is a way of culturing microorganisms using solid substances as a culture medium for microorganisms to grow on. In solid-state fermentation, the solid-supporting matrix is a water-insoluble polymer that not only provides the nutrients required by the microorganisms, but also acts as a cell anchorage, providing the microbial-demanding nutrients that are considered to be ideal culture substrates. The culture substrate has a unique role in solid-state fermentation, which affects the quality, heat transfer and micro-generation of the microbial fermentation process. In recent years, _ fermentation has been increasingly influenced by researchers. Studies have shown that there are many gamifications in the fermentation, the biggest advantage of which is the low cost and high utilization rate of the culture substrate. Due to the large amount of processing residue of agricultural products and rich nutrients such as carbohydrates, it is very suitable for the growth of filamentous fungi. Therefore, solid-state fermentation is a good way to use solid waste for agricultural products processing, and it has little environmental pollution and may become a substitute for deep fermentation to produce fermented food. , an effective technique for enzymes and other special cellular metabolites. However, in the solid-state fermentation process, there are uneven composition of the culture medium, lack of free water and fine particles of fine particles, and the cultivation parameters such as Mizaki (four), handsome, temperature and humidity, and the heat and mass transfer. Fewer studies of mathematical models have limited the controllable operation of solid-state fermentation bioreactors, 201237162 - hindering the Lai fermentation process and expanding, as described in reference (1). Domestic and international argon can replace fossil fuels in the future. The economic and social foundation can be based on renewable resources, such as raw materials, as the main source of gas production, without relying on highly polluting fossil fuels. . There are three methods for producing hydrogen, namely, thermochemical methods, electrochemical methods, and biological methods. The use of biological methods for hydrogen production can be carried out under normal temperature and pressure, and can also be used to test wastewater and waste arbitrage. _ There are clean, energy-saving, non-consumption resources, etc. (4) The importance attached by all countries. The production of hydrogen by microorganisms can be divided into photosynthesis and non-photosynthesis. Among them, photosynthesis microorganisms need to differentiate to accumulate the energy needed for growth, and produce nitrogen by water or organic matter. Among the photosynthesis microorganisms, many can produce hydrogen under anaerobic conditions, among which purple sulfur-free bacteria are the most efficient. It uses light as a source of energy, and organic matter such as ships, sugars, etc. Hydrogen is produced, and this reaction is called a photo-fermentation reaction. Non-photosynthetic microorganisms produce hydrogen by anaerobic fermentation of organic matter, which is called a dark fermentation reaction because it does not require a light source. Therefore, the dark fermentation hydrogen production refers to the gas production accompanying the anaerobic microorganisms to ferment organic matter, and the anaerobic hydrogen producing bacteria of the genus is often of the genus Bovis genus and the genus Enterobacter. In the gas fermentation process, products such as acetic acid, butyric acid, lactic acid, and ethanol are usually accompanied. Due to the role of dark fermentation nitrogen production and photo-fermentation hydrogen production, there are successive stages, so if the dark fermentation can be used to decompose the multi-enzymes of large molecules to produce hydrogen rapidly, the organic acids and alcohols formed in this process. 'There is continued decomposition by photo-fermentation to carry out the second stage of hydrogen production. In this way, not only can the organic content at the end of the discharge be reduced, but also the cost of waste disposal and the amount of hydrogen can be reduced: It should be the best biohydrogen production strategy. With the energy crisis and environmental problems becoming increasingly serious, solid-state fermentation technology has attracted great interest with its unique 201237162. Research in the field of m-state fermentation and its application in resource environments have made progress in the application of biofuels, biopesticides, biotransformation, biological detoxification and bioremediation, as in reference u, 2]. (-) Biofuels (biQ-fuel): Biofuels are mainly ethanol produced by the Jinyu Agricultural Newcasting Fermentation Process. Ethanol is the most productive fermentation product, and it is the representative of clean fuels. It is mainly converted into various renewable sugars (such as natural cellulose). The current "greenhouse effect" on the earth, the culprit is c〇2, people urgently need a kind of not producing 0) 2 __ material ^ currently can meet this need is fuel ethanol. Ethanol 疋 renewable lin. _ solid fermentation The technical production of ethanol has many advantages: it can eliminate the sugar extraction process 'saving cost; reduce the water consumption due to the fermentation process, reduce the volume of the fermenter without waste water, reduce energy consumption, etc. This is a potential method for producing ethanol, foreign Although many of its researches are mostly yeast fermentation, there are also bacterial strains that study the metabolism of glucose. Cellulose raw materials are the most abundant on the earth, and are renewable organic substances every year. They use biotechnology to regenerate resources. The conversion to high-value substances can alleviate the energy and environmental crisis facing humanity. (1) Biopesticide (bi〇-pesticide): Biopesticide is a method that neither pollutes the environment nor kills pests. A large number of literatures indicate Recently, people have paid more and more attention to the use of entomopathogenic fungi and parasitic fungi to control pests. Despande uses solid-state fermentation to produce fungal insecticides. The method (such as reference [3]), compared with Lai fermentation, not only greatly reduces the production cost, but also increases the virulence of the drug to the pest. Screening the fungus that has insecticidal ability to develop an infective propagule (like The first step of the separation of the scorpion, the tooth powder scorpion, the chlamydia scorpion, the spores, the fertilization _ son, etc., the understanding of the mechanism of action of the fungus and the pest is the production of 201237162 - have = the peasant _ main research It is beneficial to the importance of copper. (4) _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ It is one of the most important foods for the people of Asia and South America. But its protein, vitamin and mineral content is low, and it is also lacking. Sulfur amino acid. Miscellaneous is edible silky traitor blood type: it means 'having the ability to degrade many plants that cannot be immortalized or their noodles into foods with edible value. There are many kinds of foods, and there are about four kinds of foods. Read a variety of 'about 8 of them have been Now cultivated in the laboratory, about 2 kinds of commercialized raw materials have been produced by solid-state fermentation technology | The residue of n-cell crops is a source of potential for animal feeds. It is mainly composed of cellulose, hemicellulose and some lignin. Low content, indigestible, poor taste and other characteristics limit their application as an ideal feed; (2) biological detoxification (bioiogicai detoxification) Some industrial and agricultural residues contain harmful compounds, such as caffeine, hydrogen cyanide, polyphenyl compounds, counties Acids, etc., are very useful for these scums. Because they can cause serious environmental problems, it is very necessary to record their processing. Recently, _fermentation has become cassava skin, rapeseed powder, (4) Effective detoxification methods such as skin and coffee syrup; and (3) bioremediation (Bi〇-remediati〇n): bioremediation is the use of microorganisms and their metabolic processes (products are eliminated or enriched in toxic substances in the body) Repairing the local environment polluted and destroyed by human long-term life and production, making it a rejuvenating process. Due to the current environment 201237162 π dyeing is getting worse' foreign scholars are quite investing in bioremediation research. Bribe fermentation biotechnology is a useful tool for biodegradation of toxic compounds and environmental bioremediation. Regarding the design of microbial solid-state fermentation reactors, many different forms of reactors have been applied in solid-state fermentation processes, including packed bed reactions, drum reactors, gas-solid phase fluidized bed reactions, H-mixed biological reactions, and Literature (4). The removal of heat is the main problem in the design of solid-state fermentation reactors. In the liquid deep-fermentation system, the supply of oxygen is usually the main key that must be overcome. Recently, the important development of solid-state fermentation reactors has been to quantify the phenomenon of magnifying the financial aspects, such as recording (4) mathematical models, quality transmission and heat transmission. The phenomenon occurring in the solid-state fermentation reaction II can be roughly classified into a large-scale Ua)® New_fiber phenomenon (micn) Scopic. There are two reasons for establishing a small-scale phenomenon in solid-state fermentation. One is to describe the growth of fungi in solid-state fermentation, and the other is to know how small-scale phenomena in solid-state fermentation can limit growth. Due to complex _ spatial heterogeneity, most of the patterns of reaction H use a simpler representation to describe the growth mechanism, while small-scale transmission phenomena are ignored, as in reference [5]. (b) Dynamic pattern of mycelial growth and death: Although there have been studies on the growth mechanism of linear, exponentia and l0gistic solid-state fermentation, most reactors still use a simple logistic equation to describe the growth mechanism. This avoids unrestricted growth and avoids bribing the silk equation. A conscientious study of the bribery growth mechanism can reasonably predict the efficiency of the bioreactor. The use of 1 〇 gistic equati〇n to describe the mode of operation of the growth reactor generally does not set the specific growth rate (speeifie grQwth rate) and the maximum biomass concentration (maximum biomass concentration) as constant, and represent them as the 201237162 - part temperature function. Recent studies have simulated temperature transitions in cultures to simulate transient temperature changes because the specific growth rate is not only a function of temperature at that time, but rather a change in temperature throughout the culture. Arrhenius-type relationships can be used to describe an increase in death rate as temperature increases. Another recent study has pointed out that it is assumed that the respiratory rate of the cells will decrease at the end of the fermentation culture. This process is called inactivation, similar to the death caused by the intrinsic aging process. The rate of inactivation is expressed as a function of temperature in Arrhenius_type equati〇n. (c) Establishing patterns of mycelial growth, diffusion, and particle size reduction: In the past decade, there has been significant progress in the study of small-scale phenomena affecting solid-state fermentation growth. This Wei elephant includes the growth behavior of the microbes' by the partial mass transfer of the diffusion and the shrinkage of the medium particles. Mitchell Qinglin # is a carbon source, pointing out that the culture medium can be used to limit growth. Most of the gluc_ylase is released near the surface, so the powder near the surface will be quickly hydrolyzed, so the growth in the deeper areas will be affected by the glucose release rate. Oxygen in the solid state fermentation of the secret towel is an inevitable problem. Severe oxygen limitation will exist in the single-cell biQfilm towel. In the fungus with the fermentation system two located in the culture table _ penetrating _ ' will encounter oxygen limitation problems. Moreover, in terms of time and location, growth is limited by the shortage of soluble nutrients, especially the layer of bacteria and the end of fermentation. Another important phenomenon on a small scale is the reduction in the quality of the culture medium. The particle shrinks the most secret model money hypothesis. The size of the culture medium is kept constant, and the culture medium is only at the bacterial-medium interface. The oxygen consumption system is obtained. The formula is not completely correct because of the ',,, mode _ culture medium, and the fine experiment shows that the fermentation medium 201237162 - the end of the medium has the surface of the remaining, which can be explained as the low rate of hydrolysis of the hydrolyzed enzyme in the medium towel, resulting in Large internal particles are harder to access to enzymes. Bioreactor Engineering is a very important and very active branch in the field of bioengineering. It is a young discipline that has been bred in the past decade. In recent years, solid-state fermentation has been re-emphasized. There are more and more researches on the fermentation bioreactors' and not only focusing on the design of traditional bioreactors, but also adding the concept of biology, truly integrating the modern knowledge of biology with the modern knowledge of engineering. In one, develop a solid-state fermentation bioreactor that is closer to the true growth environment of micro-organisms, as in the reference [5, 6]. In the past years, there have been many different forms of bioreactors used in solid-state fermentation systems. They can be divided into six categories according to mixing and ventilation. According to the mixing, they can be divided into three categories: the culture bed can be static or reduced (four) wins. Or _ picking. According to ventilation, it can be divided into two categories: air can be circulated in the culture bed, or forced to pass through the culture medium. Mitchell et al. [7] Classification of solid-state fermentation reactors is shown in Figure :: (1) Experiment to grades such as Petri dishes, jars, widemouth Erlenmeyer flasks, Roux bottles and roller bottles. Its structure is simple, and most of it has no forced ventilation or agitation' only the culture temperature is adjusted. Representative systems are: 〇RST〇M team bioreactor; INRA team bioreactor; several drums bi〇react〇r. (2) Trial production and industrial production grade (solid medium weight in the range of a few kilograms to a few squares): When the production is enlarged, the following problems will arise in the design, such as: 1. Hot removal is difficult, 2. The hyphae are easily damaged by mechanical mixing; 3. Man-made pollution must be reduced, quality can be standardized, and production can be quantified; 4. Human cost considerations. Due to the complex structure of the solid-state fermentation tanks in the trial production and industrial production grades, most of them are caused by insufficient ventilation, causing problems in heat transfer and quality transfer. Pass 201237162 _ often have two designs··丨. Ventilation near the scale; 2) through the culture medium and divided into no mixed, intermittent or continuous mixed bed). The most important operational parameters for controlling a solid-state fermentation reactor are the water content of bed temperature, Qiu, and solid medium, since _ can only be grown in this small operating parameter. The culture and bed of the culture bed (1)_cbed) is also an important factor. Finally, nutrient concentrations and metabolic ages swell biomass (biQraass) and generation rate, _, these parameters are difficult to control, as described in [8]. The scale-up of a solid-state fermentation system is a method of transforming a small system into a large system. It is also an important key to transforming the laboratory scale into a commercial scale, providing a large amount of honesty. So it may be necessary to (4) evaluate the product. And toxic f. Scale-up involves __ as described in reference [9]: (1) changes in the amount of g produced: the cultivation of microorganisms, the change in growth, in the larger hair, the number of different species (such as shirts) It will be higher. (2) Growth of large-scale inoculum: In large-scale sputum, a large number of inoculum production, a detailed unit operating system, has always been made up of several bacteria-based fermentation tanks to increase its capacity. s« to make the necessary changes in the growth squama and rotation parameters. (3) Sterilization of medium: Sterilization of medium in large females causes many problems such as temperature distribution, physical and chemical conversion of culture medium, thermal degradation of nutrients, and formation of toxic substances. (4) Ventilation: In the laboratory, 'ventilation is carried out in a culture flask. However, in the field mold fermentation, forced aeration (forces aerati〇n) is used. (5) Searching: In aerobic fermentation, 'mixing is a very important factor, which ensures that the system is uniform and contains temperature and gas environment. Intermittent agitation is usually better than continuous agitation because it reduces the risk of bacterial damage and breaks the hyphae. (6) Heat removal: A large amount of metabolic heat of 201237162 is produced during the fermentation process. Its speed is proportional to the metabolic activity in the system. In addition, mechanical heat is also generated by the injection of agitation and aeration. Therefore, the mechanical heat generated in a static solid-state fermentation system is much lower than that of a dynamic solid-state fermentation system. Additional heat exchangers are used in larger reactors. Evaporative cooling is often used, its heat removal is better than heat and heat convection, and it removes about 80% of the heat. (7) Moisture of solids: Water has a profound influence on the physicochemical properties of solids and even affects its yield. In the fermentation tank, the most important factor of medium humidity and relative humidity, using high humidity medium and air about 90-98%, can effectively maintain the humidity of the solid. (8) pH control: In the solid-state fermentation system, although the pH electrode can measure the pH of the wet solid, it is very difficult to detect the pH in the absence of free water. The best method of pH control is that the acid and the test are in the water, and the technology can overcome the problem of scale-up. (9) Pollution control: In general, if the preventive measures are not done well, it is easy to cause pollution problems in the process of amplification. Therefore, a high ratio of inoculum is used to control pollution. In addition, low humidity, pH media is also useful to reduce the growth of contaminants. Studies such as reference [10] have shown that the development of successful large-scale commercial solid-state fermentation processes has been plagued by unknown quality and heat transfer phenomena. However, in the progress of the establishment model, many reasonable quantifications have been made on the scale-up solid-state fermentation process. (1) Mathematical model of scale-up: For the transfer-bed bioreactor, during the fermentation process In the middle of 'the right temperature does not exceed any temperature of the reactor any time = no: the height of the packed bed bioreactor. Increase the surface flow rate of the inlet gas and the height of the tube, can remove the temperature limit tower factor, but May cause excessive pressure drop and flow 201237162 - for Zymotis packed bed bioreactor, if the heat transfer plate is kept at a 5cm interval, the temperature added to the tower will be minimized without excessively high The surface flow rate of the inlet gas. Therefore, the temperature is no longer a factor limiting the height of the tower. A tower height of a few meters seems feasible, but it is necessary to consider whether an excessively high tower height will cause an excessive pressure drop. For any size drum reactor "Successful temperature control requires a ventilation rate greater than 2 vvm (v〇lumes 〇f air per total volume of bioreactor per minute), using relative dry air (e. g. 15% RH) to promote air gasification in the headspace. However, care must be taken to replenish moisture at any time by intermittently spraying water vapor onto the moving bed. (2) Dimensionless number study of scale-up: For packed bed bioreactors and drum reactors, the heat generation and heat removal items in the energy balance are proposed, and the ratio is treated as a dimensionless number (dimensionless number) ). The dimensionless parameter can be used to construct an operation diagram that indicates the operational variables required to control the bed temperature. The scale-up technology in recent years: In recent years, the understanding of the scale-up problem of solid-state fermentation has increased a lot, so some strategies have been proposed. However, some have not been proved by actual practice. In this way, the solid L-fermented organism described by the mathematical model The reaction (10) transfer phenomenon will be a powerful tool for the scale-up process. As shown in the chart in Annex 1, the stone clerk of the research on microbial fermentation and drying in the past five years. On the other hand, according to the known solid fermentation technology, it can be roughly divided into the following ways: (1) Space package: It is the most widely used culture technology at present, but it is still dominated by human-culture methods. It takes a lot of manpower, and the production volume is also limited. The capacity of the space bag is determined by the size of the bag. The larger the bag is, the worse the ventilation is. The output is about lkg. If the output is 12, 2012,162, 2 kg or more, it will not be because of the thickness. Growing. The space bag mixing method is based on manual turning (-days-times). In terms of humidity control, excess water is discharged from the outlet, so the more the package is drained, the easier it is. The space bag sterilization method is a sterilization culture temperature after manual packaging to a space package, and more than 1 kg is prone to generate heat of fermentation. The method of inoculation is to inoculate the fungus by shaking evenly. Although the above-mentioned conventional structure has the advantages that it is less likely to be polluted in the production process and is easy to be evenly distributed by small packages, it still has the production process which is labor-intensive, the production volume is limited, and the mass production of heat is not easy. (2) Vertical fermentation tank: its output is about 1〇〇吆 (limited to the thickness of the culture medium), the mixing method is the way the machine is turned upside down, the humidity control is controlled by spray and water, and the bottom layer has drainage device. Therefore, the water is more likely to be lost. The lang method is steam-wet sterilization, and the accumulation of wealth does not accumulate. The culture temperature is controlled by cold air injection, and when the fungus is inoculated, the edge is less likely to be uniformly sentenced. Representative patents such as the national patent No. M35G554 "passing the temperature of the solid temperature fermentation tank", the No. M313678 "non-fixed solid state fermentation equipment" and the new Chinese patents «_19Υ biological deep solid state fermentation reaction device", Although these conventional structures have the advantages of constant humidity, temperature, and the like, the advantages of the drainage device (10), the gelatinization of the culture medium during the culture-free culture process, and the reduction of the fermentation temperature, etc., however, there is still a process of water loss and easy to lose the culture process. There are many defects such as the need to replenish water, and the difficulty of the sentence and the large amount of culture limited by the thickness of the culture medium. (3) Team-style slogan: its production job secrets, no aging training will be too late due to too much tide and no production of the way to rotate the age of the turn, humidity control 13 201237162 - spray and water control Because of the scale of the scale, the wealth is not easy to discharge, and the sterilization method is sterilized by steam wet, so the water is easy to stay in the tank. Therefore, pay attention to the gelatinization of the culture medium during sterilization. In the case of cold air injection, the temperature is increased, and when the fungus is inoculated, the edge is less likely to be uniform. The representative patent case is as shown in the national patent No. M364709 "Microbial culture equipment". Although the conventional structure has the functions of automatic control equipment such as strange wetness and temperature, and 360-degree rotary machine turning, it has the advantages of water loss and stirring. It has the advantages of uniformity and in-situ sterilization, but it has no drainage equipment. Therefore, the culture medium will be gelatinized during sterilization and cultivation, and the tank body will not accumulate water to cause water accumulation. Furthermore, although the conventional structure is relatively mature, in the fermentation process, sterilization, temperature control, aeration, agitation, humidification and the like are relatively easy, and continuous industrial production can be carried out. However, it is not conducive to sporulation of Trichoderma. ' (4) Disc fermentation: its capacity depends on the size of the plate, the output is about 2 kg per plate (the larger the plate, the more the same, the problem of solving the thickness, but it is more labor-intensive), the thickness of the culture medium is thin, so it is not Need to flip, humidity control to cover the plastic bag or gauze to prevent water dispersion, and the artificial feed wire is drained in the later stage of cultivation. The Guanfang marriage is the medium county, and then the culture medium is laid flat on the plate on the sterile operation table, and the thin layer fermentation heat is easily lost. The inoculation method is to inoculate the fungus in a uniform manner by shaking. The representative patent case, as shown in the national patent No. M532G7 "production solid-state fermentation tray", is the best known method for the production of Trichoderma's method, which is not only able to overcome the thickness of the medium. The developmental problem 'at the same time overcomes the bottleneck of the production of space capsules, so it has the advantages that the thin layer does not need to be flipped, the heat is easy to be lost and the inoculation is more uniform. However, the tray type 201237162 fermentation method still costs people _ _, and can not be sterilized in situ, and most of the disc fermentation method does not use automated production monitoring and supervision (four) system, resulting in workers laboriously difficult to sterilize, easy to mix, It is difficult to control many defects in processes such as temperature and humidity. SUMMARY OF THE INVENTION The main object of the present invention is to provide a micro-recording solid-state fermentation reactor system capable of amplifying production with an energy-saving and multifunctional automatic production module, which not only has a self-state fermentation and a drying-continuous process, but also can have many Groups are listed in series—operational use, in order to save energy and save the cost of operation, to meet the requirements of environmental protection, energy saving and green manufacturing, and to improve the heat production and the thickness of the culture medium, so as to achieve energy saving and The in-situ sterilization effect has many features such as improving microbial fermentation quality and yield, modular cascading, magnifying production, automation, and improving manpower requirements. In order to achieve the above-mentioned effects, the technical means adopted by the present invention comprises at least one reactor, a waste heat recovery module, a solar thermal steam supply sterilization module and a solar photovoltaic device. The reactor comprises a chamber having a chamber, and the chamber is provided. Providing at least one container for filling a predetermined amount of the culture medium inoculated with the microbial strain, the waste heat recovery module comprising a first refrigerant guide f, a first refrigerant conduit, a compressor, a sink, and a water inlet pipe a water outlet pipe, a water storage pipe, an expansion valve and a predetermined amount of refrigerant; the first refrigerant conduit is disposed inside the reactor; the second refrigerant conduit is connected with the first refrigerant conduit to form a circulation loop, and the compressor and the expansion valve are disposed at In the circulation loop, the compressor is used to drive the refrigerant to flow in the circulation loop; the inlet pipe and the outlet pipe are respectively connected to the water tank, the other end of the inlet pipe is connected with a cold water source, and the other end of the outlet pipe is connected with the water storage cylinder; the solar thermal steam supply sterilization The module includes a solar heat collecting means, a water supply component and an air source 'solar heat collecting means utilizing solar heat 15 2012 37162 - The water source of the water supply component forms a high temperature water vapor with the air source; the solar photovoltaic means stores the electrical energy in the power supply means to supply the power required by the system. [Embodiment] 壹. The concept of the present invention is shown in the first to third figures. The present invention is a microbial solid-state fermentation reaction system capable of amplifying and producing the energy-saving and multi-functional automatic production module, which not only has solid-state fermentation and drying-body function. And can be used in multiple sets of series operation, or a single set of independent operation, so as to greatly save energy consumption, and reduce the operating equipment purchase cost, so as to meet the requirements of environmental protection, energy saving and green manufacturing, and can improve heat production and culture quality. The problem of thickness is to achieve energy saving and in-situ sterilization, so it has many features such as improved yield, modular design, enlarged production, and improved manpower requirements for automation. BRIEF DESCRIPTION OF THE PREFERRED EMBODIMENTS Referring to the first to third and fifth figures, the system designed by the present invention can achieve fermentation, temperature rise drying, and sterilization consistency based on the foregoing objects. A specific basic embodiment thereof includes at least one reactor (10), a drying module (2), a solar heat supply unit (3〇), and a solar photovoltaic device (4). The reactor (10) includes a tank (10) having a chamber (10) into which at least one vessel (50) can be placed. The vessel (10) can be filled with a predetermined amount of microbial species. Culture medium (51). The drying module (2) comprises a solar hot gas supply module (10) and a waste heat recovery module (20). The solar hot gas supply module (2) comprises a solar heat collecting means (2〇1) and an air source for the remaining parts. (10) 2), in the dry correction, the domain source supply component (10) supplies air, is heated by the solar moon b collecting means (201) to form high temperature dry air, and is supplied to the chamber (11 〇) 201237162 - to cooperate to dry. The waste heat recovery module (20) includes a first refrigerant conduit (21), a second refrigerant conduit (22), a compressor (23), a water tank (24), a water inlet pipe (25), and a discharge. A water pipe (26), a water storage tank (27), an expansion valve (28), a predetermined amount of refrigerant, and a drainage means (13). The first refrigerant conduit (21) is disposed inside the reactor (1), and the second refrigerant conduit (22) is connected to the first refrigerant conduit (21) to form a circulation circuit filled with refrigerant (the compressor (23) and An expansion valve (28) is disposed on the circulation circuit. The specific connection method is that the inlet pipe (25) and the outlet pipe (26) are connected to the water tank (24) respectively, and the other end of the inlet pipe (25) is connected with a cold water source. The other end of the outlet pipe (26) is stored. The water cylinder (27) is connected. When the drying is started, on the one hand, the air source supply unit (202) of the solar hot air supply module (2) supplies air, is heated by the solar heat collecting means (2〇1) to form high-temperature dry air, and supplies high-temperature dry air. To the inside of the chamber (11〇), the temperature is heated and dried. On the other hand, the compressor (23) drives the refrigerant to flow in the circulation circuit, and the water in the chamber (11 〇) condenses on the first refrigerant conduit (21). At the bottom of the chamber (11 〇), it is excluded by a drainage means (13) provided at the bottom of the chamber (11 〇). Among them, the heat of the high-temperature dry air is higher than the heat collected by the waste heat recovery module (2〇) when it is combined with drying, so the purpose of heating and drying can still be achieved. The solar thermal steam supply sterilization module (30) comprises a solar heat collecting means (31) and a water source supply component (32), wherein the solar heat collecting means (31) of the solar thermal steam supply sterilization module (30) can be combined with The solar heat collection module (2〇1) of the solar hot gas supply module (2〇〇) is the same as shown in the fourth figure. The solar heat collecting means (31) uses the solar heat to cause the water of the water supply unit (32) to form high-temperature water vapor, which is sent into the chamber (11〇) for sterilization. In addition, the solar photovoltaic means (41) converts the electric energy through a power processing circuit (42) and stores it in the power supply means (40) to supply the power required by the system. When the culture medium (51) is fermented 201237162 'and when drying is completed', each container (50) can be taken out from the reactor (10) one by one for pulverization and packaging' to achieve precise monitoring to enhance the culture medium (51). Fermentation quality. When the refrigerant is in the first refrigerant conduit (21), the waste heat discharged from the culture substrate (51) is absorbed to become a vaporized refrigerant, and the moisture in the chamber (110) is condensed into water to achieve cooling and drying. effect. On the other hand, before the refrigerant passes through the water tank (24), it is compressed by the compressor (23) to become a high-temperature and high-pressure vaporized refrigerant. When the high-temperature and high-pressure vaporized refrigerant enters the water tank (24), the heat can be discharged to the sink. The cold water of (24) is heated, and at this time, the waste heat recovery module (20) transfers the hot water to the water storage tank (27). When the high-pressure gasification refrigerant passes through the expansion valve (28), it can be expanded and reduced to a low-temperature low-pressure liquid refrigerant. By repeating the cycle, the temperature and humidity in the chamber (11〇) can be adjusted. Specific embodiments of the various components of the invention 1 Reactor «Green As shown in Figures 2 and 8 , the chamber (110) in the reactor (1〇) of the present invention can be placed in a container (50) filled with a culture medium (51), allowing The culture substrate (51) can be subjected to a consistent fermentation and drying process. In a more specific embodiment, the reaction H(10) can be used in multiple sets of series operations according to the number of uses of the required wheel n(10), thereby saving power consumption. And reduce the operating equipment purchase cost and many other purposes, based on the aforementioned effect 'reaction n (10) the number of multiple, and each reverse wire ((8) and the dry module (2) solar hot gas supply module (10)), waste heat back to the module The group (2〇) and the solar thermal steam supply sterilization module (30) are connected. When the culture medium (5) is in the fermentation stage, the temperature in the chamber (110) can be maintained at 25 to 32 degrees Celsius through the waste heat recovery module (20)' or the solar thermal steam supply sterilization module (3〇). The humidity is maintained at 79 to 98%. When the 201237162-matrix (51) is cultured in the drying stage, the solar hot gas supply module (brain) of the dry-laid group (2) and the waste heat recovery module (20) cooperate to maintain the temperature in the chamber (110) at 38 degrees Celsius. Degree, humidity is maintained in the range of 13 to 10%. Furthermore, a placement rack (12) can be provided in each chamber (HQ), and the placement rack (12) has a plurality of placement slots (120) arranged up and down for the container (2〇). As shown in the first and second figures, the first refrigerant conduit (21) is bent along the placement groove (12〇) to obtain a better and uniform temperature and humidity adjustment effect. 3. 2 For the environmental condition control means, as shown in the first, second, fifth and sixth figures, the environmental condition control means (60) of the present invention is mainly for sensing the temperature of the chamber (no) of each reactor (1〇). Environmental conditions such as sufficiency, air flow, etc. The operation of the solar hot gas supply module (200) and the waste heat recovery module (20) of the drying module (2) can be controlled based on the monitoring and comparison results. The environmental condition control means (60) comprises at least one temperature sensor (61) for sensing the temperature state of the chamber (110), and at least one humidity sensor for sensing the humidity state of the chamber (110) ( 62) at least one air flow sensor (63) for sensing the air flow state of the chamber (110), and an integrated controller (64) for monitoring the temperature state, the humidity state, and the air flow state And respectively comparing with the preset temperature value, the humidity preset value and the preset value of the air flow, and then outputting at least one control signal according to the comparison result to control the solar hot gas supply module (2〇〇) and the waste heat recovery mode The operation of group (20), in turn, regulates the temperature, humidity and air flow in the chamber (11 〇). Referring to the first, second and sixth figures, in a more specific embodiment, the environmental condition control means (60) further comprises at least one sense of light source for sensing the illumination state of the chamber (11 〇). A detector (65) and at least one gas analyzer 201237162-(66) for sensing the gas composition of the chamber (11 。). And in the chamber (11_ is provided with at least the light source assembly (10), the integrated controller (10) monitors the illumination state in the cavity to (110), and compares with the preset value of the illumination, and then controls the light source according to the comparison result. The brightness of the light source of the component (68). The specific embodiment of the light source component (10)) is an array of LED lamps, which can be respectively mounted above the plurality of placement slots (120) of the placement frame (a), such as The first and second figures are shown. Furthermore, the 'gas analyzer (65) is used to analyze the gas composition in the chamber (no) to know the pH state of the matrix, in order to understand the fermentation state of the substrate, and to provide a reference for the corresponding treatment or to carry out the chamber ( 110) Adjustment control of internal temperature and humidity. 3. 3 For the implementation of temperature and humidity control, please refer to the first, second and fourth figures. The temperature and humidity adjustment in the chamber (11〇) of the present invention is determined by the waste heat recovery module (10) or the solar hot gas supply module. The water storage cylinder (27) has a first air port (27〇) for outputting hot air, and the first air port (270) is connected to the first-hot gas conveying means (10)-end. The solar heat steam supply sterilization The solar collector means (31) of the module (30) is connected to one end of a second hot gas conveying means (71), and the other ends of the first hot gas conveying means (70) and the second hot gas conveying means (71) are respectively respectively Connected to two inlets of a first control f1! valve (72), the outlet of the first control valve (π) is connected to a third hot gas delivery means (10), and the first control side (10) can be triggered by the condition control means (10) Selecting the solar thermal steam supply sterilization module (3〇) or the water storage cylinder (27) to supply the hot gas in the third hot gas conveying means (75); on the other hand, the third hot gas conveying means (75) is the other end and too The solar heat collecting means (2〇1) of the hot gas supply module (200) are respectively connected to the two inlets of a second control valve (76) The outlet of the second control valve (76) is connected to the chamber (110) of the reactor (1). The second control valve (76) can be triggered by the environmental condition control means (6〇). The three hot gas conveying means (75) or the solar hot gas supply module (200) supplies the hot air of the chamber (110). Generally, in the stage of fermentation and drying, the chamber is supplied by the water storage tank (27) (11) 〇) High-humidity hot air of about 50 to 65 degrees Celsius to adjust the temperature and humidity of the chamber (11〇). When the culture medium (51) is taken out of the fermentation drying process, it is supplied by solar thermal steam. The sterilization module (30) supplies a high humidity hot gas of about 1 to 125 degrees Celsius in the chamber (110) to perform the step of sterilizing the inside of the chamber (110). Further, the first hot gas conveying means (70) and the second hot gas conveying means (71) each comprise a gas pipe (73) and a blower (74), and the blower (74) can be controlled by the environmental condition control means (60) to be in each gas pipe (73) The hot gas is guided into the chamber (110) of the reactor (1〇), and the environmental condition control means (6〇) package At least two pressure sensing units (69), when the pressure of the air pipe (73) exceeds a preset value, the environmental condition control means (6〇) turns off the blower (74) to adjust the air pressure of each air pipe (73); In order to discharge the condensed water of the first refrigerant conduit (21) to the chamber (110), a drainage means (13) is arranged at the bottom of the reactor (10), and a solenoid valve can be used to control the drainage means (13) to actuate In another feasible embodiment, the pressure sensing unit (10) may also be installed in the third reducing conveying means (five) towel to monitor and adjust the hot gas pressure in the second heat transfer means (75), such as the first and second The figure shows. Referring to Figures -, 2, and 4, the solar collector (31) includes at least - the remaining tube ((10)) for absorbing the sun's fluff. The water test component (10) includes at least a first pipe body (10) and a pump (10), and the solar heat steam supply module (10) comprises at least a second pipe body (33) and a heat storage tank (35), One end of the pipe body (10) is connected to the water outlet (271) of the water storage cylinder (10), the other end is connected to the slit f (tick) end, and the second end of the 21 201237162 - one pipe body (320) is pumped (37). ), used to transport the hot water in the water storage tank (27) to the heat collecting tube (310) for reheating 'to avoid waste of resources caused by hot water discharge in the water storage tank (27), and to greatly shorten the solar energy set Thermal means (31) time to produce hot gas. Moreover, the second pipe body (33) end is connected to the other end of the heat collecting pipe (310), the other end is connected to the heat storage tank (35), and the top of the heat storage tank (35) has a second air port (350). The second air port (35〇) is connected to the second hot gas conveying means (71), the third hot gas conveying means (75) is connected to the solar heat supply module (200), and the solar heat collecting means (2〇1) Connected to an inlet of a second control valve (76), the outlet of the second control valve (76) is in communication with the chamber (1丨〇), and the second control valve (76) is subject to environmental conditions ( The triggering of 6〇) selects the hot air in the chamber (11〇) by the third heat collecting means (75) or the solar heat collecting means (201) of the solar hot gas supply module (2〇〇).肆· Operation of a specific embodiment of the present invention 4.1 Microbial inoculation implementation Referring to the seventh figure, the specific embodiment of the microbial strain of the present invention may be generally beneficial to true g (such as Trichoderma g, White Stinger g, Black zombie g, face, red trough or cordyceps), photosynthetic microorganisms or non-photosynthetic microorganisms, and microbial bacterins and substrates (such as rice) are placed in the liquid fermentation tank (10) for preliminary fermentation. The rice is then placed in a pressure steel (10) for cooking, and then cooled by a foaming machine (10) and sent to a mixing device (10). The seedlings and the substrate are mixed with the rice bran to form a medium of the mosquito (5). Thus, the culture substrate (5)) can be loaded into the combiner (10)), and the fermentation and drying process can be carried out in the reactor (10) filled with the medium f (51). 22 201237162 4. 2 Specific culture process operation 凊 See the first and second figures. Take the beneficial fungi as an example. In the first three days of the culture medium (21) placed in the chamber (110), in the thin chamber (1) G) The temperature must be controlled at around 25~32 degrees Celsius'. As for the wetness, it needs to be measured at 79%~観, because the culture medium (5)) will emit metabolic heat during the fermentation process, so the cavity must be (110) The temperature inside the valve is determined by the ring-and-loop control means (60) to drive the waste heat recovery module (10) to lower the temperature in the chamber (10). Since the first refrigerant conduit (21) is disposed along the chamber (11〇)_ placement rack (10), and is located in the first refrigerant conduit (21) _ ly cold _ by the absorption medium f (5)) Since the refrigerant is condensed into water and the chamber is cooled to the room temperature of (110), the bed temperature of each container (10) can be lowered. On the other hand, when the refrigerant passing through the water tank (24) is compressed by the compressor (23) to become a high-temperature and high-pressure gasification refrigerant, the high-temperature and high-pressure gasification cold ship sink (10), high temperature and high pressure cooling The temperature of the water tank (10) will be reduced (10) to be heated to become hot water 'waste heat night (10)) and then the age Wei water tank (27) will be stored and protected/in this case, the first control fi (72) is controlled by environmental conditions (10) The triggering causes the heat reduction of the water storage cylinder (27) to be supplied to the chamber (11G) by the third hot gas transport means (7) via the first hot gas transport means (10), thereby transferring the temperature of the chamber (1) 〇) to Celsius 25~32 degree humidity is maintained at 79~class left; έ· 'When Gao Weihua cold county Naguan (28), it can be swelled and reduced to liquid refrigerant' so repeated cycle gamma, can be adjusted _ room (1)概) the degree of probabilities and humidity. At the same time, Wei condition_means (10) drives the unit ((8) adjusts the illuminance in the chamber (110) to about 25Glux, 12GD/N, thereby creating an environmental space for the fermentation of the culture medium (51). The drying period is the last three days after the culture medium (51) is placed, during which the humidity of the chamber 〇 (8) must be controlled within the range of 13% to 1%, due to being located in the first refrigerant conduit (21). The refrigerant can absorb the waste heat discharged from the culture medium (8) and become a vaporized refrigerant, so that the war in the chamber (10) is evaporated and condensed into water, and the first control 阙 (72) is turned off and the solar energy of the drying module (2) is activated. The hot gas supply module (10) and the waste heat recovery module (20) cooperate to maintain the temperature in the chamber (1) 〇) at 35 degrees Celsius and the humidity at 13 to 1 _, so that the temperature can be maintained. Wherein, if the culture medium (9) enters the drying stage and the chamber (the temperature is lower than the preset temperature (such as 38 degrees Celsius), the reversible control circuit allows the compressor (10) to transport the refrigerant in the opposite direction to the 'first-refrigerant conduit (2) The refrigerant in the refrigerant is compressed by the compressor (10) to become a chaotic refrigerant that is intermittently returned to the ink. When the high-temperature and high-pressure vaporized refrigerant enters the chamber (110) of the reactor (10), heat energy can be discharged to the chamber (11). The air inside the crucible is heated to achieve the heating and drying operation of the chamber (110). Fermentation and drying of the culture substrate (21) can be completed in about less than 10 days. The container (10) on the rack (10) is transported as shown in Figure IX (10) and then the loading medium f(5) (4) (5 smashing and packing the metaphor, in the _, the first - rewards == segment (10) triggers so that the solar collectors are about 1 Celsius. The gas is inside the chamber (10)), and the operation continues for about 2G minutes (1) 〇)__ Homework.卩K into cavity 4·3 mixing means implementation 2012 2012162 Please refer to the eighth figure, in order to achieve the purpose of stirring the culture medium (51), the present invention is further used for the culture medium on each of the cereals (50) (51) Disposing means for throwing off (77) 'This stirring means (77) can be stirred by the environmental condition controlling means ((9)) to agitate the container (50), and a specific embodiment of the stirring means (77) It can be a vibration motor or an ultrasonic vibration device installed on the container (50), so that the container (50) can be vibrated by a vibration motor or an ultrasonic vibration device to achieve timely turning of the culture medium (51). The effect. 4. 4 Implementation of the take-off means 凊 Referring to the ninth figure, the plurality of reactors (1 〇) of the modularized series of the present invention are arranged along a transport path and are disposed in each chamber (110). a placing frame (12), and placing, in the placing frame (10), a placing groove (120) including a plurality of upper and lower arrays for the container (50), and a plurality of pivoting holes at the bottom of the placing frame (12) The guide wheel (14) is provided with two parallel rails arranged in parallel along the above-mentioned transport path for a vehicle (9〇) to slide thereon. In this embodiment, the first refrigerant conduit (21) is not installed. a local space in the shelf ((2), but around the chamber (10)), so that the rack (10) is taken out and placed by the grabbing means, in order to achieve the automatic take-up rack (12) and For the purpose of the container (50), the trolley (9) has a platform (91), and the placement frame (12) can be taken out of the chamber (110) by the above-mentioned grasping means (not shown in the figure). Placed on the platform (91), and on the platform (8) is provided with a plurality of buttons (10) for positioning a plurality of guide wheels (14), and a guide wheel for the t-mounting frame (10) ((4) is positioned in the slot (92) )Time A longitudinal movement means (not shown in the figure) drives the trolley (9〇) to slide along the two guides (15) to move to the packaging area for packaging and smashing. Specifically, the implementation of the grasping means For example, the mechanical arm can be a general arm, and the longitudinal displacement means can include a power transmission mechanism of the 25 201237162 wire source shaft, and the power transmission mechanism can record the vehicle (1_ Lai (phase _ not shown) rotates. Conclusion Therefore, by the above technical features, 'Benga has the following characteristics: 1. The invention can be scaled up and produced by I industrialization, and has not only the process of fermentation and drying, but also multiple sets of series or single operation, thereby greatly saving the consumption of electric energy, and the coffee is manufactured by Xie Qing. Demand, and can improve the heat production and the thickness of the medium f, so that the ability of Daqing can be sterilized in situ, thus improving the quality and yield of microbes, molding reduction, mass production, automation and improving manpower requirements. And many other features. 2. The invention adopts the automatic monitoring and monitoring mass production mode, so that the human sweat can be reduced, the yield can be increased, the fermentation process can be accelerated and the labor cost can be reduced, and the batch can be produced according to the customer's demand. The descriptions are only one of the possible embodiments of the present invention, and are not intended to limit the scope of the patents of the present invention, and the equivalent implementations of other changes according to the contents of the following claims and the spirit of miscellaneous money should be It is included in the full-time enclosure of the present invention. The body of the body is touched by the body, and the ugly items are not tested, and it is practical and progressive. It has been in conformity with the patent requirements of the invention, and the application has been filed according to law. Please ask the fresh bureau to approve the case according to law. Legal Description [Fundamental Description] The figure is a schematic diagram of the monitoring and adjustment of the reactor of the present invention. The second figure is a schematic diagram of the reaction of the present invention in a series reaction. 201237162 - The second figure is the reactor mode of the present invention Schematic diagram of the appearance of the grouped series implementation. The fourth diagram is a schematic diagram of the connection control block of the waste heat recovery module of the present invention. The fifth figure is a schematic diagram of the control block of the modular implementation of the reactor of the present invention. Schematic diagram of the linkage control of the control means. The seventh diagram is a schematic diagram of the flow of the culture medium inoculation of the present invention. The eighth diagram is a schematic diagram of the specific implementation of the reactor of the present invention. The ninth diagram is a schematic diagram of the specific implementation of the means for feeding the present invention. : The chart is a master's thesis on microbial fermentation and drying research in the past five years. Attachment 2: is a reference. [Main component symbol description] ( 10) Reactor (11) Box (110) Chamber (12) Placement rack (120) Placement slot (13) Drainage means (14) Guide wheel (15) Guide rail (2) Drying module (200) Solar energy Hot air supply module (201) solar heat collecting means (202) air source supply unit (21) first refrigerant duct (22) second refrigerant duct (23) compressor (24) sink (25) water inlet pipe (26) Water pipe (27) water storage tank (270) first air port (28) expansion valve (30) solar hot steam simple sterilization module (31) solar heat collecting means (310) heat collecting tube 27 201237162 . (32) Water supply component (321) Pump (35) Heat storage tank (40) Power supply means (42) Power supply processing circuit (51) Culture medium (61) Temperature sensor (63) Air flow sensor ( 65) Light source sensor (68) Light source assembly (70) First hot gas delivery means (72) First control valve (74) Air blower (76) Second control valve (80) Liquid fermentation tank (82) Foaming machine ( 90) trolley (92) slot (320) first tube (33) second tube (350) second air hole (41) solar photoelectric means (50) container (60) environmental condition control means (62) humidity sense Detector (64) integrated controller (66) gas analyzer (69) pressure sensing unit (71) second hot gas conveying means (73) air pipe (75) third hot gas conveying means (77) stirring means (81) pressure cooker (83) Mixing device (91) platform 28