200808665 九、發明說明： 【發明所屬之技術領域】 本發明涉及一種有機污水厭氧處理技術，特別是涉及一種多相內循環厭氧反 【先前技術】 有機廢水是规社會生活的一種必然産物，需要經過有效的處理才能減少對 環麟成污染。目前對於各類有機廢水的生物處理方法有厭氧藤氧兩大類。相 對於好氧生物處理法，厭氧生物處理法具備了更多的優點，包括低漲産率， • 能耗、能源回收等。因此，厭氧生物處理技術是污水生物處理領域最値得大力發 ，励專案。 在厭氧生物處理方法中，到目前爲止，上流式厭氧污泥床（UASB)反應器是 最爲成功的厭氧生物處理工藝，但它也存在許多不足之處，例如在低溫條件下運 行，或在啓動初期，抑或處理較低濃度的有機廢水時，由於不能産生大量沼氣以 造成足夠的擾動，因此反應器中的混合效果較差，從而出現短流造成處理效率 低·，如果提高反應器的水力負荷來改善混合狀況，則會出現污泥流失的狀況々 在厭氧處理方式中，採用分級處理或推流式反應器可以改善水質，甚至會使 厭氧處理的出水水質達到二級標準。分級處理能明顯改善碳水化合物和其他污染 物的厭氧處理，它們的中間産物是丙酸和氫&分級厭氧處理可以補償厭氧過程由 於生麵力學常數K“半速度常數）高所産生的不利效果，麵氧生物的活性增 • 加一倍，面整個處理過程所需的生物量僅爲單級處理的一半。另外，厭氧處理系 統中推流式反應器比完全混合反應器更能有效地適應毒性和環境的衝擊-針對 上述，産生了一種新的厭氧工藝思想-分段多相厭氧反應審(爾PA, Staged Μ碰-Phase A娜r娜㈣，其思路如下：(1难各級分隔的反應室中馴養出適應 環境隨(如麵度、氫分壓、代謝申間産物等 > 及底物成分纖勢厭氧微生物 群落 '②防It系統內各反應室的污麵醒合的現象。(3)各反應室的親醒收 集。(4)系統的水力流態接近推流式，追求更高的處理去除效库及更優良的岀林 質.但所習知的推流式反應器(例如看流室厭氧反應器1 ABR)也存在一些缺 类，蠢方面有：(1)麵_第一反應銶受遠^嫌平均麵的局部麵，如此 可能發生處理纖的降低。(2>進水如何均与分佈的問題。⑶反緻深，否 則水流和麵上升速虔過大，會造成污泥流秀。 9 200808665200808665 IX. Description of the invention: [Technical field of invention] The present invention relates to an anaerobic treatment technology for organic sewage, in particular to a multi-phase internal circulation anaerobic reaction [Prior Art] Organic wastewater is an inevitable product of social life. It needs to be effectively treated to reduce pollution to the ring. At present, there are two major types of biological treatment methods for various types of organic wastewater. Compared to aerobic biological treatment, anaerobic biological treatment has many advantages, including low yield, energy consumption, energy recovery and so on. Therefore, the anaerobic biological treatment technology is the most vigorous and energetic project in the field of sewage biological treatment. In the anaerobic biological treatment method, the upflow anaerobic sludge blanket (UASB) reactor has been the most successful anaerobic biological treatment process so far, but it also has many shortcomings, such as operating under low temperature conditions. , or in the initial stage of start-up, or when processing a lower concentration of organic wastewater, because a large amount of biogas cannot be generated to cause sufficient disturbance, the mixing effect in the reactor is poor, so that short-flow causes low processing efficiency. The hydraulic load will improve the mixing condition, and there will be sludge loss. In the anaerobic treatment mode, the grading treatment or the push-flow reactor can improve the water quality, and even the effluent quality of the anaerobic treatment can reach the secondary standard. . Graded treatment can significantly improve the anaerobic treatment of carbohydrates and other pollutants. Their intermediate products are propionic acid and hydrogen & graded anaerobic treatment can compensate for the anaerobic process due to the high mechanical constant K "half speed constant" The unfavorable effect is that the activity of the surface oxygen biochemistry is doubled, and the biomass required for the entire treatment process is only half of the single-stage treatment. In addition, the push-flow reactor in the anaerobic treatment system is more than the complete mixing reactor. Can effectively adapt to the impact of toxicity and the environment - in response to the above, a new anaerobic process idea - segmented multiphase anaerobic reaction audit (P, PA, Staged, Phase A, Na Na Na (4), which has the following ideas: (1) In the reaction chamber separated by different levels, the environment is adapted to the environment (such as surface, hydrogen partial pressure, metabolic inter-products, etc.) and the substrate component of the anaerobic microbial community The phenomenon of the dirt closes together. (3) The collection of each reaction room is awakened. (4) The hydraulic flow state of the system is close to the push flow type, and the pursuit of higher treatment removal efficiency and better quality forest. Conventional push-flow reactor (see for example There are also some deficiencies in the chamber anaerobic reactor 1 (ABR). The stupid aspects are: (1) the surface _ first reaction 銶 is affected by the local surface of the average surface, so that the treatment fiber may be reduced. (2 > How to deal with the problem of distribution and distribution. (3) The anti-deepening, otherwise the water flow and the surface rising speed will be too large, which will cause the sludge to flow. 9 200808665
ί發明内容I 本發明的爲了 述不足1提種齡上麵種反應器罐 點、具有局部完全混合，達到高有機負荷、高處理效能、耐衝撃負荷、節讎穩 定良好妝Me質S的的多麵循環厭氧反應器。 本發明多枏內循環厭氧反應器，包括多個具有卜Η兩級反應區和相應氣升 管、集氣管、回流管、氣液分離器、三相分雛器、氣封的內循_氧反應室。其 MS在一個反應器池體中SB至少二«用分隔»«、並在_上串聯連 成11«態述內循環厭氧反應室，辦騰內麵厭飯應室MM#懸 並輸同一儀藏離上，或稱騰岀。 本發明多相內循反應器中臓的內》IRft反應室，設沿 室壁延伸到所述反應室底部的導流板’在所述導流板^側的氣封設置在導流板 上，所述的回流管通至導流板和分隔®之間，升働下部設置有m提器。 本發明多相內循環厭氧反應器，在叛述三相分離器隔忠的I級反應區中充塡 細4、顆粒的生物載體’开乡成膨騰床。 本翻多糖lew氧反應器，«提離祕部集氣ww?部布氣筒 _成，集_的下》t勻分佈扇形狀的缺口，所述布氣筒設一收縮喉部，其周屬 均勻分佈著直徑和數量適當的孔口，所述每個孔q有一個對應的導流溝，'所述導 流溝是麵述布器筒的內側，雛部有著相對應于孔口的扇形缺口下繊《所述 收戀管一直到爾織〇。 本發明多相內WR氧麵器，由所述具有氣勤讎麵氧麵室構成， 歷成一個多柑、高有機負荷的厭氧生物處理系統。在整値反應系統中，反應室之 • 間的水力流態爲推流流態，各反應室之間維持一定的底物濃度梯度，使每個反應 室中可以培養出與流至該反應室的基質組成和環境因數（酸鹼度、氬分壓、代謝 中簡産瓣）相讎的優勢微生物群落，形成多相的厭雛理系統。而在軍獨的 反應室中，將厭氧生化反應産生的沼氣利用氣提原理，提升反應室下層的生物載 體或顆粒污泥和底物，造成反應室內部的水力循環，成完全混流的水力流態； 內循環加強了生物污泥和底物的混合接觸，大大的提高有機容積負荷，而由於具 有高有機負荷，相對有高産氣量的沼氣産生，形成高強度的循環流量，在I.級反 應區塡充生物載體，成膨脹床或流化床的狀態，到高處理效率，子穩定的 本發明多相內循環厭氧反應器具有⑴良好的泻泥截論性能，因爲厭氧微生物 的世代期長，反應器保持高潮量是保證厭氧反應器處理高效率的基礎。⑵良好 10 200808665 ~ 齡施態 > 局部輸全齡流能讎進雜質充分&觸> 提高傳質纖，保持微生物具備充分的活往;而整體的推流流態讎系統一定的 基質濃度梯度，充分分解污水中讎質，提高出水水質，良好的微生物相赚 特性，在不同的環境條件下，各反應單元顆丨養適應於所處環境的優勢微生物菌 群，使系統內的不同微生物菌群能在其適應的環境中發揮最大麵g性。⑷反應室 可形成膨脹床或流化床，在高負荷的反應室塡充生物載體，微生物在多孔載體表 商土齒驟密赃讎賺。利用高有機負荷産生的高內循環量，在反應室时7 層反應區形成膨脹床藏化床的狀態，保證反應室內最大的單位體積生麵和維 持高的生物職。⑸具構的厭氧劇酔施做彈触的組 • [實施方式1 以下結合附麗進行詳細說明，以求對本發明的目的和優點得以更深入的理解。 僵1本發明多相內循環反應器的示意圖 圖2本發明多相內循環反廳的視圖 置3本發明多相內循環反應器申氣提器的示意圖 圖t是本發明多相內循環反應器的實施例示意圖。.多相內循環厭氧反應器用 兩個分隔板16分隔成三個內循環厭氧反應室4、5、6，三個內循環厭氧反應室 的結構是一^的^均爲具有二級反應區的內循環厭氧反應室(以下室 在每個反應室中，設麵個三相分離器10、Θ，分勝成T®的I級反驅 和上面的S級反應區，在兩個三相分離器10、θ的斜面上，_成兩個沈澱區，集 氣管連到Π級反應區的三相分離器9，氣升管14連到1級反應區的三相分離 . 器1Ό內的J級反應©，氣升管14下端上有氣提器15，反應室頂_氣液分離 器11，在其下部有回流管13直通到導流板17和分隔板16之間的進流區，反應 室側壁上和兩個三相分離器9、1謂應，設有氣封7、8，在每個反應室的入口1 處有一纖板17直通反應室底部，在導流板17 -側，氣封7、8設在導流板17 內側。 在所述三相分離器10隔出的I級反應區中充塡細小顆粒的生物載體，形成 膨脹床。 氣提器15的結構可見圖2 ,在氣升管14的下部連接每提器15，所述的氣 提器15是由外部集氣筒21和內部布氣筒22所構成。集氣筒21下緣均与分佈 扇形狀的曲線，保證達_均勻布氣的作用。布氣筒22設一收縮喉管，其周圈 均勻分佈著直徑和數量適當的孔口 24，所述每個孔口 24有一個對應的導流溝 11 200808665 2&，導流溝25是從底部有著相對應于孔口 24的扇形缺口下緣順著收縮喉管23 一直到孔口 24，它的作用是形成水力導流的作用。-氣先經外部的集氣筒21收 集，再由內部布氣筒22的孔口 24注入氣提器15內。集氣筒21的下緣均勻分 佈扇形狀的缺口，保證沼氣能均勻的進入集氣筒21 〇布氣筒22的收縮喉管23 上圓周均与分佈直徑和數量適當的孔口 24，每個孔口 24有一個對應的導流溝 25，導流溝25是從底部有著相對應于孔口 24的扇形缺口順著收縮喉管23 —直 到孔口 24 〇它的作用是形成水力導流的作用，當沼氣從均勻分佈的孔口 24注入 氣提審15時，産生文特利（Venturi)效應形成射流，將污水和厭氧生物載體的 細小粒體吸入氣提器15，在收縮喉管23處由於流速增大，形成大的剪切力將氣 體切割成微小的氣泡，造成更徽率的氣徹果和混合攪拌的作用，增大內循環 的循環量和厭氧生物載體的細小顆粒$_物的傳質效率。 P 三個反應室在水力上串聯連接，即前一反應室的出口連接後一反應室的入 口，形成推流式流態。三個麵室的氣液分離器共接同一沼氣排出管3，也可以 單獨排出收集。 在每個反應室中，污水從進水堰1沿導流板流到反應室4底部，由下而上充 滿麵室後由出水堰2流出到第二麵室5，再到第三反應室6 ,最後從出水堰 之流出經過處理的水。 在反應室下部的I級反應區，污水和厭氧生物載體的細小粒體均勻混合，進 行生物降解反應，産生大量的沼氣，三相分離器to分離出大量的沼氣，進入氣 提器15，連同第一反應室下層的泥水混合液提升到反應室頂部的氣液分離器 11，氣體由沼氣排出管3排岀，其中的厭氧生物載體和污水經由回流管13回流 _ 至反應室的進流區和進流液混合，混合液沿著導流板17進入I級反應區的底部， 完成混合液的內部循環。前面已經介紹了氣提器15的作用，由於有了氣提器15， 可以更多地提升I級反應區的泥水混合液，加強水力循環和混合流態，提高污水 和厭氧生物污泥的傳質效率。反應室可選擇性塡充粒徑0.2〜1.〇mm的生物載 體，微生物在多孔載體表面上生成緊密的生物膜結構。利用高有機負荷産生的高 內循環量，在反應室的下層反應區形成膨脹床或流化床的狀態，如此，可保證反 應室內最大的單位體積生物量和維持高的生物活性。 經I級反應區處理後，污水流至上部的Π級反應區作進一步的生化降解反 應，所産生沼氣由三相分離器9收集通過氣升管12送入氣、液分離器11 ; ϋ級反 應區的泥水混合液在沈澱區進行固液分離，沈降的厭氧生物載體的細小粒體返回 Π級反應區；分雛出的污水從第一反應器4的頂部沿第二反應器的職板進入第发明 发明 发明 I Insufficient 1 of the present invention for the above-mentioned reactors, the above-mentioned reactor tank points, with partial complete mixing, to achieve high organic load, high processing efficiency, impact resistance, thrift stability, good makeup, quality S Multifaceted circulating anaerobic reactor. The multi-turn internal circulation anaerobic reactor of the invention comprises a plurality of inner loops having a two-stage reaction zone and a corresponding gas riser, a gas collecting pipe, a return pipe, a gas-liquid separator, a three-phase splitter, and a gas seal. Oxygen reaction chamber. The MS in a reactor cell body SB at least two «separated»«, and connected in series on the _ into the 11 « state of the internal circulation anaerobic reaction chamber, the Teng inside noodles should be room MM # hang and lose the same The instrument is off, or it is called Teng. The inner IRrt reaction chamber of the helium in the multiphase internal reactor of the present invention is provided with a gas seal extending along the chamber wall to the bottom of the reaction chamber, and a gas seal on the side of the deflector is disposed on the deflector The return pipe is connected between the deflector and the partition®, and the lower part of the lift is provided with an extractor. The multiphase internal circulation anaerobic reactor of the present invention is filled with a fine 4, particle biological carrier in the class I reaction zone of the reciprocal three-phase separator. The lysing polysaccharide lew oxygen reactor, «lifting the secret part of the gas collection ww? part of the gas cylinder _ into, set _ the next" t evenly distributed the shape of the fan, the gas cylinder is provided with a contraction throat, the circumference of the uniform There are distributed orifices of appropriate diameter and number, each of the holes q has a corresponding diversion groove, 'the diversion groove is the inner side of the cloth barrel, and the leg has a fan-shaped gap corresponding to the orifice Kneeling, "The love tube has been woven." The multi-phase internal WR oxidizer of the present invention is composed of the anaerobic biological treatment system which has a gas chamber and a surface oxygen chamber. In the whole reaction system, the hydraulic flow state between the reaction chambers is a push flow state, and a certain substrate concentration gradient is maintained between the reaction chambers, so that each reaction chamber can be cultured and flowed to the reaction chamber. The matrix composition and the environmental factors (pH, argon partial pressure, metabolites in the metabolites) are superior to the microbial community, forming a multi-phase anatomical system. In the reaction chamber of the military alone, the biogas generated by the anaerobic biochemical reaction is used to extract the biological carrier or granular sludge and substrate in the lower layer of the reaction chamber, thereby causing the hydraulic circulation inside the reaction chamber to become a completely mixed hydraulic power. The flow state; the inner circulation strengthens the mixed contact of the biological sludge and the substrate, greatly increases the organic volumetric load, and due to the high organic load, relatively high gas production of biogas is generated, forming a high-intensity circulating flow, in I. The stage reaction zone is filled with a biological carrier, into a state of an expanded bed or a fluidized bed, to a high treatment efficiency, and the sub-stable multiphase internal circulation anaerobic reactor of the present invention has (1) good diarrhea performance because of anaerobic microorganisms. The long generation period, the high oxygen content of the reactor is the basis for ensuring high efficiency of anaerobic reactor treatment. (2) Good 10 200808665 ~ Ageing state> Partially transferred whole-age fluid energy can increase impurities & touch > Improve mass transfer fiber, keep microbes fully active; and the overall push flow regime 雠 system certain matrix The concentration gradient fully decomposes the enamel in the sewage, improves the quality of the effluent, and has good microbial phase earning characteristics. Under different environmental conditions, each reaction unit is conditioned to adapt to the dominant microbial flora in the environment, so that the system is different. Microbial flora can maximize its surface properties in its adapted environment. (4) Reaction chamber An expanded bed or a fluidized bed can be formed, and the biological carrier is filled in a high-load reaction chamber, and the microorganisms are earned in the porous carrier table. By using the high internal circulation generated by high organic load, the state of the expanded bed is formed in the 7-layer reaction zone in the reaction chamber, ensuring the largest unit volume of the reaction chamber and the high maintenance of the biological position. (5) A set of anaerobic dramas that are constructed to be elastically touched. [Embodiment 1 Hereinafter, a detailed description will be made in conjunction with the accompanying drawings to better understand the objects and advantages of the present invention. Schematic diagram of the multiphase internal circulation reactor of the present invention. FIG. 2 is a schematic view of the multiphase internal circulation reaction hall of the present invention. FIG. 3 is a schematic diagram of the multiphase internal circulation reactor of the present invention. Schematic diagram of an embodiment of the device. The multiphase internal circulation anaerobic reactor is divided into three internal circulation anaerobic reaction chambers 4, 5, and 6 by two partition plates 16, and the structure of the three internal circulation anaerobic reaction chambers is one Internal circulation anaerobic reaction chamber of the reaction zone (the following chambers are provided in each reaction chamber, with a three-phase separator 10, Θ, a sub-class of anti-driver of T® and an S-stage reaction zone above, in two The three-phase separator 10, the inclined surface of θ, _ into two precipitation zones, the gas collection pipe is connected to the three-phase separator 9 of the first-stage reaction zone, and the gas riser 14 is connected to the three-phase separation of the first-stage reaction zone. The J-stage reaction in 1 ©, the gas lifter 14 has a stripper 15 at the lower end, the reaction chamber top_gas-liquid separator 11, and a return pipe 13 at its lower portion is passed between the deflector 17 and the partition plate 16. In the inflow zone, on the side wall of the reaction chamber and the two three-phase separators 9, 1 are provided, and gas seals 7, 8 are provided, and at the inlet 1 of each reaction chamber, a fiberboard 17 is passed through the bottom of the reaction chamber. The flow plate 17 - side, the gas seals 7, 8 are provided inside the baffle 17. The fine-grained biological carrier is filled in the first-stage reaction zone separated by the three-phase separator 10 to form an expanded bed. The structure of the device 15 can be seen in Fig. 2. Each of the risers 15 is connected to the lower portion of the air lift pipe 14. The stripper 15 is composed of an outer gas collecting cylinder 21 and an inner air cylinder 22. The lower edges of the gas collecting cylinders 21 are distributed. The curve of the fan shape ensures the uniform air distribution. The air cylinder 22 is provided with a contraction throat, and the circumference of the circumference is evenly distributed with a diameter and a suitable number of orifices 24, each of which has a corresponding guide. The flow channel 11 200808665 2&, the guide groove 25 has a scalloped lower edge corresponding to the orifice 24 from the bottom, along the shrinking throat 23 up to the orifice 24, and its function is to form a hydraulic diversion function. The gas is first collected by the external gas collecting cylinder 21, and then injected into the stripper 15 through the orifice 24 of the inner gas cylinder 22. The lower edge of the gas collecting cylinder 21 uniformly distributes the fan-shaped notch to ensure that the biogas can enter the gas collecting cylinder 21 uniformly. The upper circumference of the shrinking throat 23 of the air cylinder 22 is distributed with an appropriate diameter and a number of orifices 24, each of which has a corresponding diversion groove 25, and the diversion groove 25 has a corresponding orifice 24 from the bottom. The fan-shaped notch runs along the shrinking throat 23 - until the orifice 24 licks its In order to form a hydraulic diversion, when the biogas is injected into the gas stripping 15 from the uniformly distributed orifice 24, a Venturi effect is generated to form a jet, and the fine granules of the sewage and the anaerobic biological carrier are sucked into the stripper. 15. At the shrinking throat 23, due to the increase of the flow velocity, a large shear force is formed to cut the gas into tiny bubbles, resulting in a more efficient gas-cutting and mixing effect, increasing the circulation of the inner circulation and the annoyance. The mass transfer efficiency of the fine particles of the oxygen biocarriers. The three reaction chambers are connected in series hydraulically, that is, the outlet of the previous reaction chamber is connected to the inlet of a reaction chamber to form a push-flow fluid state. The gas-liquid separator of the chamber is connected to the same biogas discharge pipe 3, and can also be separately discharged and collected. In each reaction chamber, sewage flows from the inlet raft 1 along the deflector to the bottom of the reaction chamber 4, from the bottom to the top chamber, and then from the effluent 堰 2 to the second chamber 5, and then to the third reaction chamber. 6. Finally, the treated water is discharged from the effluent. In the first-stage reaction zone in the lower part of the reaction chamber, the sewage and the fine granules of the anaerobic biological carrier are uniformly mixed to carry out a biodegradation reaction to generate a large amount of biogas, and the three-phase separator separates a large amount of biogas into the stripper 15 The mud-water mixture together with the lower layer of the first reaction chamber is lifted to the gas-liquid separator 11 at the top of the reaction chamber, and the gas is drained from the biogas discharge pipe 3, wherein the anaerobic biological carrier and the sewage are refluxed via the return pipe 13 to the reaction chamber. The flow zone is mixed with the influent liquid, and the mixed liquid enters the bottom of the first-stage reaction zone along the deflector 17, completing the internal circulation of the mixed liquid. The function of the stripper 15 has been described above. With the stripper 15, the mud-water mixture in the first-stage reaction zone can be more enhanced, the hydraulic circulation and the mixed flow state can be enhanced, and the sewage and anaerobic biological sludge can be improved. Mass transfer efficiency. The reaction chamber can selectively fill a biological carrier having a particle size of 0.2 to 1. 〇 mm, and the microorganism forms a compact biofilm structure on the surface of the porous carrier. By using a high internal circulation amount generated by a high organic load, an expanded bed or a fluidized bed is formed in the lower reaction zone of the reaction chamber, thus ensuring the maximum biomass per unit volume in the reaction chamber and maintaining high biological activity. After being treated by the first-stage reaction zone, the sewage flows to the upper Π-stage reaction zone for further biochemical degradation reaction, and the generated biogas is collected by the three-phase separator 9 and sent to the gas and liquid separator 11 through the gas riser 12; The mud-water mixture in the reaction zone is subjected to solid-liquid separation in the sedimentation zone, and the fine granules of the settled anaerobic biological carrier are returned to the Π-stage reaction zone; the effluent from the top of the first reactor 4 is along the second reactor Board enters the first
12 200808665 〜 二反應器5的I級反應區。 在第二反應室5中，污水的流動及生化降解過程和第一反應室4相同。依此 類推至第三反應器6。 ， 由多個具有內循環厭氧反應室構成一個多相、高有機負荷的厭氧生物處理系 統。在整個反應系統中，反應室之間的水力流態爲推流流g，各反應室之間維持 一定的底物濃度梯度，使每個反應室中可以培養出與流至該反應室的基質組成和 環繼隊(酸鹼度、氫分壓'代謝中間産％^ )相適應的優^^^獅樓，形成 ， 多相的厭氧處理系統。而在單_反應室中，將厭氧生化反應産生的沼氣利用氣 提原理，斷反應室下層的顆粒污泥和底物，造成反應室內部的水力観，形成 完全混流的水力流態；內循環加強了厭氧生物載體的細小粒體和底物的混合接 觸，大大的提高有機容積負荷，而由於具有高有機負荷，相對有高産氣量的沼氣 醫 産生，形成高強度的循環_量，如此造成極低死區百分率的厭氧反應室，達到高 處理效率 > 良好穩定的出7]C7勝改善水質，至會使厭雛理的出林質麵 二總準。 雖然本實施例中的多相內循環厭氧反應器爲三個反應室，但並不限定多相內 循環厭氧麵器的反應颜能爲三個。 本發明多相內循環厭氧反應器具備如下特性：⑴良好的污泥繼注能，因爲 厭氧微生物的世代期長，反應器保持高漲量是保麵氧反應器處理高效率的基 礎。(2)良好的水力流態，局部的完全混合流態使生物污泥能夠和進水基質充分的 混合接觸，提高傳質燃g，保持齡物具備充分的活性；而整體的推流流態保證 系統一定的基質濃度梯度，充册解污水中的基質，提高出林質。⑶良好的微 籲 生物相分離特性，在不同的環境條件下，各反應單元馴養麵於所處《105優勢 微生物菌群，使系統內的不同微生物菌群能在其適應的環境中發揮最大的活性。 (4)反應室可形成膨脹床或流化床，在高負荷的反應室塡充生讎體，歡物在多 孔載體表面上生^緊密的生物騰纖。利用簡機負荷産高內循環量，在反 應室的下層反應區形成膨脹床或雜床的狀態，保證反應室內最大的單位體積生 物麵維持高的生物酿。(5俱有模組化架搆的厭氧處理器5方便娜性化的組 合 13 200808665 【圖式簡單說明】 【主要元件符號說明】 1·進水堰 2·出水堰 3,沼氣排出管 4·第一麵室 5.第二反應室 6·第三反應室 7-氣封 8,氣封 认三相分離器 10·三相分離器 11·氣液分離器 12♦観管 13·廻流管 14. 氣 15. 氣提器 16. 分隔板 1:7 ·導流板 说纖板 说反應謙體 21·外部集氣筒 22·布氣筒 23·收麵管 24♦孔口 2匕導流溝 十、申請專利範菌： 1 ·多相肉循環厭氧反應器，包括帶L、辽画級反應區租相應氣奸管(14)、集氣 篑12).、回纖13)、氣液分離器(11)、三相分離器(9、10)、氣封(8、9)的厭 氧內循環反應室，其特徵是在反應器槽體(19).中設置至少二個用分隔艇瑪 分隔、並串聯連接的叛述內循環厭氧反應室(4、5、6)，叛述的內循環厭氧 :出^ 2 ·根據审請專利範圍第1項之處理設備.，是在內循環厭氧反應室(4、5、6)， 設置從進水堰⑴沿反應室室壁延伸到反應室底部的導流板(17)，在導流板 (17)—側的氣封(8、9)設置在導流板(17)上，所述的回流管(13)通至導流嫉1符 和分隔板(16)之間，所述氣升管(14)的下部設置氣提器(15) 〇 3 ·根據申請專利範圍第2項之處理設備，其特徵是在所述三相分離器(10)隔岀 的丄級反應區中充塡細小粒徑的生物載體，形成膨脹床或流化床的狀態。 4-根據申請專利範圍第3項之處理設備，其特徵是所述的氣提器(15)是在所述 氣升管(14)的下部連接氣提器(15)，所述氣提器(15)是由外部集氣筒(21靡內 部布氣筒(22)所構成。集氣筒(21)下緣均勻分佈扇形缺口狀的曲線，所述布 1412 200808665 ~ II reactor 5 grade I reaction zone. In the second reaction chamber 5, the flow of the sewage and the biochemical degradation process are the same as those of the first reaction chamber 4. This is analogous to the third reactor 6. An anaerobic biological treatment system consisting of a plurality of internal circulation anaerobic reaction chambers forming a multiphase, high organic load. In the whole reaction system, the hydraulic flow state between the reaction chambers is the push flow g, and a certain substrate concentration gradient is maintained between the reaction chambers, so that the matrix flowing to the reaction chamber can be cultured in each reaction chamber. The composition and the ring team (pH, hydrogen partial pressure 'metabolism intermediate production%^) are compatible with the excellent ^^^ lion building, forming a multi-phase anaerobic treatment system. In the single-reaction chamber, the biogas generated by the anaerobic biochemical reaction is subjected to the principle of stripping, and the granular sludge and the substrate in the lower layer of the reaction chamber are broken, thereby causing hydraulic enthalpy inside the reaction chamber to form a completely mixed hydraulic flow state; The circulation enhances the mixed contact of the fine granules and the substrate of the anaerobic biological carrier, greatly increasing the organic volumetric load, and due to the high organic load, relatively high gas production by the biogas is generated, forming a high-intensity cycle amount, This results in an extremely low dead zone percentage of the anaerobic reaction chamber, achieving high processing efficiency > good stability 7] C7 wins to improve water quality, so that the outcrop will be the best. Although the multiphase internal circulation anaerobic reactor in this embodiment is three reaction chambers, the reaction color energy of the multiphase internal circulation anaerobic device is not limited to three. The multiphase internal circulation anaerobic reactor of the present invention has the following characteristics: (1) good sludge subsequent injection energy, because the generation period of the anaerobic microorganisms is long, and the reactor maintains a high increase amount, which is the basis for the high efficiency of the surface oxygen reactor treatment. (2) Good hydraulic flow state, the partial complete mixed flow state enables the biological sludge to be in sufficient mixed contact with the influent substrate, improve the mass transfer fuel, maintain the full activity of the aged material, and the overall push flow state Ensure a certain matrix concentration gradient of the system, fill the matrix in the sewage, and improve the forest quality. (3) Good micro-phase bioseparation characteristics. Under different environmental conditions, each reaction unit is domesticated in the 105 dominant microbial flora, so that different microbial flora in the system can maximize its adaptation environment. active. (4) The reaction chamber can form an expanded bed or a fluidized bed, and the carcass is filled in the high-load reaction chamber, and the fungus is produced on the surface of the porous carrier. The high internal circulation amount is generated by the simple load, and an expanded bed or a mixed bed is formed in the lower reaction zone of the reaction chamber to ensure that the maximum biomass per unit volume of the living chamber in the reaction chamber is maintained high. (5 anaerobic processor with modular structure 5 convenient combination of naturalization 13 200808665 [Simple description of the diagram] [Explanation of main components] 1·Inlet 堰2·Water 堰3, Biogas venting tube 4 · First chamber 5. Second reaction chamber 6 · Third reaction chamber 7 - Gas seal 8, gas seal recognize three-phase separator 10 · Three-phase separator 11 · Gas-liquid separator 12 ♦ Tube 13 · Turbulence Tube 14. Gas 15. Stripper 16. Separator 1:7 · Deflector said fiber board said reaction mode body 21 · External gas cylinder 22 · Air cylinder 23 · Face tube 24 ♦ orifice 2 匕 diversion Ditch ten, apply for patent bacteria: 1 · Multi-phase meat circulation anaerobic reactor, including L, Liao painting-level reaction zone rent corresponding traitor tube (14), gas gathering 篑 12)., fiber return 13), gas An anaerobic internal circulation reaction chamber of a liquid separator (11), a three-phase separator (9, 10), and a gas seal (8, 9), characterized in that at least two are provided in the reactor tank (19). The rebellious internal circulation anaerobic reaction chamber (4, 5, 6) separated by a seperate boat and connected in series, the rebellious internal circulation anaerobic: out ^ 2 · according to the processing equipment of the scope of the patent application. Is the internal circulation anaerobic reaction chamber (4, 5, 6) a baffle (17) extending from the inlet raft (1) along the wall of the reaction chamber to the bottom of the reaction chamber, and a gas seal (8, 9) on the side of the baffle (17) is disposed at the deflector (17) Above, the return pipe (13) is connected between the guide 嫉1 and the partition plate (16), and the lower portion of the gas riser (14) is provided with a stripper (15) 〇3. The processing apparatus of the second aspect, characterized in that the biological reaction of the fine particle size is filled in the tertiary reaction zone of the three-phase separator (10) to form an expanded bed or a fluidized bed. 4-processing apparatus according to item 3 of the patent application, characterized in that the stripper (15) is connected to a stripper (15) at a lower portion of the gas riser (14), the stripper (15) is composed of an external gas collecting cylinder (21 靡 internal air cylinder (22). The lower edge of the gas collecting cylinder (21) is uniformly distributed with a fan-shaped notch shape, and the cloth 14