TW201221484A - Method and apparatus for sludge treatment and use thereof in sewage biotreatment - Google Patents

Method and apparatus for sludge treatment and use thereof in sewage biotreatment Download PDF

Info

Publication number
TW201221484A
TW201221484A TW099140871A TW99140871A TW201221484A TW 201221484 A TW201221484 A TW 201221484A TW 099140871 A TW099140871 A TW 099140871A TW 99140871 A TW99140871 A TW 99140871A TW 201221484 A TW201221484 A TW 201221484A
Authority
TW
Taiwan
Prior art keywords
sludge
sewage
treatment
mixed liquid
mixture
Prior art date
Application number
TW099140871A
Other languages
Chinese (zh)
Other versions
TWI445673B (en
Inventor
jin-min Li
lian-kui Zhou
da-yong Li
Original Assignee
jin-min Li
lian-kui Zhou
da-yong Li
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by jin-min Li, lian-kui Zhou, da-yong Li filed Critical jin-min Li
Priority to TW099140871A priority Critical patent/TWI445673B/en
Publication of TW201221484A publication Critical patent/TW201221484A/en
Application granted granted Critical
Publication of TWI445673B publication Critical patent/TWI445673B/en

Links

Classifications

    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Landscapes

  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Activated Sludge Processes (AREA)
  • Treatment Of Sludge (AREA)

Abstract

The present invention provides a method for sludge treatment, comprising the following steps: (1) mixing a sludge feed from a sewage biotreatment process with a first mixed liquor to obtain a second mixed liquor; (2) subjecting the second mixed liquor to an oxygen-supplying process to obtain a third mixed liquor; (3) subjecting the third mixed liquor to an anoxic process to obtain a fourth mixed liquor; (4) separating the fourth mixed liquor to obtain a supernatant liquid and a first concentrated mixed liquor; (5) discharging the supernatant liquid, and returning at least a part of the first concentrated mixed liquor as the first mixed liquor to the step (1), wherein the amount of sludge of the first concentrated mixed liquor that does not return to the step (1) is less than the amount of sludge of the sludge feed. The present invention further relates to the use of the method for sludge treatment in sewage treatment. The method for sludge treatment can achieve a long term stable run without sludge discharge.

Description

201221484 六、發明說明： 【發明所屬之技術領域】 [0001] 本發明是有關於一種污泥處理方法和裝置及其在污水生 物處理中的應用，特別是有關於一種污泥減量化處理方 法及其裝置和一種包括所述污泥減量化處理方法的污泥 減量化污水生物處理方法及其裝置。 【先前技林ί】 [0002] 隨著水污染的日益嚴重，對各種污水進行經濟有效的處 理勢在必行。目前全球範圍内已有數以萬計的汙水處理 廠正在運行，且隨著環境意識與環保要求的提高必將有 更多的污水廠行將建設。 [0003] 污水生物處理以高效低耗的突出優點被廣泛用於汙水處 理，以活性污泥和生物膜為代表的污水生物處理工藝在 水污染治理方面已取得了巨大成功。然而，現有的污水 生物處理工藝並不完善。 [0004] 在實際運行過程中，多數污水生物處理廠面臨以下問題 ··( 1 )進水水量不足，主要由超前規劃和污水排放系統 故障導致，影響汙水處理裝置的運行；（2)進水水質不 穩定，主要原因是工業廢水排入管網以及節假日和季節 變化等導致的生活習慣改變等，可造成衝擊負荷影響汙 水處理效果；（3)碳源不足，這是各汙水處理廠所共同 面臨的問題，主要由現代生活習慣所致，可導致生物的 營養物失衡影響氮和磷的去除效果。在面對這些問題時 ，傳統活性污泥法日益暴露出以下缺陷：（1 )曝氣池中 生物濃度低；（2 )而ί水質、水量衝擊負荷能力差，運行 099140871 表單編號Α0101 第4頁/共79頁 0993446280-0 201221484 不夠穩定；（3)易產生污泥膨脹；（4)污泥產量大； (5)基建和運行費用高，占地面積大等。 [0005] Ο [0006] Ο [0007] 特別地，現有污水生物處理工藝最引人注目的問題就是 大量剩餘污泥的產生。污泥處理的費用異常之高，大約 占到汙水處理廠建設和運行總費用的5〇%〜6〇%左右。剩 餘/亏泥㈤要進行必要的處置因而增加了汙水處理的運行 費用，同時也限制了污泥處理方法的選擇。常見的污泥 減量方法有消化法（包括厭氧消化和好氧消化）、污泥 熱處理法例如濕式氧化法、污泥濃縮法例如重力濃縮法 和軋浮濃縮法、污泥脫水法例如機械脫水和化學混凝法 、汚泥幹化法例如自然幹化法和烘乾法。然而，這些污 泥減量方法並未完全解決污泥排放的問題。 中國專利申請公開CN101481191A公開了一種污泥回流消 化減量的汙水處理方法，其中將剩餘污泥返回厭氧沉澱 池中在厭氧沉澱池下部的沉澱污泥區長期♦累以便將污 泥消化減量，污水進料通過厭氧沉澱池後進行汙水處理 得到淨化水和剰餘污泥，未消化的污泥需要定期清掏。 美國專利申請公開US2002/0030003A1公開了一種活性 污泥汙水處理系統和方法，其中在接觸罐令用污泥處理 污水，然後在固液分離器中分離污泥和水，分離的污泥 與部分污水在消化罐中混合並曝氣以使污泥消化減量， 經曝氣的泥水混合液部分返回接觸罐，部分排出。 再者，現有污水生物處理工藝中對磷的去除效果普遍不 佳。磷是造成水體富營養化的主要限制因數，並且是人 099140871 表單蝙號A0101 第5頁/共79頁 0993446280-0 [0008] 201221484 類可持續發展的重要元素，因此目前對水體中磷含量的 控制日益嚴格，並且逐漸從單一“去除”轉向“回收” 。目前的脫磷工藝大都基於聚磷菌在厭氧釋磷後在好氧 狀態下超量攝磷現象，因此必須排出一定量的污泥來最 終除磷，這對污泥減量也構成了巨大挑戰。 [0009] 綜上所述，仍然需要發展新的污泥處理方法和污水生物 處理方法以解決上述問題，特別是污泥減量的問題。 【發明内容】 [0010] 在一個方面，本發明提供一種污泥處理方法，包括以下 步驟： [0011] ( 1 )將來自污水生物處理過程的污泥進料與第一混合液 混合得到第二混合液； [0012] (2)將第二混合液進行給氧處理得到第三混合液； [0013] ( 3 )將第三混合液進行缺氧處理得到第四混合液； [0014] (4)將第四混合液分離得到上清液和第一濃縮混合液； [0015] (5)將上清液排出，並且將至少部分第一濃縮混合液返 回步驟（1)用作第一混合液，其中未返回步驟（1)的 第一濃縮混合液的污泥量小於污泥進料的污泥量。 [0016] 根據本發明的污泥處理方法的一些實施方案，在步驟（5 )中，將任意合適的比例，例如至少6 0 %、優選至少6 5 %、更優選至少70%、更優選至少75%、更優選至少80 %、更優選至少85%、更優選至少90%、更優選至少93 %、更優選至少95%、更優選至少98%、最優選基本上 099140871 表單編號A0101 第6頁/共79頁 0993446280-0 201221484 100%的第-濃縮混合液返回步驟⑴用作第一混合液 ，並且任祕將未返酵驟⑴㈣—濃縮混合液排出 。換句話說，在步驟⑸+，未返回步驟⑴的第-濃縮混合液的污泥量與污泥進料的污泥量的比例可以為 任意合適的值，例如選自小於約40%，小於約35%、小於 約30%、小於約25%，小於約2Q%、小於約15%，小於約 13%、小於約1〇%、小於約8% 小於約5%、小於約3%，小 Ο [0017] 於約U和賴。根據本發明的污泥處理方法的一些實施方案，在步驟⑸中將基本上全部第—濃縮混合液返回 步驟（1)用作第一混合液。 根據本發料污泥處理方㈣—㈣施方案，在步驟 )中’將有機營養物（優選污水進料)、污泥進料和第 混口液说合得到第二混合液。也就是說，步驟⑴還 包括將污水進料引入第—混合液。 [0018] 〇 根據本發明的污泥處理方法的一些實施方案，步驟（1) 中污泥進料與污水進料的流量比為1:0, 01〜1:100，優 選1:0·1〜1:10，更優選為1:0 5〜1:5。具體而言污 泥進料與污水進料的流量比可以為任何合適的值，例如 選自 L10G 〜1:5G、1:5G 〜1:2G、1:2G 〜1:1〇、1:1〇 〜1:5、1:5〜1:2、1:2〜1:1.5、1:1· 5〜1:1、1:1〜 1.0.8、1.0.8〜1:〇.5、ι:〇·5〜1:〇.2、1:〇.2〜 卜〇. 1、10. 1 〜1:0. 05、1:0. 05〜1:〇 〇2和1:〇 〇2〜1:0.01 。 [0019] 099140871 根據本發明的污泥處理方法的一些實施方案，步驟（2)的給氧處理時間為〇. 1〜4小時，優選〇. 5〜2小時，更優 表單編號A0101 第7頁/共79頁 0993446280-0 201221484 [0020] 選0. 5〜1. 5小時。 根據本發明的污泥處理方法 的缺氧處理時間為0. 8〜6,j 〜3小時。 的一些實知方案，步驟（3) 、時，優選1〜4小時，更優選1 [0021] 根據本發明的污泥處理方法 處理時間與缺氧處理時間的 〜1:3，更優選ι:1. 5〜1:2 的-些實施方案’其中給氧 比為1:0·5〜1:6，優選1.1 ，最優選1 :2。 [0022] [0023] 根據本發明的污泥處理方法的—些實施方案步驟⑴ 的給氧處私錢或連續魏时式進行。 根據本發日㈣污泥處理枝的―些實施方案，在步驟（: )中’第三混合液的溶解氧濃度為〇. 1〜4rag/L，優選 〜3mg/L，更優選2〜3mg/L。 [0024] [0025] [0026] 根據本發日㈣污泥處理方法m财案，步驟（3) 和步驟（4)以沉澱方式進行。 根據本發明的污錢理方法L實施方案，在步驟（1 )中，第二混合液的污泥濃度為3000〜30000mg/L，優 選3000〜2_〇mg/L，更優選4刪〜15〇〇()mg/L。 根據本發明的污泥處理方法的一些實施方案，其中兼性 微生物為第一、第二、第三和第四混合液的污泥中的優勢群類。 [0027] 根據本發明的污泥處理方法的一些實施方案，還包括回 收步驟（2 )和/或（3 )中產生的氣態含磷化合物的回收 步驟。 099140871 表單編號A0101 第8頁/共79頁 0993446280-0 201221484 [0028] 在另一方面，本發明還提供一種污水生物處理方法，包 括： [0029] (1 )將來自污水生物處理過程的污泥進料和第一混合液 混合得到第二混合液； [0030] (2)將第二混合液進行給氧處理得到第三混合液； [0031] (3)將第三混合液進行缺氧處理得到第四混合液； [0032] (4)將第四混合液分離得到上清液和第一濃縮混合液； Ο _ (5)將上清液排出，並且將至少部分第一濃縮混合液返 回步驟（1 )用作第一混合液，其中未返回步驟（1 )的 第一濃縮混合液的污泥量小於污泥進料的污泥量； [0034] (6)將至少部分步驟（5)的上清液和任選的部分污水 進料進行污水生物處理得到第二濃縮混合液和淨化出水 9 [0035] 〇 (7)將淨化出水排出，並且任選地將至少部分步驟（6 )的第二濃縮混合液返回步驟（1)用作污泥進料； [0036] 其中將污水進料引入步驟（1)與污泥進料和第一混合液 混合得到第二混合液和/或在步驟（6)中與所述至少部 分步驟（5)的上清液一起進行污水生物處理，優選將至 少部分污水進料在步驟（1)中與污泥進料和第一混合液 混合得到第二混合液，更優選將全部污水進料在步驟（1 )中與污泥進料和第一混合液混合得到第二混合液。 [0037] 根據本發明的污水生物處理方法的一些實施方案，在步 驟（5)中，將至少60%、優選至少65%、更優選至少70 099140871 表單編號A0101 第9頁/共79頁 0993446280-0 201221484 %、更優選至少75%、更優選至少80%、更優選至少85 %、更優選至少90%、更優選至少93%、更優選至少95 %、更優選至少98%、最優選基本上100%的第一濃縮混 合液返回步驟（1)用作第一混合液，並且任選地將未返 回步驟（1)的第一濃縮混合液排出。 [0038] [0039] [0040] [0041] 根據本發明的污水生物處理方法的一些實施方案，在步 驟（6)中，將至少20% '優選至少35% '更優選至少5〇 %、更優選至少65%、更優選至少80%、更優選至少85 %、更優選至少90%、更優選至少93%、更優選至少95 %、更優選至少98%、最優選基本上100%的步驟（5) 的上清液進行污水生物處理。 根據本發明的污水生物處理方法的一些實施方案，在步 驟（1)中引入至少20 %、優選至少35%、更優選至少5〇 %、更優選至少65%、更優選至少80%、更優選至少85 %、更優選至少90%、更優選至少93%、更優選至少95 %、更優選至少98%、最優選基本上100%的污水進料， 並且在步驟（6)中引入剩餘部分的污水進料。在一些優 選的實施方案中，在步驟（1)中引入全部的污水進料， 並且在步驟（6)中不引入污水進料。 根據本發明的污水生物處理方法的一些實施方案，步驟 (2) 的給氧處理時間為〇·丨〜4小時，優選〇 5〜2小時 ’更優選0.5〜1.5小時。 根據本發明的污水生物處理方法的—些實施方案，步驟 (3) 的缺氧處理時間為〇 8〜6小時，優選丨〜4小時更 099140871 表單編號A0101 第10頁/共79頁 0993446280-0 201221484 優選1〜3小時。 [0042] 根據本發日㈣污水生物處理方法的—些實施方案，給氧 處理時間與缺氧處理時間的比為1:0.5〜1:6 ,優選1:1 H更優選1:1. 5〜1:2,最優選1:2。 ^ _本發0㈣污水生減财法的—些㈣方案，步驟 )的、'η氧處理以間歇曝氣或連續曝氣的方式進行。201221484 VI. Description of the Invention: [Technical Field] [0001] The present invention relates to a sludge treatment method and apparatus and application thereof in sewage biological treatment, in particular to a sludge reduction treatment method and The apparatus and a sludge degrading sewage biological treatment method and apparatus comprising the sludge reduction treatment method. [Previous Tech Lin] [0002] With the increasing pollution of water, it is imperative to deal with all kinds of sewage economically and effectively. At present, tens of thousands of sewage treatment plants are in operation worldwide, and with the environmental awareness and environmental protection requirements, more sewage plants will be built. [0003] Sewage biological treatment is widely used in sewage treatment with its outstanding advantages of high efficiency and low consumption. The sewage biological treatment process represented by activated sludge and biofilm has achieved great success in water pollution control. However, the existing sewage biological treatment process is not perfect. [0004] In the actual operation process, most sewage biological treatment plants face the following problems: (1) Insufficient water inflow, mainly caused by advance planning and failure of sewage discharge system, affecting the operation of sewage treatment equipment; (2) The water quality is unstable, mainly due to the change of living habits caused by the discharge of industrial wastewater into the pipe network and holidays and seasonal changes, which may cause the impact load to affect the sewage treatment effect; (3) the carbon source is insufficient, which is the sewage treatment. The problems faced by the factory are mainly caused by modern living habits, which can lead to the imbalance of nutrients of the organisms affecting the removal of nitrogen and phosphorus. In the face of these problems, the traditional activated sludge process is increasingly exposed to the following defects: (1) low biological concentration in the aeration tank; (2) and ί water quality, water impact load capacity is poor, run 099140871 Form No. Α 0101 Page 4 / Total 79 pages 0993446280-0 201221484 Not stable enough; (3) easy to produce sludge expansion; (4) large sludge production; (5) high infrastructure and operating costs, large area. [0005] [0007] In particular, the most striking problem with the existing sewage biological treatment process is the production of a large amount of excess sludge. The cost of sludge treatment is abnormally high, accounting for about 5% to 6% of the total cost of construction and operation of the sewage treatment plant. Residual/depleted sludge (5) The necessary disposal is required to increase the operating cost of sewage treatment and also limit the choice of sludge treatment methods. Common sludge reduction methods include digestion (including anaerobic digestion and aerobic digestion), sludge heat treatment such as wet oxidation, sludge concentration methods such as gravity concentration and rolling flotation, sludge dewatering such as machinery. Dehydration and chemical coagulation methods, sludge drying methods such as natural drying and drying methods. However, these sludge reduction methods have not completely solved the problem of sludge discharge. Chinese Patent Application Publication No. CN101481191A discloses a sewage treatment method for sludge reflux digestion and reduction, wherein the excess sludge is returned to the anaerobic sedimentation tank in the sedimentation sludge zone at the lower part of the anaerobic sedimentation tank for a long period of time to reduce the sludge digestion. The sewage feed is treated with sewage through the anaerobic sedimentation tank to obtain purified water and residual sludge, and the undigested sludge needs to be cleaned regularly. U.S. Patent Application Publication No. US 2002/0030003 A1 discloses an activated sludge sewage treatment system and method in which sewage is treated with sludge in contact with a tank, and then sludge and water are separated in a solid-liquid separator, and the separated sludge and parts are separated. The sewage is mixed and aerated in the digester to reduce the sludge digestion, and the aerated muddy water mixture is partially returned to the contact tank and partially discharged. Furthermore, the removal of phosphorus in the existing sewage biological treatment process is generally poor. Phosphorus is the main limiting factor for eutrophication of water bodies, and it is human 099140871 Form bat number A0101 Page 5 / Total 79 pages 0993446280-0 [0008] 201221484 An important element of sustainable development, so the current phosphorus content in water Control is becoming more stringent and gradually shifts from a single “removal” to “recycling”. Most of the current dephosphorization processes are based on the phenomenon of excessive phosphorus uptake by a polyphosphate bacteria in an aerobic state after anaerobic phosphorus release. Therefore, a certain amount of sludge must be discharged to finally remove phosphorus, which also poses a huge challenge to sludge reduction. . [0009] In summary, there is still a need to develop new sludge treatment methods and sewage biological treatment methods to solve the above problems, particularly the problem of sludge reduction. SUMMARY OF THE INVENTION [0010] In one aspect, the present invention provides a sludge treatment method comprising the following steps: [0011] (1) mixing a sludge feed from a sewage biological treatment process with a first mixed liquid to obtain a second [0012] (2) the second mixed liquid is subjected to oxygen treatment to obtain a third mixed liquid; [0013] (3) the third mixed liquid is subjected to anoxic treatment to obtain a fourth mixed liquid; [0014] The fourth mixed liquid is separated to obtain a supernatant liquid and a first concentrated mixed liquid; [0015] (5) discharging the supernatant liquid, and returning at least a portion of the first concentrated mixed liquid to the step (1) as the first mixed liquid The amount of sludge of the first concentrated mixture which has not been returned to the step (1) is smaller than the amount of sludge of the sludge feed. [0016] According to some embodiments of the sludge treatment method of the present invention, in step (5), any suitable ratio, for example at least 60%, preferably at least 650%, more preferably at least 70%, more preferably at least 75%, more preferably at least 80%, more preferably at least 85%, more preferably at least 90%, more preferably at least 93%, more preferably at least 95%, more preferably at least 98%, most preferably substantially 099140871 Form No. A0101 Page 6 / Total 79 pages 0993446280-0 201221484 100% of the first-concentrated mixture returning step (1) is used as the first mixed liquid, and the secret mixture (1) (4) - concentrated mixture is discharged. In other words, in the step (5)+, the ratio of the amount of the sludge of the first concentrated liquid mixture which has not returned to the step (1) to the sludge amount of the sludge feed may be any suitable value, for example, selected from less than about 40%, less than About 35%, less than about 30%, less than about 25%, less than about 2Q%, less than about 15%, less than about 13%, less than about 1%, less than about 8%, less than about 5%, less than about 3%, small Ο [0017] About U and Lai. According to some embodiments of the sludge treatment method of the present invention, substantially all of the first concentrated liquid mixture is returned to the step (1) as the first mixed liquid in the step (5). According to the present invention, the sludge treatment side (4)-(iv), in the step of 'receiving organic nutrient (preferably sewage feed), sludge feed and the first mixed liquid to obtain a second mixed liquid. That is, step (1) also includes introducing the sewage feed into the first mixture. [0018] According to some embodiments of the sludge treatment method of the present invention, the flow ratio of the sludge feed to the sewage feed in step (1) is 1:0, 01 to 1:100, preferably 1:0. ~1:10, more preferably 1:0 5~1:5. Specifically, the flow ratio of the sludge feed to the sewage feed may be any suitable value, for example, selected from the group consisting of L10G to 1:5G, 1:5G to 1:2G, 1:2G to 1:1, 1:1. 〇~1:5, 1:5~1:2, 1:2~1:1.5, 1:1·5~1:1, 1:1~10.8, 1.0.8~1:〇.5, ι:〇·5~1:〇.2, 1: 〇.2~ 〇. 1, 10.1 ～1:0. 05, 1:0. 05~1: 〇〇2 and 1: 〇〇2 ~1:0.01. [0019] 099140871 According to some embodiments of the sludge treatment method of the present invention, the oxygen treatment time of the step (2) is 〇. 1~4 hours, preferably 〇. 5~2 hours, more excellent form number A0101 page 7 5〜1. 5小时。 The total of 0. 5~1. 5 hours. 〜3小时。 The anoxic treatment time of the sludge treatment method according to the present invention is 0. 8~6, j ~ 3 hours. Some known schemes, step (3), time, preferably 1 to 4 hours, more preferably 1 [0021] The sludge treatment method according to the present invention has a treatment time of ~1:3, and more preferably ι: 1. Some embodiments of 5 to 1:2 wherein the oxygen ratio is from 1:0 to 5:1, preferably 1.1, most preferably 1:2. [0023] According to the sludge treatment method of the present invention, the oxygen supply at the step (1) of the embodiment is carried out in a private money or continuous Wei time. According to some embodiments of the sludge treatment branch of the present day (4), in the step (:), the dissolved oxygen concentration of the third mixed liquid is 11 to 4 rag/L, preferably 〜3 mg/L, more preferably 2 to 3 mg. /L. [0025] [0026] According to the present invention (4) sludge treatment method m, step (3) and step (4) are carried out in a precipitation manner. According to the embodiment of the present invention, in the step (1), the sludge concentration of the second mixed liquid is 3000 to 30000 mg/L, preferably 3000 to 2_〇mg/L, more preferably 4 to 15 〇〇()mg/L. Some embodiments of the sludge treatment method according to the present invention, wherein the facultative microorganism is a dominant group in the sludge of the first, second, third and fourth mixtures. Some embodiments of the sludge treatment method according to the present invention further comprise the step of recovering the gaseous phosphorus-containing compound produced in the steps (2) and/or (3). 099140871 Form No. A0101 Page 8 / Total 79 Page 0993446280-0 201221484 [0028] In another aspect, the present invention also provides a sewage biological treatment method comprising: [0029] (1) sludge from a biological treatment process of sewage The feed and the first mixed liquid are mixed to obtain a second mixed liquid; [2] (2) the second mixed liquid is subjected to oxygen treatment to obtain a third mixed liquid; [0031] (3) the third mixed liquid is subjected to anoxic treatment Obtaining a fourth mixed liquid; [4] (4) separating the fourth mixed liquid to obtain a supernatant liquid and a first concentrated mixed liquid; Ο _ (5) discharging the supernatant liquid, and returning at least a portion of the first concentrated mixed liquid Step (1) is used as the first mixed liquid, wherein the amount of sludge of the first concentrated mixed liquid that has not returned to the step (1) is smaller than the amount of sludge of the sludge feed; [0034] (6) at least part of the step (5) a supernatant and optionally a portion of the sewage feed for biological treatment of the sewage to obtain a second concentrated mixture and purified water 9 [0035] 〇 (7) will drain the purified water, and optionally at least part of the step (6) The second concentrated mixture is returned to the step (1) for use as a sludge feed; [0036] Wherein the sewage feed introduction step (1) is mixed with the sludge feed and the first mixed liquid to obtain a second mixed liquid and/or in step (6) together with the supernatant of the at least part of the step (5) The biological treatment of sewage, preferably at least part of the sewage feed is mixed with the sludge feed and the first mixed liquid in the step (1) to obtain a second mixed liquid, more preferably all the sewage is fed in the step (1) with the sludge The feed and the first mixture are mixed to obtain a second mixture. [0037] According to some embodiments of the biological wastewater treatment method of the present invention, in step (5), at least 60%, preferably at least 65%, more preferably at least 70 099140871, Form No. A0101, Page 9 / Total 79, 0993446280 - 0 201221484%, more preferably at least 75%, more preferably at least 80%, more preferably at least 85%, more preferably at least 90%, more preferably at least 93%, more preferably at least 95%, more preferably at least 98%, most preferably substantially 100% of the first concentrated mixture is returned to the step (1) for use as the first mixed liquid, and optionally the first concentrated mixed liquid which has not returned to the step (1) is discharged. [0040] [0041] According to some embodiments of the sewage biological treatment method of the present invention, in the step (6), at least 20% 'preferably at least 35%' is more preferably at least 5%, more Preferably at least 65%, more preferably at least 80%, more preferably at least 85%, more preferably at least 90%, more preferably at least 93%, more preferably at least 95%, more preferably at least 98%, most preferably substantially 100% (steps) 5) The supernatant is subjected to biological treatment of sewage. According to some embodiments of the biological treatment method for sewage according to the present invention, at least 20%, preferably at least 35%, more preferably at least 5%, more preferably at least 65%, more preferably at least 80%, more preferably, is introduced in step (1) At least 85%, more preferably at least 90%, more preferably at least 93%, more preferably at least 95%, more preferably at least 98%, most preferably substantially 100% of the sewage feed, and introducing the remainder in step (6) Sewage feed. In some preferred embodiments, all of the sewage feed is introduced in step (1) and no sewage feed is introduced in step (6). According to some embodiments of the biological biological treatment method of the present invention, the oxygen supply treatment time of the step (2) is 〇·丨~4 hours, preferably 〇5 to 2 hours ′ more preferably 0.5 to 1.5 hours. According to some embodiments of the biological treatment method for sewage according to the present invention, the anoxic treatment time of step (3) is 〇8~6 hours, preferably 丨~4 hours and more 099140871 Form No. A0101 Page 10/Total 79 Page 0993446280-0 201221484 is preferably 1 to 3 hours. [0042] According to some embodiments of the fourth (4) sewage biological treatment method, the ratio of the oxygen treatment time to the hypoxia treatment time is 1:0.5~1:6, preferably 1:1H is more preferably 1:1. ~1:2, most preferably 1:2. ^ _ Benfa 0 (four) sewage production and wealth reduction method - some (four) program, steps), 'η oxygen treatment by intermittent aeration or continuous aeration.

[_] _本㈣的污水生物處財法的—些實施方案，在步 驟（2)巾，第二混合液的溶解氧濃度為j〜*呢/l， 優選h 5〜3mg/L，更優選2〜3mg/L。 剛根據本發明的縣生物處理方法的—些實齡案，步驟 (3)和步驟⑷以沉财式進行，也就是說缺氧處理 和分離可通過赌（優選在沉搬池中職）完成。[_] _ Ben (4) Sewage Biological Division of the financial method - some implementation, in step (2) towel, the second mixture of dissolved oxygen concentration is j ~ * / l, preferably h 5 ~ 3mg / L, more It is preferably 2 to 3 mg/L. Some of the real cases of the county biological treatment method according to the present invention, step (3) and step (4) are carried out in a financial manner, that is to say, the anoxic treatment and separation can be completed by gambling (preferably in the sinking pool) .

[_]根據本發明的污水生物處理方法的一些實施方案，在步 驟⑴中，第二混合液的污泥$度今3〇〇〇〜3〇〇_g/L 優選3000〜2〇〇00mgi/L，更優選4脚〜15〇〇〇d^/l。 闺«本發_污核物處岭法的—些實財案，還包 回收步驟（2)和/或（3)中產生的氣態含鱗化合物的 回收步驟。 _]根據本發明的污水生物處理方法的一些實施方案，步驟 ⑺中返回步驟⑴用作污泥進料的第二濃縮混合液 占第二濃縮混合液的比例為卜刚％，優選約8〇〜1〇〇% ’更優選約100%。 [_]根據本發明的污水生物處理方法的一些實施方案，步驟 099140871 表單編號A0101 第11頁/共79頁 0993446280-0 201221484 (7 )中返回步驟（1 )的第二濃縮混合液占步驟（1 )的 污泥進料的比例為1〜100%，優選約80〜100%，更優選 約100% 。 [0050] 根據本發明的污水生物處理方法的一些實施方案，步驟 (6 )是選自根據Wuhrraann工藝、A/Ο工藝、Bardenpho 工藝、Phoredox工藝、A2/0工藝、倒置A2/0工藝、UCT 工藝、MUCT工藝、VIP工藝、0WASA工藝、JHB工藝、 TNCU工藝、Dephanox工藝、BCFS工藝、MSBR工藝、SBR 工藝、AB工藝、氧化溝工藝、生物膜工藝、流動床工藝 或其組合的污水生物處理步驟。 [0051] 在另一方面，本發明還提供一種用於上述污泥處理方法 的污泥處理裝置，包括：能夠將污水進料、污泥進料與 第一混合液混合得到第二混合液的第一設備；能夠將第 二混合液進行給氧處理得到第三混合液的第二設備；能 夠將第三混合液進行缺氧處理得到第四混合液的第三設 備；能夠將第四混合液分離得到上清液和第一濃縮混合 液的第四設備；能夠將上清液排出的第五設備；能夠將 至少部分第一濃縮混合液作為第一混合液引入第一設備 並且使未返回第一設備的第一濃縮混合液的污泥量小於 污泥進料的污泥量的第六設備。 [0052] 根據本發明的污泥處理裝置的一些實施方案，第二設備 經設置使得給氧處理時間為0. 1〜4小時，優選0. 5〜2小 時，更優選0. 5〜1. 5小時。 [0053] 根據本發明的污泥處理裝置的一些實施方案，第三設備 099140871 表單編號A0101 第12頁/共79頁 0993446280-0 201221484 經設置使得缺氧處理時間為0. 8〜6小時，優選1〜4小時 ，更優選1〜3小時。 [0054] 根據本發明的污泥處理裝置的一些實施方案，第二設備 和第三設備經設置使得給氧處理時間與缺氧處理時間的 比為1:0. 5〜1:6，優選1:1〜1:3，更優選1:1.5〜1:2 ，最優選1:2。 [0055] 根據本發明的污泥處理裝置的一些實施方案，第二設備 是曝氣池。[_] According to some embodiments of the biological treatment method for sewage according to the present invention, in the step (1), the sludge of the second mixed liquid is in the range of 3 〇〇〇 to 3 〇〇 _g / L, preferably 3000 to 2 〇〇 00 mgi /L, more preferably 4 feet ~ 15 〇〇〇 d ^ / l.闺 本 本 本 本 污 污 污 污 污 污 污 污 污 污 污 污 污 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些 些_] According to some embodiments of the biological treatment method for sewage according to the present invention, the ratio of the second concentrated mixture used as the sludge feed in the step (7) to the second concentrated mixture in the step (7) is 5%, preferably about 8 〇. ~1%% is more preferably about 100%. [_] According to some embodiments of the sewage biological treatment method of the present invention, step 099140871 Form No. A0101, page 11 / page 79, 0993446280-0 201221484 (7) returns the second concentrated mixture of step (1) in the step ( The ratio of the sludge feed of 1) is from 1 to 100%, preferably from about 80 to 100%, more preferably about 100%. [0050] According to some embodiments of the sewage biological treatment method of the present invention, step (6) is selected from the group consisting of Wuhrraann process, A/Ο process, Bardenpho process, Phoredox process, A2/0 process, inverted A2/0 process, UCT Wastewater biological treatment of process, MUCT process, VIP process, 0WASA process, JHB process, TNCU process, Dephanox process, BCFS process, MSBR process, SBR process, AB process, oxidation ditch process, biofilm process, fluidized bed process or combination thereof step. [0051] In another aspect, the present invention also provides a sludge treatment apparatus for the above sludge treatment method, comprising: capable of mixing a sewage feed, a sludge feed, and a first mixed liquid to obtain a second mixed liquid. a first device; a second device capable of performing oxygen treatment on the second mixed liquid to obtain a third mixed liquid; a third device capable of performing anoxic treatment on the third mixed liquid to obtain a fourth mixed liquid; capable of applying the fourth mixed liquid a fourth device for separating the supernatant and the first concentrated mixed solution; a fifth device capable of discharging the supernatant; capable of introducing at least a portion of the first concentrated mixed liquid as the first mixed liquid into the first device and returning to the first device A sixth apparatus in which the amount of sludge of the first concentrated mixture of the apparatus is less than the amount of sludge of the sludge feed. 5〜1小时。 More preferably 0. 5~1. More preferably 0. 5~1. More preferably 0. 5~1. 5 hours. 8〜6小时,优选优选。 The first embodiment of the present invention, the third device 099140871 Form No. A0101 page 12 / a total of 79 pages 0993446280-0 201221484 is set so that the anoxic treatment time is 0. 8~6 hours, preferably 1 to 4 hours, more preferably 1 to 3 hours. 5〜1:6,优选1。 The ratio of the ratio of the oxygen treatment time to the hypoxia treatment time is 1:0. : 1 to 1:3, more preferably 1:1.5 to 1:2, most preferably 1:2. [0055] According to some embodiments of the sludge treatment device of the present invention, the second device is an aeration tank.

[0056] 根據本發明的污泥處理裝置的一些實施方案，第三設備 和第四設備是沉澱池，也就是說將沉澱池同時作為第三 設備和第四設備。 [0057] 根據本發明的污泥處理裝置的一些實施方案，所述污泥 處理裝置還包括能夠收集並回收氣態含磷化合物的回收 設備。[0056] According to some embodiments of the sludge treatment apparatus of the present invention, the third apparatus and the fourth apparatus are sedimentation tanks, that is, the sedimentation tanks are simultaneously used as the third apparatus and the fourth apparatus. [0057] According to some embodiments of the sludge treatment apparatus of the present invention, the sludge treatment apparatus further includes a recovery apparatus capable of collecting and recovering gaseous phosphorus-containing compounds.

[0058] 在另一方面，本發明還提供一種用於上述污水生物處理 方法的污水生物處理裝置，包括，：能夠將污泥進料與第 一混合液混合得到第二混合液的第一設備；能夠將第二 混合液進行給氧處理得到第三混合液的第二設備；能夠 將第三混合液進行缺氧處理得到第四混合液的第三設備 :能夠將第四混合液分離得到上清液和第一濃縮混合液 的第四設備；能夠將上清液排出的第五設備；能夠將至 少部分第一濃縮混合液作為第一混合液引入第一設備並 且使未返回第一設備的第一濃縮混合液的污泥量小於污 泥進料的污泥量的第六設備；能夠將至少部分第五設備 099140871 表單編號A0101 第13頁/共79頁 0993446280-0 201221484 排出的上清液進行污水生物處理得到第二濃縮混合液和 淨化出水的第七設備；能夠將淨化出水排出的第八設備 :能夠將污水進料引入第一設備與污泥進料和第一混合 液混合得到第二混合液和/或引入第七設備與上清液一起 進行污水生物處理的第九設備；以及任選的能夠將至少 部分第二濃縮混合液引入第一設備的第十設備。 [0059] 根據本發明的污水生物處理裝置的一些實施方案，第二 設備經設置使得給氧處理時間為0. 1〜4小時，優選0. 5〜 2小時，更優選0. 5〜1. 5小時。 [0060] 根據本發明的污水生物處理裝置的一些實施方案，第三 設備經設置使得缺氧處理時間為0. 8〜6小時，優選1〜4 小時，更優選1〜3小時。 [0061] 根據本發明的污水生物處理裝置的一些實施方案，第二 設備和第三設備經設置使得給氧處理時間與缺氧處理時 間的比為1:0. 5〜1:6，優選1:1〜1:3，更優選1:1. 5〜 1:2，最優選1:2。[0058] In another aspect, the present invention also provides a sewage biological treatment apparatus for the above sewage biological treatment method, comprising: a first apparatus capable of mixing a sludge feed with a first mixed liquid to obtain a second mixed liquid a second device capable of oxygenating the second mixed liquid to obtain a third mixed liquid; a third device capable of performing anoxic treatment on the third mixed liquid to obtain a fourth mixed liquid: capable of separating the fourth mixed liquid a fourth device for clearing liquid and a first concentrated mixed solution; a fifth device capable of discharging the supernatant; capable of introducing at least a portion of the first concentrated mixed liquid as the first mixed liquid into the first device and returning to the first device The sixth device for the amount of sludge of the first concentrated mixture is smaller than the amount of sludge for the sludge feed; the supernatant capable of discharging at least part of the fifth device 099140871 Form No. A0101 Page 13 / Total 79 Page 0993446280-0 201221484 a seventh device for biologically treating sewage to obtain a second concentrated mixed liquid and purifying the effluent; an eighth device capable of discharging purified purified water: capable of introducing the sewage feed into the first device and the sewage Mixing the feed with the first mixture to obtain a second mixture and/or a ninth device for introducing a seventh device with the supernatant for biological treatment of the sewage; and optionally capable of introducing at least a portion of the second concentrated mixture into the first The tenth device of the device. 5〜2小时。 More preferably 0. 5~1. More preferably 0. 5~1. More preferably 0. 5~1. 5 hours. [0060] According to some embodiments of the sewage biological treatment device of the present invention, the third device is set such that the anoxic treatment time is 0.8 to 6 hours, preferably 1 to 4 hours, more preferably 1 to 3 hours. 5〜1:6,优选1。 The ratio of the ratio of the oxygen treatment time to the anoxic treatment time is 1:0. : 1 to 1:3, more preferably 1:1. 5 to 1:2, most preferably 1:2.

ILIL

[0062] 根據本發明的污水生物處理裝置的一些實施方案，第二 設備是曝氣池。 [0063] 根據本發明的污水生物處理裝置的一些實施方案，第三 設備和第四設備是沉澱池，也就是說將沉澱池同時作為 第三設備和第四設備。 [0064] 根據本發明的污水生物處理裝置的一些實施方案，所述 污泥處理裝置還包括能夠收集並回收氣態含磷化合物的 回收設備。 099140871 表單編號A0101 第14頁/共79頁 0993446280-0 201221484 [0065] 根據本發明的污水生物處理裝置的-些實施方案’第七 設備是選自能夠根據Wuhrmann卫藝、_工蔽、 Id611*工 藝、A2/〇 工藝、倒置 A2/0工藝、UCT工藝、臟τ工藝、np工藝、議工藝 JHB工藝、TNCU工藝、工藝、工藝、 MSBR工藝、敝藝、Αβ工藝、氣化溝工藝生賴工 藝、流動床工藝或其組合的進行污水生物處理的設備。 [0066] Ο [0067] 在另-方面’本發明還提供一種降低來自污水生物處理 過程的污泥中碳、氮㈣含量的方法，包括將污泥作為 污泥進料通過上述祕處理方料降低其中碳、氣和碟 的含量。 在另-方面’本發明還提供—祕低污水t碳氮和鱗 含董的方法，包括將污水作為污水進料通過上述污水生 物處理方法來降低其中碳、氮和磷的含量。 [0068] 〇 在另一方面，本發明還提供一種回收來自污水生物處理 過程的污泥中射方法，包括（i)將污泥作為污泥進料 通過上述污泥處理方法將其中:的含磷化合物，特別是以 溶液形式存在的㈣化合物，轉化為氣態含填化合物而 逸出，和（ii)回收步驟（i)中逸出的氣態含磷化合物 [0069] 在另一方面，本發明還提供一種回收污水中磷的方法， 包括（i)將污水作為污水進料通過上述污水生物處理方 法將其中的含碟化合物，特別是以溶液形式存在的含鱗 化合物，轉化為氣態含磷化合物而逸出，和（ii)回收 099140871 表單編號A0101 第15頁/共79頁 0993446280-0 201221484 步驟（i )中逸出的氣態含填化合物。 [0070] 本發明的發明人驚奇地發現，採用上述污泥處理方法或 污泥減量化處理方法可以實現長期穩定運行而無需排泥 並且無污泥積累。因此，本發明的污泥處理方法或污泥 減量化處理方法能夠基本上消除污泥排放，徹底解決了 污泥排放問題，具有巨大的社會和經濟意義。 [0071] 本發明的上述污泥處理方法或污泥減量化處理方法可以 方便地與各種合適的污水生物處理方法結合從而形成的 新的污水生物處理方法。特別地，所述污水生物處理方 法產生的剩餘污泥可以由本發明的污泥處理方法處理而 消解。此外，由本發明的污泥處理方法產生的出水（上 清液）通常呈中性（即pH值在6〜8之間，尤其在6.5〜 7.5之間），因此無需調節pH值即可通過進一步的污水生 物處理得到符合排放標準的淨化出水。尤其特別地，本 發明的污水生物處理方法可在基本不排泥的情況下仍然 取得良好的除磷效果。 [0072] 與傳統污水生物處理方法相比，新的污水生物處理方法 能夠顯著減少甚至完全消除污泥排放，並且還具有良好 的汙水處理效果和出水水質、更小的設備占地面積、更 少的建設成本和運行成本以及更高的抗衝擊負荷能力和 運行穩定性。本發明的上述污泥處理方法或污泥減量化 處理方法還特別適合用於改造各種現有的污水生物處理 裝置以便顯著減少甚至完全消除污泥排放。 【實施方式】 [0073] 為了進一步瞭解本發明，下面結合附圖對本發明的一些 099140871 表單編號 A0101 第 16 頁/共 79 頁 0993446280-0 201221484 [0074] ❹ [0075] [0076] Ο 099140871 優選實施方案進行描逑。應當理解，這⑽述只是為了 =步說明本發明的特、優點，而不找本發明權利 要求保護範圍的限制。 在本發明中，術語“ . 是指任何可用生物處理方法 ^的主要含有機污染物的污水，包括任何合適的工業 廢水 '生活污水及其任音 污水可以是從產生污水=合’特別是城市生活污：。 搜集得到污水、將污^點直接制污水、通過管網 7存~定時間後得到的污水'或 疋5 1過發酵、酸域調節'成分調節、濃度調節 以及沉澱、過濾、離心 珉刀^ P 得到的污水。 ^物、化學和/或物理處理之後 在本發明中，術語“ /T水生物處理”是指利用微生物的 代謝作用使污水中的有機污染物轉化為穩定的無害物質 的過程。根據微生物對氧的需求，可以分為好氧生物處 理、厭氧生物處理等。 h. | i 3 d f Ά...,:::.:厂、_ 好氧生物處理根據微生物在水中存在的狀態，可分為活 心泥法和生物哺。活性污泥法是目前最廣泛應用的 X生物處理方去，其中將空氣鼓入含有大量有機物質 =污水二’經過-定時間後’水中即形纽物絮凝體— 亏;匕在活性污泥上棲息、生活著大量的微生物 ，這些微生物財中的有職料食料，獲得能量並不 斷增長繁殖’從而使污水得到淨化。活性污泥法的基本 流程如第丨_示。生物膜法是通過污核麵體填料， 在填料上生成污泥㈣生物膜，生物❹㈣Η量的 微生物起到與活性污泥同樣的淨化污水的作用。生 表單編號Α0101 第17頁/共79頁 201221484 法的設施包括生物渡池、生物轉盤、生物接觸氧化和生 物流化床等。 [0077] 厭氧生物處理是利用兼性厭氧菌和專性厭氧菌在無氧條 件下降解有機污染物的處理技術。厭氧生物處理的設施 包括普通消化池、厭氧濾池、厭氧污泥床、厭氧轉盤、 擋板式厭氧反應器等。 [0078] 由於污水中的污染物質多種多樣，往往需要幾種處理方 法結合才能達到淨化目的。常見的污水生物處理法的例 子包括活性污泥法、OSA (Oxic-Settl ing-Anaerobic )工藝、厭氧生物處理工藝（例如厭氧生物濾池、厭氧 生物轉盤、厭氧接觸法、上流式厭氧污泥床和分段厭氧 消化法等）、Wuhrmann工藝:'、A/Ο工藝、Bardenpho工 藝、Phoredox工藝、A2/0工藝、倒置A2/0工藝、UCT工 藝、MUCT工藝、VIP工藝、0WASA工藝、JHB工藝、TNCU 工藝、Dephanox工藝、BCFS工藝、，SBR (Sequencing Batch Reactor Activaten Sludge Process )工藝 、MSBR工藝、AB工藝、生物膜工藝例如生物濾池、生物 轉盤、生物接觸氧化法、生物流化床和曝氣生物遽池等 、以及上述各種工藝的任意合適的組合。 [0079] 在本發明中，術語“污泥”是指污水生物處理過程中產 生的任何含有活性污泥的污泥。活性污泥是污水中的生 物形成的絮凝體，主要含有水和各種微生物，例如好氧 菌、厭氧菌和兼性菌，還有真菌、藻類、原生動物等。 隨著污泥的馴化和所處環境的改變，污泥中各種微生物 類群也會發生例如數量和比例的變化甚至基因突變等以 099140871 表單編號A0101 第18頁/共79頁 0993446280-0 201221484 適應生存環境。按污水的來源來分，污泥的例子可以包 括生活污水污泥和工業廢水污泥。按污泥的來源來分 ，巧泥的例子通常可以包括：來自活性污泥法二次沉澱 池的排泥（也成為剩餘污泥或剩餘活性污泥，其主要成 - 刀為微生物和水）、來自生物膜法二次沉澱的排泥（也 稱為腐殖污泥，主要成分為脫落的生物膜）、來自汙水 處理廠初次沉澱池的排泥（也稱為初次沉澱污泥，主要 成分為固體有機物和微生物等）、廢水經厭氧處理後排 0 出的污泥（也稱為厭氧污泥）、將上述污泥經消化後的 巧泥（也稱消化污焉或熟污泥）、以及來自化學沉澱池 的污泥（也稱為化學污泥）等、按'污泥的不同階段來分 ，污泥的例子可以包括：生污泥或新鮮污泥（即，未經 , 任何處理的污泥）、濃縮污泥、消化污泥、脫水污泥、 幹化污泥等。本發明的污泥可以是上述任何污泥及其組 合，特別是含水量為90%以上、95%以上、優選97%以上 的剩餘污泥’優選新鮮污泥。 〇 [0080]在本發明中’術語“混合液”是指上述污泥與水形成的 混合物’也稱為泥水混合物或泥水混合液。合適的混合 液中的污泥具有良好的沉降性能，特別是在曝氣和沉澱 過程中不發生污泥膨脹或污泥上浮◊通常，混合液的污 泥體積指數（SVI，常用SVI30表示，指混合液在lOOOmL 量筒中靜置30分鐘以後’ 1克活性污泥懸浮固體所占的體 積’單位為mL/g)有利地為小於給氧處理時發生污泥膨 脹的最小值’例如SVI30可以小於2〇〇ml/g ,小於 150ml/g，小於i〇〇mi/g ,或小於5〇ml/g。 099140871 表單編號A0101 第19頁/共79頁 0993446280-0 201221484 [0081] 在本發明中，術語“濃縮混合液”是指將上述混合液經 分離除去至少部分水後得到的污泥濃度提高的混合液， 在一些情況中也稱為污泥，例如第一濃縮混合液也可以 稱為第一污泥。所述分離可以是沉澱分離、離心分離、 過濾分離等。在沉澱分離的情形中，混合液中的污泥逐 漸下沉形成處於混合液上部的上清液和處於混合液下部 的污泥濃度增加的濃縮混合液。在一些情況中，可以將 占整個混合液體積5〜85% (例如：5〜10%、10〜15%、 15〜20% ' 20〜25%、25〜30%、30〜35%、35〜40%、 40〜45%、45〜50%、50〜55%、55〜60%、65〜70%、 70〜75%、75〜80%、80〜85%)的下部混合液作為濃縮 混合液。 [0082] 在本發明中，術語“給氧處理”是指使氧與混合液接觸 ，尤其是含氧氣體（例如空氣）與混合液接觸。在本發 明中，“給氧處理”可以通過任何能夠使含氧氣體與混 合液接觸的方法來實現，例如通過將含氧氣體通入流動 的或非流動的混合液中進行，特別是用含氧氣體對混合 液曝氣來實現。好氧處理即是典型的給氧處理。給氧處 理可以在任何合適的條件下以任何合適的方式進行，例 如在常壓、加壓、常溫、低溫和/或升溫條件下以鼓風曝 氣、機械曝氣、射流曝氣等方式在合適的設備例如曝氣 池、氧化溝、流化床、移動床或膜設備等中進行。優選 使用曝氣池曝氣。任何合適的含有氧氣的氣體都可用於 曝氣，優選使用空氣曝氣。在給氧處理中，混合液的溶 解氧濃度可以逐漸升高到期望值。給氧處理的時間一般 099140871 表單編號A0101 第20頁/共79頁 0993446280-0 201221484 由混合液在給氧處理裝置中的停留時間（或混合液與氧 接觸的時間）以及通入的含氧氣體的量來確定。通常， 在給氧處理中，好氧生物和兼性生物得到増長而厭氧 生物受到抑制。 [0083] Ο Ο 在本發明中，術語“缺氧處理”是指基本上避免含氧氣 體與混合液接觸。缺氧處理可以通過任何能夠基本避免 含氧氣體與混合液接觸的方法來實現。例如，通過停止 曝氣和任選的脫氣過程來實現。在本發明中，無論是否 存在硝態氮’只要基本上不存在溶解氣，例如溶解氧水 準低於0. lmg/L時，即可認為是處於缺氧矣理狀態。也就 是說，在一些文獻中所述的缺氧條件（有確態氮無溶解 氧）和厭氧條件（無硝態氮無溶解氧）下都可以進行本 發明的缺氧處理。在一些情形中，隨著含氣氣體的逸出 和溶解氧的消耗’溶解氧濃度可以逐漸降低到期望值’ 例如約等於Omg/L的水準。特別地，缺氧處理可以通過在 停止曝氣的情況下使混合液在沉澱池中緩’慢流動的方式 實現。合適的沉澱池可以是平流式、豎流式和輻流式沉 澱池》缺氧處理的時間一般由混合液在缺氧處理裝置中 的停留時間確定。通常’在缺氧處理中，厭氧生物和兼 性生物得到增長’而好氧生物受到抑制。 [0084] 在本發明中，術語“污泥量”也稱污泥含量，通常是指 污泥或污水或混合液或濃縮混合液中的固體含量或懸淨 物含量。固體或懸浮物通常主要包括生物體和有機固體 物質（包括可生物降解的和難生物降解的有機物質）。 在一些情況下’污泥量也可以用MLSS總量表示。MLSS是 099140871 '表單編號A0101 第21頁/共79頁 0993446280^ 201221484 /«i 〇 液心浮固體》農度（mixed iiqU〇r SUSpende(j s ο 1 i d s )的簡寫，它又稱為混合液污泥濃度，它表示的是 在曝氣池單位谷積混合液内所含有的活性污泥固體物的 總重量（mg/L)。 [0085] [0086] [0087] 099140871 在一個方面’本發明提供一種污泥處理方法，其中所述 污泥產生於污水生物處理過程，所述方法包括·· （1)將 污泥進料與第―混合液混合得到第二混合液；（2)將第 一混合液進行給氧處理得到第三混合液；（3)將第三混 =液進行缺氧處理得到第四混合液；⑷將第四混合液 刀離得ii上β液和第—;農縮混合液；（5 )將上清液排出 ，將至少部分第一濃縮混合液返回步驊（1 )用作第一混 合液，其中未返回步驟⑴的第一濃縮混合液的污泥量 小於污泥進料的污泥量。 根據本發明的污泥處理方法，未返回步驟⑴的第—濃 縮混合液的污泥量小於污泥進_緣量，也即存 在污泥量的淨輸人。特別是在第—濃縮混合液全部返回 =⑴的情況下，污泥量的淨輸入就是污泥進料的污 泥量（如第2圖所示）。 明的發明人驚奇地發現，在長期運行時儘管存在 :泥量的淨輸人，混合液中的污泥量仍然保持在相對穩 定的水準而不會無限制地增長，該水準受污泥進料的成 分和流量以及其_作條件的影響，例如在存在污水進 料時，也受污水進料的流量的影響。因此，本發明的污 泥處理方法是-種科減量化處理料。也就是說，本 發明的污泥處理方法能夠消解污泥進料中的污 表單編號編1 帛22頁/共79 Η 201221484 泥減量。在魏的實施^巾，本發_污泥處理方法 可以在〉了泥進料連續加入的料下，長期穩定地運行而 無需排泥，從而消除了污泥的排放。此外，本發明的發 明人還驚奇地發現，即便污一料具有較高含量的I 氣和磷’並以排出任何第1縮混合液’上清液 、氮_含量也能減錢低切，也就是說，本發明 的污泥處理方法具有顯著的去除碳、氮和磷的效果。 [0088] ❹ [0089] ❹ [0090] 099140871 不受任何理論的約束，本發明的發明人認為本發明的、亏 泥處理方域料誠定地運行心需排泥的部分可能 原因如下。 首先’由於排㈣污泥量切外加的污泥量，現合液中 的污泥量本應持續增長，然而在穩定運行中混合液的污 泥濃度儘管很高但並未持續增加而是在高水準下保持穩 定（也就是說在敎運行中，系統中混合液的污泥量基 本保持不變），因此可以認為混合液中的生物類群處ς 消長平衡的狀態，即新增的污泥量（包括污泥進料的污 泥量和混合液中生物繁殖而增:加的污泥量）和死亡並消 解的污泥量達到了動態平衡，因而沒有污泥量的淨增長 在已知的各種污水生物處理方法中，由於生物的增殖， 無論二沉池的污泥是否回流返回卫藝的上游，都有剩餘 污泥排出。就整個工藝而言，由於通常只有污水原水進 料而沒有污泥的淨輸人’因此排出的污泥量總是大於外 加的污泥量。此外’由於二沉池出水中溶解性有機物濃 度必須處於祕的水準⑽収W錢要求，曝氣池 表單編號Α0101 第23頁/共79頁 0993446280-0 201221484 必須採用足夠高的曝氣量和足夠長的曝氣時間以降低水 中溶解性有機物的濃度。然而，在好氧條件下，低有機 物濃度通常有利於絲狀菌的增殖而導致污泥膨脹。同時 ，高曝氣量和長曝氣時間也進一步增加了含較高濃度污 泥的混合液發生污泥膨脹的可能性。因此，在已知的各 種活性污泥工藝中，曝氣池中的污泥濃度通常難以達到 較高水準，也就是說無法實現生物類群的消長平衡狀態 。另外，由於生物對惡劣環境（例如較低的營養物濃度 )的抵抗，已知的污泥好氧處理方法和污泥厭氧處理方 法通常僅能消解不足6 0 %的污泥（也即無法將污泥完全消 解），因此採用這些方法的工藝也仍然需要排出一定量 的剩餘污泥。 [0091] 在本發明的污泥處理方法中，由於主要目的是消解污泥 ，排出的上清液中溶解性有機物的濃度可不受限制而處 於較高水準，因此有利地限制了絲狀菌的增殖，降低了 需氧量（例如曝氣量），從而減小了給氧處理例如曝氣 時發生污泥膨脹的可能性。此外，較高水準的溶解性有 機物為生物體提供了足夠的營養，形成了有利於生物的 代謝、繁殖和程式死亡的環境，使得污泥中的生物體在 大量繁瘦的同時也大量地消解。 [0092] 此外，在本發明的污泥處理方法中，污泥交替、反復地 經歷了給氧處理和缺氧處理，有利於菌膠團細菌的增殖 ，污泥的沉降速度和澄清效果得到提高。因此，本發明 的污泥處理方法可以實現高污泥濃度而不發生污泥膨脹 099140871 表單編號A0101 第24頁/共79頁 0993446280-0 201221484 [0093] 另外，由於第一濃縮混合液通常大量甚至全部回流返回 ’ [0094] 步驟（1)使得污泥齡相對較長（例如數月、數年甚至更長 )，因此繁殖速率較慢的能分解難降解物質的微生物得 以正常生長，增強了污泥的分解作用。同時在高污泥濃 度條件下，依次經過給氧處理和缺氧處理，混合液中的 可生物降解物質和難生物降解物質（包括死亡生物體） 都得到了快速有效的消解，使得含碳、氮、磷等的化合 物成為溶解性有機物隨上清液排出或成為揮發性物質而 逸出。 綜上所述，在本發明的污泥處理方法中，混合液中的污 泥具有優異的沉降性能和較低的需氧量（例如曝氣量） 並且能夠降解各種有機物質（包括死亡生物體）使之成 為水溶性物質或氣態物質，因此混合液可以具有相當高 的污泥濃度使生物類群處於消長平衡狀態而不發生污泥 膨脹，從而使得本發明的污泥處理方法能夠長期穩定地 運行以減少甚至完全消除污泥排放。 〇 [0095] 在一些實施方案中，步驟（2)的給氧處理和步驟（3) 的缺氧處理可以在同一構築物或容器中以續批的方式進 行。例如，步驟（1)至（4)可以在同一構築物或容器 中進行，其中在步驟（1)中將一批污泥進料與前批污泥 進料處理後得到第一濃縮混合液（作為第一混合液）混 合得到第二混合液，在步驟（2)中將第二混合液進行給 氧處理得到第三混合液，在步驟（3)中將第三混合液進 行缺氧處理得到第四混合液，在步驟（4)中將第四混合 液分離得到上清液和第一濃縮混合液，在步驟（5)中將 099140871 表單編號A0101 第25頁/共79頁 0993446280-0 201221484 並且將至少部分（優選全部）第-濃縮混合 ^在所述構築物或容器中並用作步驟⑴的第-混合 史’然後將下一批污;尼進料5|入所述構築物或容器並重 複上述步驟。步驟（5)巾，上清奸料過能夠將上清 _出的設_如排液管來排出。採用續批的方式可以 即約用地和建設投資。在―些實施方案中，步驟⑴的 給氧處理和步驟⑴㈣氧處理可以在步驟⑷的分 離前反復地進行一次或多次。 [0096] 在另一些實施方案中，在本發_污泥處理方法中步 驟⑴的給氧處理和步驟(3)的缺氧處理可以在不同 的構築物或容射以半連續或連續的方式進行。例如， 步驟⑴i⑷可以在不同的構築物中半連續（即一 些步驟以連續方式運行而另__些步驟以間歇方式運行的 情形）或連續地進行’其中在步驟⑴中將污泥進料間 歇或連續地弓丨人第-構築物並與第—混合液混合得到第 二混合液，將第二混合液間歇或連續地引人第二構築物 以間歇或連續地賴步驟⑴的給氧處理得到第三混合 液’將第二混合液間歇或連續地引入第三構築物以間歇 或連續地進行步驟⑴的缺氧處理得到第四混合液，將 第四混合液通過分離設備間歇或連續地進行步驟（4)的 分離以得到上清液和第一濃縮混合液，在步驟中將 上清液間歇或連續地排出，將至少部分第一濃縮混合液 間歇或連續地引入第一區，並任選地將第一濃縮混合液 的剩餘部分間歇或連續地排出，其中未返回步驟（1)的 第一濃縮混合液的污泥量小於污泥進料的污泥量。第一 099140871 表單編號A0101 第26頁/共79頁 0993446280-0 201221484 、第二和第三構築物可以是各自獨立的不同構築物或者 是同一構築物的不同區域。如果步驟（3)的缺氧處理以 沉澱方式進行，那麼步驟（4)的分離可以與步驟（3) ❹ [0097] 在同一構築物中同時進行（也就是說第三構築物也用作 分離設備）。在步驟（5)中，上清液可以通過能夠將上 清液排出的設備例如排液管排出，第一濃縮混合液可以 通過例如污泥回流管引入第一構築物。採用半連續或連 續的方式可以有利地改善污泥處理的效率。各步驟是否 以間歇或連續方式進行主要根據污泥進料的流量和成分 以及各設備的操作條件來確定，以便有利地優化和穩定 運行從而獲得最佳的處理效果。 在本發明的污泥處理方法中，在步驟（5)中未返回步驟 (1 )的第一濃縮混合液的污泥量小於污泥進料的污泥量 ο 。在一些情形中，在步驟（5)中基本上全部第一濃縮混 合液都返回步驟（1 )用作第一混合液，因此基本上沒有 排出第一濃縮混合液。然而，也不排除在連續操作的某 些情況下，暫態排出的第一濃縮混合液的污泥量大於污 泥進料的污泥量，只要在長期運行中排出的第一濃縮混 合液的剩餘部分的污泥量的平均值小於污泥進料的污泥 量的平均值從而存在污泥量的淨輸入即可。根據本發明 的污泥處理方法的一些實施方案，在步驟（5)中未返回 步驟（1)的第一濃縮混合液的污泥量至多為污泥進料的 污泥量的下列任意比例之一，例如約95%、約85%、約 70%，約50%、約30%，約25%，約20%，約 15%，約 10%， 約5%，約3%，約1%，約0%。該比例有利地為約0%，也就 099140871 表單編號Α0101 第27頁/共79頁 0993446280-0 201221484 是說將步驟（5 )的第一濃縮混合液基本上全部返回步驟 (1 )用作第一混合液。此外，該比例特別有利地小於約 30%，約25%，約20%，約15%，約 10%，約5%，約3%，約 1%，尤其是約0% ’以便獲得較長的泥齡。不受任何理論 約束’較長的泥齡使得繁殖速率較慢的能分解難降解物 質的微生物得以正常生長，增強了污泥的分解作用。同 時’ s亥比例小於約3 0 % ’約2 5 % ’約2 0 %，約15 %，約1 〇 % ’約5 Z ’約3 % ’約1 % ’尤其是約〇 % ’這樣也有利於提高 第一、第二、第三和第四混合液的污泥濃度。 ... ......[0062] According to some embodiments of the sewage biological treatment device of the present invention, the second device is an aeration tank. [0063] According to some embodiments of the sewage biological treatment apparatus of the present invention, the third apparatus and the fourth apparatus are sedimentation tanks, that is, the sedimentation tanks are simultaneously used as the third apparatus and the fourth apparatus. [0064] According to some embodiments of the sewage biological treatment apparatus of the present invention, the sludge treatment apparatus further includes a recovery apparatus capable of collecting and recovering gaseous phosphorus-containing compounds. 099140871 Form No. A0101 Page 14 of 79 Page 99993446280-0 201221484 [0065] Some embodiments of the sewage biological treatment apparatus according to the present invention are selected from the group consisting of Wuhrmann's Weiyi, Yigong, Id611* Process, A2/〇 process, inverted A2/0 process, UCT process, dirty tau process, np process, process JHB process, TNCU process, process, process, MSBR process, 敝 art, Αβ process, gasification ditch process A process for biological treatment of sewage by a process, a fluidized bed process, or a combination thereof. [0066] In another aspect, the present invention also provides a method for reducing the content of carbon and nitrogen (IV) in sludge from a biological treatment process of sewage, comprising passing the sludge as a sludge feed through the above-mentioned secret treatment materials. Reduce the amount of carbon, gas and dish. In a further aspect, the invention also provides a method for lowering sewage t carbon nitrogen and scales, comprising using sewage as a sewage feed to reduce the carbon, nitrogen and phosphorus contents thereof by the above sewage biological treatment method. [0068] In another aspect, the present invention also provides a method for recovering sludge from a sewage biological treatment process, comprising: (i) using sludge as a sludge feed through the sludge treatment method described above: a phosphorus compound, in particular a compound of the formula (4) in the form of a solution, which is converted to a gaseous form-containing compound, and (ii) a gaseous phosphorus-containing compound which is recovered in the recovery step (i). In another aspect, the invention There is also provided a method for recovering phosphorus in sewage, comprising: (i) converting sewage into a gaseous phosphorus-containing compound by using the sewage as a sewage feed by the above-mentioned sewage biological treatment method, wherein the dish-containing compound, particularly the scaly compound existing in the form of a solution, is converted into a gaseous phosphorus-containing compound And escape, and (ii) recovery 099140871 Form No. A0101 Page 15 / Total 79 Page 0993446280-0 201221484 The gaseous inclusion compound escaped in step (i). The inventors of the present invention have surprisingly found that the above-described sludge treatment method or sludge reduction treatment method can achieve long-term stable operation without sludge discharge and sludge accumulation. Therefore, the sludge treatment method or the sludge reduction treatment method of the present invention can substantially eliminate sludge discharge, completely solves the problem of sludge discharge, and has great social and economic significance. The above-described sludge treatment method or sludge reduction treatment method of the present invention can be easily combined with various suitable sewage biological treatment methods to form a new sewage biological treatment method. In particular, the excess sludge produced by the sewage biological treatment method can be treated by the sludge treatment method of the present invention to be digested. In addition, the effluent (supernatant) produced by the sludge treatment method of the present invention is generally neutral (ie, the pH is between 6 and 8, especially between 6.5 and 7.5), so that it is possible to further pass without adjusting the pH. The biological treatment of sewage gets purified water that meets emission standards. In particular, the sewage biological treatment method of the present invention can still achieve a good phosphorus removal effect without substantially draining mud. [0072] Compared with the traditional sewage biological treatment method, the new sewage biological treatment method can significantly reduce or even completely eliminate sludge discharge, and also has good sewage treatment effect and effluent water quality, smaller equipment footprint, and more Low construction and operating costs as well as higher impact load capacity and operational stability. The above sludge treatment method or sludge reduction treatment method of the present invention is also particularly suitable for retrofitting various existing sewage biological treatment apparatuses in order to significantly reduce or even completely eliminate sludge discharge. [Embodiment] [0073] In order to further understand the present invention, some 099140871 form numbers A0101 will be described below with reference to the accompanying drawings. Page 16 of 79 0993446280-0 201221484 [0074] 007 [0076] 007 099140871 Preferred implementation The program is described. It should be understood that this (10) is only for the purpose of explaining the features and advantages of the present invention, and does not limit the scope of the claims. In the present invention, the term "." refers to any available biological treatment method that mainly contains organic pollutants, including any suitable industrial wastewater, 'situary sewage and its sulphuric sewage can be generated from sewage = combined 'especially the city Staining of life: Collecting sewage, collecting sewage directly into sewage, passing through the pipe network 7 and collecting the sewage after a certain period of time 'or 发酵5 1 fermentation, acid domain regulation' composition adjustment, concentration adjustment and precipitation, filtration, The sewage obtained by centrifuging the boring tool ^ P. After the physical, chemical and/or physical treatment, in the present invention, the term "/T water biological treatment" means the use of the metabolism of microorganisms to convert the organic pollutants in the sewage into stable The process of harmless substances. According to the demand of microorganisms for oxygen, it can be divided into aerobic biological treatment, anaerobic biological treatment, etc. h. | i 3 df Ά...,:::.: factory, _ aerobic biological treatment according to The state in which microorganisms exist in water can be divided into living core mud method and biological feeding. Activated sludge method is the most widely used X biological treatment method, in which air is blown into a large amount of organic matter = sewage two - After a certain period of time, 'the water is shaped as a floc--deficient; the cockroach inhabits and lives a large number of microorganisms on the activated sludge. These microbial resources have the feed materials, gain energy and grow and multiply' to purify the sewage. The basic process of the activated sludge process is shown in Figure _. The biofilm method is to use the nucleus surface filler to form sludge on the filler (4) biofilm, and the biological ❹ (4) Η amount of microorganisms to purify the same sewage as the activated sludge. The role of the form. Α0101 Page 17 of 79201221484 The facilities of the method include biological water tank, biological turntable, biological contact oxidation and biological fluidized bed, etc. [0077] Anaerobic biological treatment is the use of facultative anaerobic bacteria And obligate anaerobic bacteria to degrade organic pollutants under anaerobic conditions. Anaerobic biological treatment facilities include common digester, anaerobic filter, anaerobic sludge blanket, anaerobic turntable, baffle anaerobic Reactors, etc. [0078] Due to the variety of pollutants in sewage, it is often necessary to combine several treatment methods to achieve purification purposes. Examples of common sewage biological treatment methods include Sludge method, OSA (Oxic-Settling-Anaerobic) process, anaerobic biological treatment process (such as anaerobic biofilter, anaerobic bio-rotary, anaerobic contact, upflow anaerobic sludge bed and segmentation Oxygen digestion, etc.), Wuhrmann process: ', A / Ο process, Bardenpho process, Phoredox process, A2 / 0 process, inverted A2 / 0 process, UCT process, MUCT process, VIP process, 0WASA process, JHB process, TNCU process , Dephanox process, BCFS process, SBR (Sequencing Batch Reactor Activaten Sludge Process) process, MSBR process, AB process, biofilm process such as biofilter, biological turntable, biological contact oxidation, biological fluidized bed and aerated biological enthalpy Pools, etc., and any suitable combination of the various processes described above. [0079] In the present invention, the term "sludge" refers to any sludge containing activated sludge produced during the biological treatment of sewage. Activated sludge is a floc formed by biological substances in sewage. It mainly contains water and various microorganisms such as aerobic, anaerobic and facultative bacteria, as well as fungi, algae and protozoa. With the domestication of the sludge and the change of the environment, various microbial groups in the sludge will also occur, for example, changes in quantity and proportion, and even genetic mutations, etc., 099140871 Form No. A0101 Page 18 / Total 79 Page 0993446280-0 201221484 Adapt to Survival surroundings. According to the source of the sewage, examples of the sludge may include domestic sewage sludge and industrial wastewater sludge. According to the source of the sludge, the example of the skillful mud can generally include: sludge from the secondary sedimentation tank of the activated sludge process (also becoming surplus sludge or residual activated sludge, which is mainly formed into a microbe and water). The sludge from the secondary precipitation of the biofilm method (also known as humic sludge, the main component is the shedding biofilm), and the sludge from the initial sedimentation tank of the sewage treatment plant (also known as the primary sedimentation sludge, mainly The components are solid organic matter, microorganisms, etc., and the sludge discharged from the wastewater after anaerobic treatment (also called anaerobic sludge), and the mud that has been digested by the above sludge (also called digestive pollution or maturity) Mud), as well as sludge from chemical sedimentation tanks (also known as chemical sludge), etc., according to different stages of sludge, examples of sludge may include: raw sludge or fresh sludge (ie, not , any treated sludge), concentrated sludge, digested sludge, dewatered sludge, dried sludge, etc. The sludge of the present invention may be any of the above-mentioned sludges and combinations thereof, particularly, excess sludge of preferably 90% or more, 95% or more, preferably 97% or more, preferably fresh sludge. 00 [0080] In the present invention, the term "mixture" means a mixture of the above sludge and water, which is also referred to as a muddy water mixture or a muddy water mixture. The sludge in the suitable mixture has good sedimentation performance, especially in the process of aeration and sedimentation, no sludge expansion or sludge floating. Generally, the sludge volume index of the mixture (SVI, commonly used in SVI30, refers to After the mixture is allowed to stand in a 1000 mL measuring cylinder for 30 minutes, the volume of '1 gram of activated sludge suspended solids' is mL/g) is advantageously less than the minimum value of sludge expansion occurring during oxygen treatment. For example, SVI30 can be smaller than 2〇〇ml/g, less than 150ml/g, less than i〇〇mi/g, or less than 5〇ml/g. 099140871 Form No. A0101 Page 19/79 Page 0993446280-0 201221484 [0081] In the present invention, the term "concentrated mixture" refers to a mixture of increased sludge concentration obtained by separating at least a portion of water from the above mixture. The liquid, also referred to as sludge in some cases, for example, the first concentrated mixture may also be referred to as a first sludge. The separation may be precipitation separation, centrifugation, filtration separation, and the like. In the case of precipitation separation, the sludge in the mixed solution gradually sinks to form a supernatant liquid in the upper portion of the mixed liquid and a concentrated mixed liquid in which the concentration of the sludge in the lower portion of the mixed liquid is increased. In some cases, it may be 5 to 85% of the entire volume of the mixed solution (for example, 5 to 10%, 10 to 15%, 15 to 20% '20 to 25%, 25 to 30%, 30 to 35%, 35 ~40%, 40~45%, 45~50%, 50~55%, 55~60%, 65~70%, 70~75%, 75~80%, 80~85%) of the lower mixture as a concentrate Mixture. In the present invention, the term "oxygenation treatment" means bringing oxygen into contact with a mixed solution, especially an oxygen-containing gas such as air, in contact with the mixed solution. In the present invention, the "oxygenation treatment" can be carried out by any method capable of bringing an oxygen-containing gas into contact with the mixed liquid, for example, by passing an oxygen-containing gas into a flowing or non-flowing mixed liquid, in particular, Oxygen gas is achieved by aeration of the mixture. Aerobic treatment is a typical oxygen treatment. The oxygen treatment can be carried out in any suitable manner under any suitable conditions, for example, under normal pressure, pressure, normal temperature, low temperature and/or elevated temperature conditions, by means of blast aeration, mechanical aeration, jet aeration, etc. Suitable equipment is carried out, for example, in an aeration tank, an oxidation ditch, a fluidized bed, a moving bed or a membrane apparatus. It is preferred to use an aeration tank for aeration. Any suitable oxygen-containing gas can be used for aeration, preferably air aeration. In the oxygen treatment, the dissolved oxygen concentration of the mixture can be gradually increased to a desired value. Oxygen treatment time is generally 099140871 Form No. A0101 Page 20 / Total 79 Page 0993446280-0 201221484 The residence time of the mixture in the oxygen treatment unit (or the time when the mixture is in contact with oxygen) and the oxygen-containing gas that is introduced The amount to determine. Generally, in oxygen treatment, aerobic organisms and facultative organisms are elongated and anaerobic organisms are inhibited. 008 Ο In the present invention, the term "anoxic treatment" means substantially avoiding contact of an oxygen-containing body with a mixed liquid. The anoxic treatment can be carried out by any method capable of substantially avoiding the contact of the oxygen-containing gas with the mixed liquid. This is achieved, for example, by stopping aeration and optionally degassing. In the present invention, regardless of the presence or absence of nitrate nitrogen, as long as there is substantially no dissolved gas, for example, the dissolved oxygen level is less than 0.1 mg/L, it is considered to be in an anoxic state. That is, the anoxic treatment of the present invention can be carried out under the conditions of anoxic conditions (with no dissolved oxygen in the nitrogen) and anaerobic conditions (no dissolved nitrogen in the absence of dissolved nitrogen) as described in some literature. In some cases, the dissolved oxygen concentration may gradually decrease to a desired value with the escape of the gas-containing gas and the consumption of dissolved oxygen, for example, approximately equal to the level of Omg/L. In particular, the anoxic treatment can be achieved by slowing the slow flow of the mixture in the sedimentation tank while stopping the aeration. Suitable sedimentation tanks can be advection, vertical flow and radial flow sedimentation tanks. The time of anoxic treatment is generally determined by the residence time of the mixture in the anoxic treatment unit. Usually, in anoxic treatment, anaerobic organisms and facultative organisms grow, and aerobic organisms are inhibited. In the present invention, the term "amount of sludge" is also referred to as a sludge content, and generally refers to a solid content or a suspended matter content in a sludge or sewage or a mixed liquid or a concentrated mixed liquid. Solids or suspensions typically consist primarily of organisms and organic solids (including biodegradable and biodegradable organic materials). In some cases, the amount of sludge can also be expressed in terms of the total amount of MLSS. MLSS is 099140871 'Form No. A0101 Page 21 / Total 79 Page 0993446280^ 201221484 / «i 〇心心浮固体》 农度 (mixed iiqU〇r SUSpende (js ο 1 ids) shorthand, which is also known as mixed sludge Concentration, which represents the total weight (mg/L) of activated sludge solids contained in the aerated unit unit mixture. [0086] [0087] In one aspect, the present invention provides A sludge treatment method, wherein the sludge is produced in a sewage biological treatment process, the method comprising: (1) mixing a sludge feed with a first mixed liquid to obtain a second mixed liquid; (2) first The mixed solution is subjected to oxygen treatment to obtain a third mixed liquid; (3) the third mixed liquid is subjected to anoxic treatment to obtain a fourth mixed liquid; (4) the fourth mixed liquid is separated from the β liquid and the first; Mixing liquid; (5) discharging the supernatant, returning at least a portion of the first concentrated mixed liquid to the step (1) for use as the first mixed liquid, wherein the amount of sludge of the first concentrated mixed liquid that has not returned to the step (1) is less than that of the contaminated liquid The amount of sludge fed to the mud. The sludge treatment method according to the present invention does not return The amount of the sludge in the first concentrated liquid of the step (1) is smaller than the amount of the sludge inflow, that is, the net amount of the sludge is present. Especially in the case where the first concentrated mixture returns all = (1), the amount of sludge The net input is the amount of sludge fed into the sludge (as shown in Figure 2). The inventors of the invention were surprised to find that in the long run, despite the presence of a net amount of mud, the amount of sludge in the mixture It remains at a relatively stable level without unrestricted growth, which is affected by the composition and flow of the sludge feed and its conditions, such as in the presence of sewage feed, as well as the flow rate of the sewage feed. Therefore, the sludge treatment method of the present invention is a species reduction treatment material. That is, the sludge treatment method of the present invention can digest the sewage form number in the sludge feed 1 帛 22 pages / total 79 Η 201221484 Mud reduction. In the implementation of Wei, the _ sludge treatment method can be used for long-term stable operation without the need for sludge discharge under the continuous addition of the mud feed, thus eliminating sludge discharge. The inventor of the present invention was also surprised to find Even if the sewage has a higher content of I gas and phosphorus 'and discharges any of the first shrinking liquid' supernatant, the nitrogen content can be reduced and cut, that is, the sludge treatment method of the present invention has Significant removal of carbon, nitrogen and phosphorus. [0088] 99 [0090] 099140871 Without any theory, the inventors of the present invention believe that the sludge treatment domain of the present invention operates in a determined manner. The reason why the heart needs to drain the mud may be as follows. Firstly, the amount of sludge in the ready-mixed liquid should continue to increase due to the amount of sludge added by the discharge of the sludge (four), but the sludge concentration of the mixed liquid in the stable operation is It is very high but does not continue to increase but remains stable at a high level (that is to say, the amount of sludge in the system remains basically unchanged during the operation of the helium), so it can be considered that the biological group in the mixture is fading The state of equilibrium, ie the amount of new sludge (including the amount of sludge fed into the sludge and the increase in biological growth in the mixture: the amount of sludge added) and the amount of sludge that has died and digested have reached a dynamic equilibrium, thus No net increase in sludge volume Various methods known biological sewage treatment, since the proliferation of the organism, regardless of whether the secondary clarifier sludge return upstream guard reflux arts, there is surplus sludge discharge. As far as the whole process is concerned, since only the raw sewage of the sewage is fed without the net input of the sludge, the amount of sludge discharged is always larger than the amount of the added sludge. In addition, because the concentration of dissolved organic matter in the effluent of the secondary settling tank must be at the secret level (10), the aeration tank form number Α0101, page 23 / total 79 pages 0993446280-0 201221484 must be high enough for aeration and sufficient Long aeration time to reduce the concentration of dissolved organics in the water. However, under aerobic conditions, low organic concentrations generally favor the proliferation of filamentous bacteria leading to sludge bulking. At the same time, the high aeration and long aeration time further increase the possibility of sludge expansion of the mixture containing the higher concentration of sludge. Therefore, in various known activated sludge processes, the sludge concentration in the aeration tank is often difficult to reach a high level, that is, the growth and balance of the biological group cannot be achieved. In addition, due to the resistance of organisms to harsh environments (such as lower nutrient concentrations), known sludge aerobic treatment methods and sludge anaerobic treatment methods usually only dissolve less than 60% of the sludge (ie, cannot The sludge is completely digested, so the process using these methods still requires a certain amount of excess sludge to be discharged. [0091] In the sludge treatment method of the present invention, since the main purpose is to digest the sludge, the concentration of the dissolved organic matter in the discharged supernatant can be at a high level without limitation, thereby advantageously limiting the filamentous fungus. Proliferation reduces the amount of oxygen required (e.g., aeration), thereby reducing the likelihood of sludge swelling during oxygenation, such as aeration. In addition, the higher level of dissolved organic matter provides enough nutrients for the organism to form an environment conducive to the metabolism, reproduction and programmed death of the organism, so that the organisms in the sludge are also largely degraded while being bulky. . Further, in the sludge treatment method of the present invention, the sludge is subjected to oxygen treatment and anoxic treatment alternately and repeatedly, which is advantageous for the proliferation of the bacteria micelle, and the sedimentation speed and the clarification effect of the sludge are improved. . Therefore, the sludge treatment method of the present invention can achieve high sludge concentration without sludge swelling. 099140871 Form No. A0101 Page 24 / Total 79 Page 0993446280-0 201221484 [0093] In addition, since the first concentrated mixture is usually large or even Returning all of the return '[0094] Step (1) makes the sludge age relatively long (for example, several months, years or even longer), so that microorganisms capable of decomposing refractory substances with a slower reproduction rate can grow normally and enhance the pollution. Decomposition of mud. At the same time, under the condition of high sludge concentration, through the oxygen treatment and the anoxic treatment, the biodegradable substances and the difficult biodegradable substances (including dead organisms) in the mixed liquid are quickly and effectively digested, so that carbon is contained. A compound such as nitrogen or phosphorus is dissolved as a dissolved organic substance which is discharged as a supernatant or becomes a volatile substance. In summary, in the sludge treatment method of the present invention, the sludge in the mixed liquid has excellent sedimentation performance and low oxygen demand (for example, aeration amount) and is capable of degrading various organic substances (including dead organisms). It is made into a water-soluble substance or a gaseous substance, so that the mixed liquid can have a relatively high sludge concentration so that the biological group is in a state of growth and balance without sludge expansion, so that the sludge treatment method of the present invention can be stably operated for a long period of time. To reduce or even completely eliminate sludge emissions. [0095] In some embodiments, the oxygenation treatment of step (2) and the anoxic treatment of step (3) can be carried out in batches in the same structure or vessel. For example, steps (1) to (4) may be carried out in the same structure or vessel, wherein in step (1), a batch of sludge feed is fed to the previous batch of sludge to obtain a first concentrated mixture (as The first mixed liquid is mixed to obtain a second mixed liquid, and in the step (2), the second mixed liquid is subjected to oxygen treatment to obtain a third mixed liquid, and in the step (3), the third mixed liquid is subjected to anoxic treatment to obtain a first mixed liquid. a mixture of four, in step (4), separating the fourth mixture to obtain a supernatant and a first concentrated mixture, in step (5), 099140871 Form No. A0101, page 25 / page 79, 0993446280-0 201221484 and At least a portion (preferably all) of the first-concentration is mixed in the structure or vessel and used as the first-mixing history of step (1) and then the next batch of sewage is fed into the structure or vessel and the above is repeated step. In step (5), the smear can be discharged by discharging the supernatant. The use of renewal methods can be used for both land use and construction investment. In some embodiments, the oxygenation treatment of step (1) and the step (1) (iv) oxygen treatment may be repeated one or more times before the separation of step (4). [0096] In other embodiments, the oxygenation treatment of step (1) and the anoxic treatment of step (3) in the present invention may be carried out in a semi-continuous or continuous manner in different structures or containment. . For example, step (1) i(4) may be semi-continuous in different structures (ie, some steps are run in a continuous mode and some steps are operated in a batch mode) or continuously [wherein the sludge feed is intermittent or in step (1) Continuously arching the human first structure and mixing with the first mixed liquid to obtain a second mixed liquid, and introducing the second mixed liquid intermittently or continuously into the second structure to intermittently or continuously obtain the third mixing by the oxygen supply treatment of the step (1) The liquid mixture is introduced into the third structure intermittently or continuously to intermittently or continuously perform the anoxic treatment of the step (1) to obtain a fourth mixed liquid, and the fourth mixed liquid is subjected to the step (4) intermittently or continuously through the separating device. Separating to obtain a supernatant and a first concentrated mixture, in which the supernatant is intermittently or continuously discharged, at least a portion of the first concentrated mixture is introduced into the first zone intermittently or continuously, and optionally The remainder of the concentrated mixture is discharged intermittently or continuously, wherein the amount of sludge that has not returned to the first concentrated mixture of step (1) is less than the amount of sludge of the sludge feed. First 099140871 Form No. A0101 Page 26 of 79 0993446280-0 201221484 The second and third structures may be separate structures of different structures or different areas of the same structure. If the anoxic treatment of the step (3) is carried out in a precipitation manner, the separation of the step (4) can be carried out simultaneously with the step (3) ❹ [0097] in the same structure (that is, the third structure is also used as a separation device). . In the step (5), the supernatant may be discharged through a device capable of discharging the supernatant, such as a drain pipe, and the first concentrated mixture may be introduced into the first structure through, for example, a sludge return pipe. The efficiency of sludge treatment can be advantageously improved in a semi-continuous or continuous manner. Whether each step is carried out in a batch or continuous manner is mainly determined based on the flow rate and composition of the sludge feed and the operating conditions of the respective equipment, so as to be advantageously optimized and stabilized to obtain an optimum treatment effect. In the sludge treatment method of the present invention, the amount of sludge of the first concentrated mixed liquid which is not returned to the step (1) in the step (5) is smaller than the sludge amount of the sludge feed. In some cases, substantially all of the first concentrated mixture in step (5) is returned to step (1) for use as the first mixture, so that substantially no first concentrated mixture is discharged. However, it is not excluded that in some cases of continuous operation, the amount of sludge of the first concentrated mixed solution discharged temporarily is greater than the amount of sludge of the sludge feed, as long as the first concentrated mixed liquid discharged during long-term operation The average amount of sludge in the remaining portion is smaller than the average amount of sludge in the sludge feed, so that there is a net input of the amount of sludge. According to some embodiments of the sludge treatment method of the present invention, the amount of the sludge of the first concentrated mixture which is not returned to the step (1) in the step (5) is at most the following ratio of the amount of sludge of the sludge feed. One, for example about 95%, about 85%, about 70%, about 50%, about 30%, about 25%, about 20%, about 15%, about 10%, about 5%, about 3%, about 1% , about 0%. The ratio is advantageously about 0%, that is, 099140871 Form No. Α0101, page 27/79, 0993446280-0, 201221484, that is to say that the first concentrated mixture of step (5) is substantially all returned to step (1) as the first A mixture. Moreover, the ratio is particularly advantageously less than about 30%, about 25%, about 20%, about 15%, about 10%, about 5%, about 3%, about 1%, especially about 0% 'in order to obtain longer The age of the mud. Without any theoretical constraints, the longer sludge age allows the slower reproduction of microorganisms that can decompose refractory substances and enhance the decomposition of sludge. At the same time, the ratio of 'shai is less than about 30% 'about 2 5 % 'about 20%, about 15%, about 1 〇% 'about 5 Z 'about 3 % 'about 1% 'especially about 〇%' It is advantageous to increase the sludge concentration of the first, second, third and fourth mixed liquids. ... ......

[0098] [0099] 在一些方案中，第一 it縮混合液的流量可以為污泥進料 流量（在存在污水進料的情況下，為污水進料和污泥進 料的總流量）的1 0 %〜1 0 〇 〇%，例如10〜20 %、2 〇〜3 〇 %、30〜40%、40〜60%、60〜80%、8〇〜100%、 100〜150%、150〜200%、200〜40〇.:私、400〜600% 、600〜800%、800〜1 000%。該比例也稱為第一濃縮 混合液的回流比。合適的回流比有利地使給氧處理時間 和/或缺氧處理時閟為期望值。在一些情況下，合適的回 流比可以較小，例如為10〜2〇%、20〜3〇%、3〇〜4〇% 、40〜60%，以有利地節約動力消耗。在另一些情況下 ，合適的回流比可以較大，例如為6〇〜8〇%、8〇〜1〇〇 %、100〜150%、150〜200%、2〇〇〜400%、400〜 600%、600〜800%、800〜1000%以獲得較短的給氧 處理時間和/或缺氧處理時間。優選的回流比為5〇〜15〇% 〇 在本發明的污泥處理方法的一些實施方案中，步驟（2) 099140871 表單編號A0101 第28頁/共79頁 0993446280Ό 201221484 的給氧處理時間小於好氧微生物成為優勢群類的時間（ 例如小於好氧微生物的世代週期，例如小於約5小時）， 並且步驟（3)的缺氧處理時間小於厭氧微生物成為優勢 群類的時間（例如小於厭氧微生物的世代週期，例如小 於約40小時），從而使得兼性微生物成為優勢群類。不 文任何理論約束，可以認為，由於常溫下兼性微生物的 世代週期約為0. 2〜0. 5小時，以兼性微生物為優勢群類 的污泥在經歷交替的給氧處理（好氧條件）和缺氧處理 ❹ (缺氧條件和/或厭氧條件）時將會發生大量的生物增殖 和生物程式死亡，從而大量消化和降解（主要包括代謝 和水解）各«機物質（包括死亡生物）使其成為溶解 性化合物而隨上清液排出或成為氣態化合物而逸出，這 在高污泥濃度條件下尤其明顯。[0099] In some aspects, the flow rate of the first iteration mixture may be the sludge feed flow rate (in the case of the presence of the sewage feed, the total flow rate of the sewage feed and the sludge feed) 10%~1 0 〇〇%, for example 10~20%, 2 〇~3 〇%, 30~40%, 40~60%, 60~80%, 8〇~100%, 100~150%, 150 ~200%, 200~40〇.: private, 400~600%, 600~800%, 800~1 000%. This ratio is also referred to as the reflux ratio of the first concentrated mixture. A suitable reflux ratio advantageously provides the desired value for the oxygen treatment time and/or the anoxic treatment. In some cases, a suitable reflux ratio may be small, for example, 10 to 2%, 20 to 3%, 3 to 4%, 40 to 60% to advantageously save power consumption. In other cases, a suitable reflux ratio may be large, for example, 6〇~8〇%, 8〇~1〇〇%, 100~150%, 150~200%, 2〇〇~400%, 400~ 600%, 600 to 800%, 800 to 1000% to obtain a shorter oxygen treatment time and/or an anoxic treatment time. Preferably, the reflux ratio is 5 〇 15% 〇 〇 In some embodiments of the sludge treatment method of the present invention, step (2) 099140871 Form No. A0101 Page 28 / Total 79 Page 0993446280 Ό 201221484 The oxygen treatment time is less than good The time during which the oxygen microorganisms become dominant groups (eg, less than the generation period of aerobic microorganisms, eg, less than about 5 hours), and the anoxic treatment time of step (3) is less than the time during which the anaerobic microorganisms become dominant groups (eg, less than anaerobic) The generational cycle of microorganisms, for example less than about 40 hours, makes facultative microorganisms a dominant group. Without any theoretical constraints, it can be considered that the generation period of facultative microorganisms at room temperature is about 0. 2~0. 5 hours, the sludge with facultative microorganisms as the dominant group undergoes alternating oxygen treatment (aerobic Conditions) and anoxic treatment of ❹ (hypoxic conditions and / or anaerobic conditions) will occur a large number of biological proliferation and biological death, resulting in a large number of digestion and degradation (mainly including metabolism and hydrolysis) of various substances (including death) Biological) It becomes a soluble compound and escapes as the supernatant is discharged or becomes a gaseous compound, which is particularly noticeable under high sludge concentration conditions.

[0100] G 在-些實施方案中，步驟⑴的給氧處理時間可以小於 例如5小時以免好氧微生物成為優勢群類，同時還可以大 於例如0. 1小時以使兼錄生物得収細增殖並充分抑 制厭氧微生物的增殖，從而”地使紐In an embodiment, the oxygenation treatment time of the step (1) may be less than, for example, 5 hours to prevent the aerobic microorganisms from becoming a dominant group, and may also be greater than, for example, 0.1 hour to allow the recorded organism to receive fine proliferation. And fully inhibit the proliferation of anaerobic microorganisms, thus

勢群類。在-些情形中，給氧處理時間可以為;;H 時，優選0· 5〜2小時， 0.1〜0.2小時、0.2〜 更優選0 · 5〜1 5 <1、b4 / 3』、時，例如選自 〇.3小時、〇.3〜〇.4小時、04、 " υ · 〇 〜1 小 、卜1·2小時、1·2〜1·5小時、h5〜18小時、i 8 2小時、2〜2. 2小時、2. 2〜2.5小時、2 5〜3小時和 3.5〜4小時。在-些實施方案中，步驟⑴的給氧處理 以間歇或連續方式進行’例如以，曝氣或連續曝氣的 099140871 表單編號A0101 第29頁/共79頁 0993446280-0 201221484 方式進行β [0101] [0102] 在-些實施方案中’步驟（3 )的缺氧處理時間可以小於 例如6小時以免厭氧微生物成為優勢群類並有利於減小裝 置尺寸’同時還可以大於例如時以使兼性微生物得 到足夠的增殖並充分抑制好氧微生物的增殖，從而使兼 性微生物成為優勢群類》缺氧處理時間可以為〇. 8〜6小 時’優選1〜4小時’更優選卜3小時，例如選自um 小時、1〜1.2小時、1.2〜1.4小時、6小時、 1. 6〜1. 8小時、1. 8〜2小時、2〜2· 5小時、2. 5〜3小 時、3〜3· 5小時' 3. 5&4小時、4〜4. 5小時、4. 5〜5 小時、5〜5. 5小時和5. 5〜6小時。在一些實施方案中， 步驟（3)的缺氧處理可以沉澱方式進行。在缺氧處理以 沉澱方式進行時，缺氧處理時間有利地大於〇. 5小時，特 別有利地大於1小時以使沉澱充分完成，同時有利地小於 4小時以減小裝置尺寸。 ·：,,,.： 在一些實施方案中’給氧處理時間與缺氡處理時間的比 為1:0. 5〜1:6，優選1:1〜1:3，更優選1:1 5〜1:2， 最優選^’例如選自^^〜^^^^〜^.?、 1:0.7 〜1.0.8、1:〇.8 〜ΐ:〇·9、1:0.9 〜1:1、1:1 〜 1:1.1、1:1.1〜1:1.2、1:1.2〜1:1.3、1:1.3〜 1:1.4、1:1.4 〜1:1.5、1:1.5 〜1:1.6、1:1.6 〜 1:1.7、1:1.7〜1:1.8' 1:1.8〜1:1.9、1:1.9〜1:2 、1:2〜1:2. 1、1:2.1〜1:2.2、1:2.3〜1:2.4、 1:2.4〜1:2.5、1:2.5〜1:2.6、1:2.6〜1:2.8、 1:2.8 〜1:3、1:3 〜1:3.2、1:3.2〜1·· 3.4、1:3.4 〜 099140871 表單編號A0101 第30頁/共79頁 0993446280-0 201221484 1:3.6、1:3.6〜1:3.8、1:3.8〜1:4、1:4〜1:4.5、 1:4. 5〜1:5、1:5〜1:5. 5和1:5. 5〜1:6 ’以有利地使 兼性微生物成為優勢群類。 [0103] 在一些實施方案中，為使污泥經歷足夠的給氧處理以便 有利地使兼性微生物成為優勢群類並促進污泥的消化和 水解’步驟（2)的第三混合液的溶解氧濃度可以為〇. 1 〜4mg/L ’優選1，5〜3mg/L ’更優選2〜3mg/L，例如選 自 0.1〜0. 3mg/L、〇·3〜0. 5mg/L、0.5〜0. 7mg/L、 Ο 0.7〜0. 9mg/L、0. 9〜1. lmg/L、1.1〜1.3mg/L、1 3 〜1. 5mg/L、1. 5〜l' 7mg/t、1· 7〜1. 9mg/L、1. 9〜 2.lmg/L、2.1〜2. 3mg/L、2.3〜2· 5mg/L·、2. 5〜 2.7mg/L、2.7〜2. 9mg/L、2. 9〜3. lmg/L ' 3. 1〜 3.3mg/L、3.3〜3. 5mg/L、3. 5〜3. 7mg/L和3. 7〜 3.9mg/L 。 [0104] Ο 在一些實施方案中，在步驟（1),之前將污泥進料進行給 氧處理^不受任何理論的限制，可q認為這樣更有利於 使兼性微生物成為優勢群類。此外，當污泥進料來自活 性污泥工藝的二沉池時，由於污泥進料中的有機物含量 相當低，污泥進料中的生物在給氧處理時將主要發生内 源消化從而減小了污泥量。同時，這樣的給氧處理也可 以減輕步驟⑴的給氧處理的需氧量（例如曝氣量）， 進-步減少第-區發生污泥膨脹的可能性^在—些實施 方案中，污泥進料給氧處理的時間可以為Μ 5小時 、〇.5〜1小時、1〜h5小時、1.5〜2小時和2〜2.5小 時，處理後污泥進料的溶解氧濃度選自〇. !〜〇 5mg/L、 099140871 表單編號A0101 第31頁/共79頁 0993446280-0 201221484 二.5mg/L、2. 5〜3rag/L、3〜3, 5軌和3」〜4嗔。 —些實施方案t，這樣的給氧處理以間歇或連續方式 進仃，例如以間歇或連續曝氣的方式進行。 [0105] [0106] Γ% 在-些實施方案中，為使污泥經歷充分的缺氧處理以便 有利地使紐微生物成為優勢群類並促進污泥的消化和 水解，在步驟⑴#(3)之間可以對第三混合液進行 去乳處理。例如，可用脫氣池進行去氧處理，其中混合 液中的含氧氣泡上浮’從而'使混合液的溶解氧含量不再 增長，為隨後的缺氧處理做好準備。在_本發明的污 泥處理方法的-些實施方案中，去氧處理的時間可以為 〇.1〜〇.2小時、0.2〜0.3小時、〇3〜〇.5小時、〇} 〇.8小時和"叫小時’處理後的第三混合液的溶解氧; 度選自小於0. lmg/L，小於0. 〇5mg/L和約〇mg/L。 在—些實施方案中，給氧處理時間：去氧處理時間：缺 氧處理時間的比例可以為1: : (〇 5〜4) ，優選1: (0.1〜0.3) : (1丨〜3):，更優選為1: (〇」 〜0.2) : (1.5〜2.5)，例如優選為ι:0.1:1或 1:0.15:2。 [0107] 在一些實施方案中，在本發明的污泥處理方法中，污泥 進料可以是一股或多股污泥進料，優選新鮮污泥進料， 各股污泥進料可以相同或不同。通常，污泥進料的含水 率例如為至少40%，至少60%，至少80%，至少9〇%，至 少95%，至少98%或更高，優選97%或更高。在一些情況 下’污泥進料也可以是幹污泥等低含水量污泥及其與水 099140871 表單編號A0101 第32頁/共79頁 0993446280-0 201221484 [0108] K有機營養物或其他污泥進料的混合物。 2據本發明的巧泥處理方法的一些實施方案，步驟⑴ 還L括將5水轉狀第—混合液。在存在污水進料的 凊形中，步驟⑴中污泥進料與污水進料的流量比可以 選自 1:100 〜1:5〇、1:50〜1:20、1:2〇〜1:1〇、1:1〇 15 1-5〜1:2、1:2〜1:1.5、1:1. 5〜1:1、1:1 〜 18、1:〇.8〜1:0. 5 ' 1:〇·5〜1:0.2、1:〇·2〜 1·〇·1 〜1:0.、1:〇·〇5〜1:0.02和 1:〇,〇2 〇 [0109] 〜1 : 0, 01。 在一些實施方案中，步驟⑴中第二混合液的污泥體積 才曰數（SVI ’常用SVI30表示,，指混合-液在印⑽此量筒中 靜置30分鐘以後，1克活性污泥懸:浮固辕辦友的體積，單 位為mL/g)應當小於給氧處理時發生污泥膨脹的最小值 。根據本發明的污泥處理方法的一些實施方案，污泥體 積才曰數例如SVI30可以小於|.3〇::〇in..l/g，小，於200ml/g，小 於 150ml/g ’ 小於i〇〇mi/g，，或小於5〇ml/g。 ^ [0110] 在一些實施方案中’步驟（1)申第二混合液的污泥濃度 可以為使生物處於消長平衡狀態時的濃度。根據一些實 施方案’在步驟（1 )中第二混合液的污泥濃度為至少約 2500〜3000mg/L 、 3000〜3500mg/L 、 3500〜 4000mg/L、4000〜4500mg/L、4500〜5000mg/L、 5000〜5500mg/L 、 5500〜6000mg/L 、 6000〜 6500mg/L 、 6500〜7000mg/L 、 7000〜7500mg/L 、 7500〜8000mg/L 、 8000〜8500mg/L 、 8500〜 9000mg/L 、 9000〜9500mg/L 、 9500〜10000mg/L 、 099140871 表單編號A0101 第33頁/共79頁 0993446280-0 201221484 10000〜12000mg/L 、 12000〜14000mg/L 、 14000〜 16000mg/L 、 16000〜18000mg/L 、 18000〜20000mg/L 和至少約20000mg/L，優選3000〜20000mg/L，更優選 4000〜1 5000mg/L。 [0111] 在一些實施方案中，上述污泥處理方法還包括回收氣態 含磷化合物的回收步驟。氣態含磷化合物包括步驟（2) 和/或步驟（3)中產生的磷化氫等。例如，該回收步驟 可以與步驟（2)和/或步驟（3)同時進行以回收步驟（ 2)和/或步驟（3)中產生的氣態含磷化合物。該回收步 驟可以是任何合適的回收氣態含磷混合物的方法，例如 可以是能夠將氣態含磷物質轉化為液態或固態物質的方 法，例如可以通過冷凍或者通過用能夠物理和/或化學吸 附氣態含磷物質的吸收劑的吸收、沖洗或吸附來進行該 回收步驟。所述吸收劑可以是能夠溶解該氣態含磷化合 物的物質或能夠與該氣態含磷化合物反應的物質。例如 ，能夠吸收磷化氫氣體的物質包括例如高錳酸鉀溶液、 高錳酸鉀和苛性鹼的混合溶液、氣化鐵溶液、次溴酸鈉 溶液等。對於磷化氫，還可用活性碳等吸附劑吸附，或 用臭氧氧化成低毒物或者在嚴格控制下燃燒等方式進行 回收。 [0112] 在另一方面，本發明還提供一種污水生物處理方法，包 括 [0113] ( 1 )將污泥進料與第一混合液混合得到第二混合液； [0114] ( 2 )將第二混合液進行給氧處理得到第三混合液； 099140871 表單編號A0101 第34頁/共79頁 0993446280-0 201221484 [0115] ( 3 )將第三混合液進行缺氧處理得到第四混合液； [0116] (4)將第四混合液分離得到上清液和第一濃縮混合液； . [0117] (5)將上清液排出；將至少部分第一濃縮混合液返回步 驟（1)用作第一混合液，其中未返回步驟（1)的第一 濃縮混合液的污泥量小於污泥進料的污泥量； [0118] (6)將至少部分步驟（5)的上清液進行污水生物處理 得到第二濃縮混合液和淨化出水； 〇 剛 (7)將淨化出水排出；以及任選地將至少部分步驟（6 )的第二濃縮混合液返回步驟（1 )用作污泥進料； [0120] 其中將污水進料引入步驟（1)與污泥進料和第一混合液 混合得到第二混合液和/或引入步驟（6)中與所述至少 部分步驟（5)的上清液一起進行污水生物處理。 [0121] ❹ 可見步驟（1)至（5)組成了前述本發明的污泥處理方 法。因此，本發明的污水生物處理方法實際上是前述本 發明的污泥處理方法在污水生物處理中的應用。由於本 發明的污泥處理方法中排出的上清液通常仍含有較高濃 度的可溶性有機污染物，該上清液通常需要進一步處理 才能達到環境安全的排放標準。因此，在一些實施方案 中，污水進料引入步驟（1)，由此步驟（1 )至（5)形 成的本發明的污泥處理方法可以作為一級生物處理步驟 置於作為二級生物處理的步驟（6)的污水生物處理之前 ，污水進料先經過該一級生物處理得到上清液，然後上 清液作為進料經二級生物處理得到淨化出水。優選該淨 化出水是環境安全的，符合通常的排放標準。同時，二 099140871 表單編號A0101 第35頁/共79頁 0993446280-0 201221484 級生物處理中產生的剩餘污泥（即：第二濃縮混合液） 可以作為污泥進料在―級生物處理中得到消解，從而有 利地減少甚至避免整個污水生物處理中的污泥排放。在 另一些實施方案中，污水進料由步驟⑻引人由此從 5水進料的角度來看，步驟⑴i (5)形成的本發明 的污泥處理方法置於步驟⑷的污水生物處理之後，主 要用於消解步驟⑷的污水生物處理中產生的剩餘污泥 (即·第二濃縮混合液）。同時，步驟（5)的上清液也 可以作為污水進料引人步驟⑴。在再另—些實施方案 中，污水進料也可以同時引入步驟(1)和步驟（6)。 [0122] 在一些實施方案中，可以將步驟（6)的第二濃縮混合液 的 1 〜10%、1〇〜20%、20〜30%、30〜4勝、40〜50%、 50〜60%、60〜70%、70〜80%、80〜85%、85〜90%、 9〇〜95%或95〜1〇〇% ,特別有利地是基本上1〇〇%用作步 驟（1 )的污泥進料，以便有利地利用上述污泥處理方法 . .. .: .V. 將第二濃縮混合液部分地甚至基本上完全消解，從而使 整個污水生物處理方法排出的污泥減少甚至基本上完全 消除。在一些實施方案中，來自步驟（6)的第二濃縮混 合液占步驟（1 )的污泥進料的比例為1〜1〇%、1〇〜2〇% 、20〜30%、30〜40%、40〜50%、50〜60%、60〜70% 、70〜80%、80〜85%、85〜90%、90〜95%或95〜1〇〇% 〇 根據本發明的污水生物處理方法，前述本發明的污泥處 理方法作為第一生物處理步驟可以與任何適合作為第二 生物處理步驟的污水生物處理方法結合。與單獨採用作 099140871 表單編號A0101 第36頁/共79頁 0993446280-0 [0123] 201221484 為第二生物處理步驟的污水生物處理方法時相比，本發 月的污水生物處理方法顯著減少甚至完全消除了剩餘污 泥的排放，同時獲得了良好的處理效果。 []在本發明的污水生物處理方法中，如果污水進料在步驟 (1 )和步驟（6 )中同時引入，引入步驟（1 )的污水進 料與引入步驟（6)的污水進料的比例可以根據需要任意 選擇，以有利地平衡系統的負荷，優化整個污水生物處 理方法的效果。 Ο [〇125]在一些實施方案中，特別有利地在步驟（1)中將污水進 料引入。由於步驟（1 )的混合液具有恨高的污泥濃度， 可以有利地對抗污水進料的水量和污染物等方面的衝擊 負荷，同時高濃度的污泥也可以加快反應速度使污水進 _ 料中的污染物在高濃度污泥作用下高效、快速消解，一 些難降解物質也可在第一生物處理步驟中逐漸降解為易 降解物質，從而有利於改善汙水處理效果、縮小整個汙 水處理襞置的體積、節約巧地、減少設備投資和運轉費 〇 用。這一點對c〇I)通常較低的;污水，例如城市生活污水的 處理尤其有利，因為步驟（1)至組成的污泥處理 過程實際上將部分污泥進料轉化為易降解的物質從而適 當增加了上清液中的C0D濃度，使得後續針對上清液進行 生物處理的過程能夠更加有效地去除水中的鱗和氮，從 . 而提尚淨化出水的品質。因此，本發明特別適合於C0D值Potential group. In some cases, the oxygen treatment time may be:; H, preferably 0·5 to 2 hours, 0.1 to 0.2 hours, 0.2 to more preferably 0·5 to 1 5 <1, b4 / 3, For example, from 〇.3 hours, 〇.3~〇.4 hours, 04, " υ · 〇~1 small, Bu 1·2 hours, 1·2~1·5 hours, h5~18 hours, i 8 2 hours, 2 to 2. 2 hours, 2. 2 to 2.5 hours, 2 5 to 3 hours, and 3.5 to 4 hours. In some embodiments, the oxygenation treatment of step (1) is carried out in a batch or continuous manner, for example, by aeration or continuous aeration of 099140871 Form No. A0101 Page 29 / Total 79 Page 0993446280-0 201221484. [0102] In some embodiments, the hypoxic treatment time of step (3) may be less than, for example, 6 hours to prevent anaerobic microorganisms from becoming a dominant group and to facilitate reducing the size of the device while also being greater than, for example, Sexual microorganisms get enough proliferation and fully inhibit the proliferation of aerobic microorganisms, so that facultative microorganisms become dominant groups. The hypoxic treatment time can be 〇. 8~6 hours 'preferably 1~4 hours' is more preferably 3 hours, For example, it is selected from um hours, 1 to 1.2 hours, 1.2 to 1.4 hours, 6 hours, 1. 6 to 1. 8 hours, 1. 8 to 2 hours, 2 to 2 hours, 5 hours, 2. 5 to 3 hours, 3 〜5·5小时的。。。。。。。。。。。。。。。。。。。。。。。。。。。。 In some embodiments, the anoxic treatment of step (3) can be carried out in a precipitation mode. When the anoxic treatment is carried out in a precipitation mode, the anoxic treatment time is advantageously greater than 0.5 hours, particularly advantageously greater than one hour to allow the precipitation to be fully completed, while advantageously less than 4 hours to reduce the size of the apparatus. The ratio of the oxygen treatment time to the defect treatment time is 1:0. 5~1:6, preferably 1:1 to 1:3, more preferably 1:1 5 in some embodiments. ~1:2, most preferably ^' is selected, for example, from ^^~^^^^~^.?, 1:0.7 to 1.0.8, 1: 〇.8 ΐ: 〇·9, 1:0.9 〜1: 1, 1:1 ~ 1:1.1, 1:1.1~1:1.2, 1:1.2~1:1.3, 1:1.3~11.4, 1:1.4~1:1.5, 1:1.5~1:1.6, 1:1.6 ~ 1:1.7, 1:1.7~1:1.8' 1:1.8~1:1.9, 1:1.9~1:2, 1:2~1:2. 1, 1:2.1~1:2.2, 1:2.3~1:2.4, 1:2.4~1:2.5, 1:2.5~1:2.6, 1:2.6~1:2.8, 1:2.8~1:3, 1:3~1:3.2, 1: 3.2~1·· 3.4, 1:3.4~ 099140871 Form No. A0101 Page 30/79 Page 0993446280-0 201221484 1:3.6, 1:3.6~1:3.8, 1:3.8~1:4, 1:4~ 1:4.5, 1:4. 5~1:5, 1:5~1:5. 5 and 1:5. 5~1:6 ' advantageously to make facultative microorganisms a dominant group. [0103] In some embodiments, the sludge is subjected to sufficient oxygen treatment to advantageously make the facultative microorganisms a dominant group and promote digestion and hydrolysis of the sludge 'the dissolution of the third mixture of step (2) 5 mg/L, mg·3~0. 5mg/L,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,, 5〜l' 7mg, 0.5mg/L, Ο 0.7~0. 9mg/L, 0. 9~1. lmg/L, 1.1~1.3mg/L, 1 3~1. 5mg/L, 1. 5~l' 7mg /t, 1·7~1. 9mg/L, 1. 9~ 2.lmg/L, 2.1~2. 3mg/L, 2.3~2·5mg/L·, 2. 5~ 2.7mg/L, 2.7 〜2. 9〜3. 3〜3. 〜3. 3~3. /L. [0104] In some embodiments, prior to step (1), the sludge feed is subjected to oxygen treatment without any theoretical limitation, which may be considered to be more advantageous for making the facultative microorganisms a dominant group. In addition, when the sludge feed comes from the secondary settling tank of the activated sludge process, since the organic matter content in the sludge feed is relatively low, the organisms in the sludge feed will mainly undergo endogenous digestion during the oxygen treatment. Small amount of sludge. At the same time, such oxygen supply treatment can also reduce the oxygen demand (for example, aeration amount) of the oxygen supply treatment in the step (1), and further reduce the possibility of sludge expansion in the first region. In some embodiments, the sewage treatment The time for the oxygen feed treatment of the sludge feed may be Μ5 hours, 〇5~1 hour, 1~h5 hours, 1.5~2 hours, and 2~2.5 hours, and the dissolved oxygen concentration of the sludge feed after treatment is selected from 〇. !~〇5mg/L, 099140871 Form No. A0101 Page 31/Total 79 Page 0993446280-0 201221484 Two.5mg/L, 2. 5~3rag/L, 3~3, 5 tracks and 3"~4嗔. In some embodiments t, such oxygenation is carried out in a batch or continuous manner, for example in batch or continuous aeration. [0106] Γ% In some embodiments, in order to subject the sludge to a sufficient anoxic treatment to advantageously make the New Zealand microorganisms a dominant group and promote digestion and hydrolysis of the sludge, in step (1) #(3) The third mixture can be de-milked between. For example, degassing can be carried out using a degassing tank in which the oxygen-containing gas bubbles in the mixture are floated 'so that' the dissolved oxygen content of the mixture is no longer increased, ready for subsequent anoxic treatment. In some embodiments of the sludge treatment method of the present invention, the deoxidation treatment time may be 〇.1~〇.2 hours, 0.2~0.3 hours, 〇3~〇.5 hours, 〇} 〇.8 The hourly and "hours' treated third mixture of dissolved oxygen; the degree is selected from less than 0.1 mg/L, less than 0. 〇5 mg/L and about 〇mg/L. In some embodiments, the oxygen treatment time: deoxygenation time: the ratio of the anoxic treatment time may be 1: (〇5~4), preferably 1: (0.1~0.3): (1丨~3) More preferably, it is 1: (〇) ～0.2) : (1.5 to 2.5), for example, preferably ι: 0.1:1 or 1:0.15:2. [0107] In some embodiments, in the sludge treatment method of the present invention, the sludge feed may be one or more sludge feeds, preferably fresh sludge feed, and each sludge feed may be the same Or different. Typically, the sludge feed has a moisture content of, for example, at least 40%, at least 60%, at least 80%, at least 9%, at least 95%, at least 98% or higher, preferably 97% or higher. In some cases, the sludge feed can also be a low-water sludge such as dry sludge and its water with water 099140871 Form No. A0101 Page 32 / Total 79 Page 0993446280-0 201221484 [0108] K Organic nutrients or other pollution a mixture of mud feeds. 2. According to some embodiments of the inventive method of treating mud, step (1) further comprises converting the 5 water to the first mixture. In the shape of the sewage feed, the flow ratio of the sludge feed to the sewage feed in the step (1) may be selected from 1:100 to 1:5 〇, 1:50 to 1:20, 1:2 〇~1. :1〇, 1:1〇15 1-5~1:2, 1:2~1:1.5, 1:1. 5~1:1, 1:1~18, 1: 〇.8~1:0 5 ' 1:〇·5~1:0.2, 1: 〇·2~ 1·〇·1 ～1:0., 1: 〇·〇5~1: 0.02 and 1: 〇, 〇2 〇[0109 ] ~1 : 0, 01. In some embodiments, the sludge volume of the second mixture in step (1) is only the number of turns (SVI 'usually represented by SVI30, meaning that the mixture-liquid is allowed to stand in the cylinder for 10 minutes after printing (10), 1 gram of activated sludge suspension The volume of the floating solids, in mL/g, should be less than the minimum value of sludge expansion during oxygen treatment. According to some embodiments of the sludge treatment method of the present invention, the sludge volume number, for example, SVI30, may be less than |.3〇::〇in..l/g, small, at 200 ml/g, less than 150 ml/g 'less than I〇〇mi/g, or less than 5〇ml/g. [0110] In some embodiments, step (1) suggests that the sludge concentration of the second mixture may be the concentration at which the organism is in a growth and equilibrium state. According to some embodiments, the sludge concentration of the second mixture in step (1) is at least about 2500~3000mg/L, 3000~3500mg/L, 3500~4000mg/L, 4000~4500mg/L, 4500~5000mg/ L, 5000~5500mg/L, 5500~6000mg/L, 6000~6500mg/L, 6500~7000mg/L, 7000~7500mg/L, 7500~8000mg/L, 8000~8500mg/L, 8500~ 9000mg/L, 9000~9500mg/L, 9500~10000mg/L, 099140871 Form No. A0101 Page 33/Total 79 Page 0993446280-0 201221484 10000~12000mg/L, 12000~14000mg/L, 14000~16000mg/L, 16000~18000mg/L 18000 to 20000 mg/L and at least about 20,000 mg/L, preferably 3,000 to 20,000 mg/L, more preferably 4000 to 15,000 mg/L. [0111] In some embodiments, the sludge treatment method described above further includes a recovery step of recovering the gaseous phosphorus-containing compound. The gaseous phosphorus-containing compound includes the phosphine produced in the step (2) and/or the step (3), and the like. For example, the recovery step can be carried out simultaneously with step (2) and/or step (3) to recover the gaseous phosphorus-containing compound produced in step (2) and/or step (3). The recovery step can be any suitable method for recovering a gaseous phosphorus-containing mixture, for example, a method capable of converting a gaseous phosphorus-containing material into a liquid or solid material, for example, by freezing or by being capable of physically and/or chemically adsorbing a gaseous state. This recovery step is carried out by absorption, rinsing or adsorption of the absorbent of the phosphorus species. The absorbent may be a substance capable of dissolving the gaseous phosphorus-containing compound or a substance capable of reacting with the gaseous phosphorus-containing compound. For example, substances capable of absorbing phosphine gas include, for example, a potassium permanganate solution, a mixed solution of potassium permanganate and caustic, a gasified iron solution, a sodium hypobromite solution, and the like. For phosphine, it can also be adsorbed by an adsorbent such as activated carbon, or oxidized to low toxicity by ozone or burned under strict control. [0112] In another aspect, the present invention also provides a biological treatment method for sewage, comprising [0113] (1) mixing a sludge feed with a first mixed liquid to obtain a second mixed liquid; [0114] (2) The second mixed solution is subjected to oxygen treatment to obtain a third mixed liquid; 099140871 Form No. A0101 Page 34 / Total 79 Page 0993446280-0 201221484 [0115] (3) The third mixed liquid is subjected to anoxic treatment to obtain a fourth mixed liquid; 0116] (4) separating the fourth mixed liquid to obtain a supernatant liquid and a first concentrated mixed liquid; [0117] (5) discharging the supernatant; returning at least a portion of the first concentrated mixed liquid to the step (1) for use as a first mixed liquid in which the amount of sludge of the first concentrated mixed liquid not returned to the step (1) is smaller than the amount of sludge of the sludge feed; [0118] (6) at least a part of the supernatant of the step (5) is carried out Biological treatment of sewage to obtain a second concentrated mixture and purified water; 〇Gang (7) discharges the purified effluent; and optionally returns at least part of the second concentrated mixture of step (6) to step (1) for use as sludge [0120] wherein the sewage feed is introduced into the step (1) with the sludge feed and the first mixture Biological sewage treatment with the supernatant obtained by mixing the second mixture and / or introduced in step (6) with at least part of step (5). [0121] It can be seen that the steps (1) to (5) constitute the sludge treatment method of the present invention described above. Therefore, the sewage biological treatment method of the present invention is actually the application of the aforementioned sludge treatment method of the present invention in sewage biological treatment. Since the supernatant discharged from the sludge treatment method of the present invention usually still contains a relatively high concentration of soluble organic pollutants, the supernatant usually requires further treatment to achieve environmentally safe discharge standards. Therefore, in some embodiments, the sewage feed is introduced into step (1), whereby the sludge treatment method of the present invention formed by steps (1) to (5) can be placed as a primary biological treatment step as a secondary biological treatment. Before the biological treatment of the sewage in step (6), the sewage feed is first treated by the primary biological treatment to obtain a supernatant, and then the supernatant is used as a feed to obtain purified water by secondary biological treatment. Preferably, the purified effluent is environmentally safe and meets normal emission standards. At the same time, two 099140871 Form No. A0101 Page 35 / Total 79 Page 0993446280-0 201221484 The excess sludge produced in the biological treatment (ie: the second concentrated mixture) can be digested as a sludge feed in the level biological treatment. Thereby advantageously reducing or even avoiding sludge discharge throughout the biological treatment of sewage. In other embodiments, the sewage feed is introduced from step (8) from the point of view of the 5 water feed, and the sludge treatment method of the present invention formed in step (1) i (5) is placed after the biological treatment of sewage in step (4) It is mainly used to digest the excess sludge (ie, the second concentrated mixture) generated in the biological treatment of sewage in the step (4). At the same time, the supernatant of step (5) can also be used as a sewage feed introduction step (1). In still other embodiments, the sewage feed can also be introduced simultaneously to steps (1) and (6). [0122] In some embodiments, 1 to 10%, 1 to 20%, 20 to 30%, 30 to 4, 40 to 50%, 50~ of the second concentrated mixture of the step (6) may be used. 60%, 60 to 70%, 70 to 80%, 80 to 85%, 85 to 90%, 9 to 95% or 95 to 1%, particularly advantageously substantially 1% for use as a step ( 1) sludge feed to advantageously utilize the sludge treatment method described above. . . . . . . . V. Partially or even substantially completely digest the second concentrated mixture, thereby allowing the sludge discharged from the entire sewage biological treatment method Reduce or even completely eliminate it. In some embodiments, the second concentrated mixture from step (6) comprises from 1 to 1%, 1% to 2%, 20% to 30%, 30% of the sludge feed of step (1). 40%, 40 to 50%, 50 to 60%, 60 to 70%, 70 to 80%, 80 to 85%, 85 to 90%, 90 to 95% or 95 to 1% by weight 〇 sewage according to the present invention The biological treatment method, the aforementioned sludge treatment method of the present invention as a first biological treatment step can be combined with any sewage biological treatment method suitable as a second biological treatment step. Used alone as 099140871 Form No. A0101 Page 36 / Total 79 Page 0993446280-0 [0123] 201221484 Compared with the sewage biological treatment method of the second biological treatment step, the sewage biological treatment method of this month is significantly reduced or even completely eliminated. The discharge of excess sludge was obtained and a good treatment effect was obtained. [] In the sewage biological treatment method of the present invention, if the sewage feed is simultaneously introduced in the step (1) and the step (6), the sewage feed of the step (1) and the sewage feed of the introduction step (6) are introduced. The ratio can be arbitrarily selected as needed to advantageously balance the load of the system and optimize the effectiveness of the overall biological treatment of sewage. Ο [〇125] In some embodiments, it is particularly advantageous to introduce the sewage feed in step (1). Since the mixture of the step (1) has a high sludge concentration, it can advantageously resist the impact load of the sewage feed water and pollutants, and the high concentration sludge can also accelerate the reaction speed to make the sewage feed into the feed. The pollutants in the high-concentration sludge are efficiently and rapidly digested, and some refractory substances can be gradually degraded into easily degradable substances in the first biological treatment step, thereby improving the sewage treatment effect and reducing the overall sewage treatment. The size, cost savings, equipment investment and operating costs of the device are reduced. This is generally lower for c〇I); the treatment of sewage, such as municipal sewage, is particularly advantageous because the sludge treatment process of step (1) to the actual conversion of part of the sludge feed into readily degradable material The concentration of COD in the supernatant is appropriately increased, so that the subsequent biological treatment of the supernatant can more effectively remove the scale and nitrogen in the water, thereby improving the quality of the purified water. Therefore, the present invention is particularly suitable for C0D values.

低於500mg/L，低於350mg/L，低於30〇mg/L，低於 250mg/L ’ 低於200mg/L，低於 150mg/L或低於i〇〇mg/L 的污水進行污水生物處理。當然，在污水進料中各種污 099140871 表單編號A0101 第37頁/共79頁 0993446280-0 201221484 染物的比例不平衡而導致碳源缺乏時 ，也可以在在污水 進料中補充合適的碳源，例如_例如甲醇和其他有機 營養物例如澱粉、糖蜜等。 [0126] [0127] 根據本發明的污水生物處理方法可轉別㈣地將任何 排出剩餘污泥的污水生物處理方法（例如各種常規的好 氧污水生物處理方法和厭氧污水生物處理方法） 作為步 驟（6)的污水生物處理步驟。在一些實施方案中，步驟 (6)的污水生物處理步驟可以是根據wuhrmann工藝、 A 0 « Bardenpho工藝、ph〇red〇x工藝、A2/〇工藝 、倒置A2/0工藝、11(^工藝、MUCT工藝、νιρ工藝、 0MSA工藝、JHB工藝、TNCU工藝、Dephan〇x工藝、 BCFS工藝、MSBR工藝、SBR工藝、AB工藝、氧化溝工藝 、生物膜工藝、流動床工藝或其組合的污水生物處理步 驟。 第3圖示出根據本發明污水生物處理方法的一些實施方案 的工藝流程的示意圖，其中“進水”代表污水進料，“ 污泥消解裝置”代表能夠進行根據本發明的污泥處理方 法（即步驟（1)至（5))的裝置，“常規汙水處理裝 置代表能夠進行步驟（6)的污水生物生物處理步驟的 任意合適的汙水處理裝置，“出水”代表淨化出水，“ 剩餘污泥回流代表用作步驟（1 )的’污泥進料的第_ '農 縮混合液。 第4圖示出根據本發明污水生物處理方法的另一些實施方 案的工藝流程的示意圖，其中各個術語與第3圖中術語的 意思相同’而污泥”代表另一來源的污泥進料。 099140871 表單編號A0101 第38頁/共79頁 0993446280-0 [0128] 201221484 [0129] [0130] Ο [0131] Ο [0132] 第5圖為傳統氧化溝汙水處理工藝流程圖^。該工藝可以作 為本發明污水生物處理方法的步驟（6 )的污水生物處理 步驟’其巾“進水，，可以是步驟（5)的上清液和/或污 水進水，“出水”意指淨化出水，“剩餘污泥”可以作 為步驟（1 )的污泥進料。 第6圖為傳統SBR汙水處理工藝流程圖。該工藝可以作為 本發明污水生物處理方法的步驟（6)的污水生物處理步 驟’其中各個術語的意思同第5圖。SBR ( Sequencing Batch React〇r Activaten Sludge Process)是序 批式活性污泥法’好氧*池的入水緊貼池底由過水洞進入 SBR池’污水透過SBR池中的污泥層出水時，污泥層能夠 起到過濾和截留的作用，降低了出水中懸浮物的含量， 使得出水水質優於普通二沉池的出水。本發明還採用空 氣堪控制出水，防止曝氣期間的懸浮物進入出水堰從而 可有效地控制出水懸浮物。 第7圖為傳統AB法汙水處理工藝斤程圖》該工藝可以作為 本發明污水生物處理方法的步褲（6)的涔水生物處理步 驟’其中各個術語的意思同第5圖。 第8圖為a/ο法汙水處理工藝流程圖。該工藝可以作為本 發明污水生物處理方法的步驟（6)汙水處理步騍，其中 各個術語的意思同第5圖。 第9圖為A20法汙水處理工藝流程圖。該工藝可以作為本 發明污水生物處理方法的步驟（6)的汸水生物處理步驟 ，其中各個術語的意思同第5圖。 099140871 表單編號A0101 第39頁/共79頁 0993446280-0 [0133] 201221484 [0134] 第1 0圖為MSBR汙水處理工藝流程圖。該工藝可以作為本 發明污水生物處理方法的步驟（6)的污水生物處理步驟 ，其中各個術語的意思同第5圖。 [0135] 在另一方面，本發明還提供一種用於上述污泥處理方法 的污泥處理裝置，包括：能夠將污泥進料與第一混合液 混合得到第二混合液的第一設備；能夠將第二混合液進 行給氧處理得到第三混合液的第二設備；能夠將第三混 合液進行缺氧處理得到第四混合液的第三設備；能夠將 第四混合液分離得到上清液和第一濃縮混合液的第四設 備；能夠將上清液排出的第五設備；能夠將至少部分第 一濃縮混合液引入第一設備並且使未返回第一設備的第 一濃縮混合液的污泥量小於污泥進料的污泥量的第六設 備。 [0136] 在一些實施方案中，第一設備可以是任意合適的能夠混 合污泥進料與混合液的構築物或容器。第二設備可以與 第一設備是同一設備，或者是不同的設備，例如與第一 設備水利學連通的能夠使含氧氣體例如空氣與混合液接 觸的設備，例如帶有曝氣設備的曝氣池。第三設備可以 與第一設備和第二設備是同一設備，其在例如停止曝氣 的情況下實現缺氧處理（以序批方式運行）；或者第三 設備與第二設備可以是不同的設備，例如與第二設備水 利學連通的能夠基本上避免含氧氣體與混合物接觸的構 築物或容器（例如沉澱池）（以連續或半連續方式運行 )。第四設備可以與第一設備、第二設備和第三設備為 同一設備，或者僅與第三設備為同一設備，其在例如停 099140871 表單編號A0101 第40頁/共79頁 0993446280-0 201221484 止曝氣和/或攪拌的情況下通過例如沉澱來實現上清液與 第一濃縮混合液的分離（以序批方式運行）；或者第四 設備可以為獨立的與第三設備連通的能夠將混合液分離 得到上清液和第一濃縮混合液的設備，例如獨立的沉澱 池、離心分離設備或過濾分離設備（以連續或半連續方 式運行）。第五設備可以是任意合適的能夠從第四設備 中取出上清液的設備，例如排水口、排水管、没水器等 。第六設備可以與第一設備、第二設備、第三設備和第 四設備為同一設備（以序批方式運行）；或者為獨立的 能夠將至少部分第一濃縮混合液從第四設備輸送到第一 設備的設備，例如與第一設備和第四設備水利學連通的 任選具有輸送泵和控制閥的回流管（以連續或半連續方 式運行）。第六設備還任選地具有能夠讓第一濃縮混合 液的剩餘部分排出的設備，例如具有控制閥的排液口或 排液管，以控制未返回第一設備的第一濃縮混合液的污 泥量小於污泥進料的污泥量。 [0137] 在一些實施方案中，第二設備可以是曝氣池、氧化溝、 流化床、移動床或膜設備等，優選為曝氣池，更優選為 推流式矩形曝氣池。第三設備優選為沉澱池，更優選為 推流式矩形沉澱池。 [0138] 根據本發明的污泥處理裝置的一些實施方案，所述污泥 處理裝置還包括與第一設備連通的能夠對污泥進料進行 給氧處理的設備，例如污泥預曝氣設備。 [0139] 根據本發明的污泥處理裝置的一些實施方案，所述污泥 處理裝置還包括設置在第二設備和第三設備之間並分別 099140871 表單編號A0101 第41頁/共79頁 0993446280-0 201221484 理的去氧設備，例如 與其水利學連通的能夠進行去氧處 脫氣池。 [0140] [0141] [0142] 099140871 根據本發明的污泥處理裝置的—些實施方案，立中第二 設備經設計使得給氧處理時間能_自0.丨〜〇 2小時、 U〜0.3小時、0.3〜0‘4小時、〇4〜〇 5小時、"〜 〇.6小時、〇.6〜°·8小時、〇.8叫小時、卜"小時、 U〜1.5小時、小時、18〜2小時、2〜2 2 小時、2. 2〜2. 5小時、2. 5〜3小時和3, 5〜4小時，優選 1· 5〜3小時。例如’當以連續方式運行時，可以根據第 二設備中第二混合液職量，將斯望的給氧處理時間作 為第二混合液的停留時間來確定第二設備的體積。 根據本發明的污泥處理裝置的一些實施方案其中第三 設備經設計使得缺氧處理時間能夠選自〇. 8〜1小時、i 1.2小時、1.2〜14小時、14〜16小時、16〜18小 時、1. 8〜2小時、2〜2. 5小時、2, 5广3小時、3〜3. δ 小時、3· 5〜4小時、4〜4.丨5小時、4, 5〜5小時、5〜 5. 5小時和5. 5〜6小時，優選3〜4Φ時。例如，當以連 續方式運行時，可以根據第三設備中第三混合液的流量 ’將期望的缺氧處理時間作為第三混合液的停留時間來 確定第二設備的體積。 在一些情況下，第二設備和第三設備經設計使得給氧處 理時間與缺氧處理時間的比能夠選自1:0. 5〜1:ι、1:1 5、1:1.5〜1: 2、1:2〜1:2.5、1:2.5〜1:3、 1:3〜1:3.6、1:3.6〜1:4、1:4〜1:4.5、1:4.5〜 1 : 5、1 : 5 〜1 : 5. 5 和 1 : 5. 5 〜1 : 6，優選 1 ’· 1 〜1 : 3。例 0993446280-0 表單蝙號A010〗 第42頁/共79頁 201221484 如，當以連續方式運行時，可以根據期望的給氧處理時 間與缺氧處理時間的比來確定第二設備與第三設備的體 積比。 [0143] 根據本發明的污泥處理裝置的一些實施方案，所述污泥 處理裝置還包括能夠收集並回收氣態含磷化合物的回收 設備。例如，該回收設備可以與第二設備和/或第三設備 連通以將第二設備和/或第三設備中產生的氣態含磷化合 物回收。在一些實施方案中，該回收設備可以是冷凍設 0 備、燃燒設備、或者具有固體或液體吸附劑的吸附塔、 吸收罐等。 [0144] 在另一方面，本發明還提供一種用於上述污水生物處理 方法的污水生物處理裝置，包括：能夠將污泥進料與第 一混合液混合得到第二混合液的第一設備；能夠將第二 - 混合液進行給氧處理得到第三混合液的第二設備；能夠 將第三混合液進行缺氧處理得到第四混合液的第三設備 ;能夠將第四混合液分離得到上清液和第一濃縮混合液 〇 的第四設備；能夠將上清液排出的第五設備；能夠將至 少部分第一濃縮混合液引入第一設備並且使未返回第一 設備的第一濃縮混合液的污泥量小於污泥進料的污泥量 的第六設備；能夠將至少部分第五設備排出的上清液進 行污水生物處理得到第二濃縮混合液和淨化出水的第七 設備；能夠將淨化出水排出的第八設備；能夠將污水進 料引入第一設備和/或第七設備的第九設備，以及任選的 能夠將至少部分第二濃縮混合液引入第一設備的第十設 備0 099140871 表單編號A0101 第43頁/共79頁 0993446280-0 201221484 [0145] [0146] [0147] [0148] [0149] 根據本發明的污水生物處理裝置的一歧叙 〜汽方&方累，第七 設備是能夠根據Wuhrmann工藝、Α/0_χ黏 sc、Bardenpho 工藝、Ph〇redox工藝、A2/0工藝、倒置A2/〇工藝、uct 工藝、MUCT工藝、VIP工藝、議A工藝遍工藝、 TNCU工藝、Dephanox工藝、BCFS工藝、MSBR工藝、sbr 工藝、AB工藝、氧化溝工藝、生物膜工藝、流動床工藝 或其組合進行污水生物處理的設備。 在另一方面，本發明還提供一種污泥減量化汙水處理系 統，包括：常規汙水處理裝置和與其進水口連接的污泥 消解裝置，所述常規汗水處理裝置的剩餘污泥管連接至 污泥消解裝置。 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述污泥消解裝置包括高濃度污泥反應裝置。 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述污泥消解裝置包括放氰绽爽裝置，所述高濃度污 泥反應襞置的出水口輿厭氧沉澱裝置的入水口連接所 述厭氧沉澱襞置包括第一污泥回流瞀，所述第—污泥回 流管連接至高濃度污泥反應裝置。 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述剩餘污泥回流管將全部剩餘污泥回流至污泥消解 裝置。 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述污泥消解裝置包括厭氧沉搬裝置，所述高濃度污 泥反應裝置的出水口與厭氧沉澱裝置的入水口連接，所 099140871 表單編號A0101 第44頁/共79頁 0993446280-0 [0150] 201221484 述厭氧沉澱裝置包括第一污泥回流管，所述第一污泥回 流管連接至高濃度污泥反應裝置，所述剩餘污泥回流管 將全部剩餘污泥回流至污泥消解裝置。 [0151] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，其特徵在於，高濃度污泥反應裝置的污泥濃度為 4000mg/L〜20000mg/L ;例如6000mg/L、8000mg/L、 10000mg/L 、 12000mg/L 、 14000mg/L 、 15000mg/L 、 1 6000mg/L或者 18000rag/L。 0 [0152] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述高濃度污泥反應裝置的水力停留時間為1. 5h〜 3. Oh，出口溶解氧為 lmg/L 〜1. 5mg/L 、1. 5mg/L 〜 2mg/L、2mg/L〜2.5mg/L或2.5mg/L〜3mg/L。 [0153] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述污泥回流管將0. 4Q〜0. 7Q的污泥回流至高濃度污 泥反應裝置。 q [0154] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述高濃度污泥反應裝置與厭氧沉澱裝置之間設置去 氧裝置。 [0155] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，還包括剩餘污泥曝氣池，所述常規汙水處理裝置的剩 餘污泥管先連接至剩餘污泥曝氣池，剩餘污泥曝氣池再 與高濃度污泥反應裝置連接。 [0156] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述污泥消解裝置的進水口處設置預處理裝置，所述 099140871 表單編號A0101 第45頁/共79頁 0993446280-0 201221484 預處理裝置為至少一級格柵。 [0157] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述預處理裝置為兩級格柵。 [0158] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述常規汙水處理裝置包括依次串聯的厭氧反應裝置 、好氛反應裝置和沉殿裝置，沉澱裝置包括第二污泥回 流管和剩餘污泥管，所述第二污泥回流管連接至厭氧反 應裝置。 [0159] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述好氧反應裝置為好氧池或氧化溝。 [0160] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述常規汙水處理裝置包括依次串聯的厭氧反應裝置 、缺氧反應裝置、好氧反應裝置和沉澱裝置，沉澱裝置 包括第三污泥回流管和剩餘污泥管，所述第三污泥回流 管連接至缺氧反應裝置。 [0161] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述沉澱裝置為SBR池或沉澱池。 [0162] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述SBR池的污泥濃度為2000mg/L〜4000mg/L，溶解 氧含量為2mg/L〜4mg/L，在一週期内靜沉時間為lh〜 1. 5 h，恒水位排水時間為1. 5 h〜2. 5 h。 [0163] 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述第二污泥回流管連接至厭氧反應裝置，將0. 5Q〜 099140871 表單編號A0101 第46頁/共79頁 0993446280-0 201221484 [0164] 1Q的污泥回流至厭氧反應裝置。 根據本發明的污泥減量化汙水處理系統的一些實施方案 ，所述第三污泥回流管連接至厭氧反應裝置，將0. 5Q〜 1Q的污泥回流至厭氧反應裝置。 [0165] 在另一方面，本發明還提供一種污泥減量化汙水處理方 法，其特徵在於，包括： [0166] 步驟a)使污水與污泥的混合液進行污泥消解反應； ^ [0167] 〇 步驟b)將污泥消解反應後的污水進行常規汙水處理； [0168] 步驟C)將處理後的污水排出，使常規汙水處理產生的剩 餘污泥回流參與污泥消解反應。 [0169] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，其特徵在於，所述步驟a)中污泥消解反應包括對污水 和污泥的混合液進行高濃度污泥反應。 [0170] 根據本發明的污泥減量化汙水處理方法的一些實施方案 〇 ，所述步驟a)中污泥消解反應包括對高濃度污泥反應後 的污水與污泥的混合液進行厭氧沉澱，經厭氧沉澱的污 泥回流參與高濃度污泥反應。 [0171] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述剩餘污泥回流為全部回流。 • [0172] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述步驟a)中污泥消解反應包括對高濃度污泥反應後 的污水與污泥的混合液進行厭氧沉澱，經厭氧沉澱的污 泥回流參與高濃度污泥反應，所述剩餘污泥回流為全部 099140871 表單編號A0101 第47頁/共79頁 0993446280-0 201221484 回流。 [0173] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述高濃度污泥反應時，污泥濃度為4000mg/L〜 20000mg/L ;例如 6000mg/L、8000mg/L、1 0000mg/L ' 1 2000mg/L ' 14000rag/L ' 1 5000mg/L > 1 6000mg/L 或者 18000mg/L。 [0174] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述高濃度污泥反應的水力停留時間為1. 5h〜3. Oh， 出口溶解氧為 lmg/L〜1.5mg/L 、1.5mg/L〜2mg/L、 2mg/L〜2.5mg/L或2. 5mg/L〜3mg/L。 [0175} 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述厭氧沉澱的污泥回流參與高濃度污泥反應的回流 比為0· 4Q〜0. 7Q。 [0176] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述高濃度污泥反應後的污水和污泥的混合液先進行 去氧再進行厭氧沉澱。 [0177] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述剩餘污泥先進行污泥曝氣再進行高濃度污泥反應 〇 [0178] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述污泥曝氣的溶解氧含量為0. 2mg/L〜0. 9mg/L。 [0179] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，污水進行污泥消解反應前先進行預處理，清除雜物。 099140871 表單編號A0101 第48頁/共79頁 0993446280-0 201221484 [0180] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ' [0181] ，所述步驟b)中常規汙水處理包括厭氧反應、好氧反應 和沉澱，好氧反應後的污水經過沉澱後排出，產生的污 泥回流參與厭氧反應。 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述步驟b)中常規汙水處理包括厭氧反應、缺氧反應 、好氧反應和沉澱，好氧反應後的污水經過沉澱後排出 ，產生的污泥回流參與厭氧反應。 Q [0182] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述產生的污泥回流參與厭氧反應的回流比為0. 5Q〜 1Q ° [0183] 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述沉澱採用SBR工藝。 [0184] ❹ 根據本發明的污泥減量化汙水處理方法的一些實施方案 ，所述SBR工藝採用的污泥濃度為2000mg/L〜4000mg/L ，溶解氧含量為2mg/L〜4rag/L，在一週期内靜沉時間為 1 h〜1. 5 h，恒水位排水時間為1. 5 h〜2. 5 h。 [0185] 在另一方面，本發明還提供一種污泥減量化汙水處理系 統，其特徵在於，包括：依次争聯的高濃度污泥反應裝 置、厭氧沉澱裝置和常規汙水處理裝置，所述厭氧沉澱 裝置的污泥回流管連接至高濃度污泥反應裝置，所述常 規汙水處理裝置的剩餘污泥管與高濃度污泥反應裝置連 接。 [0186] 根據本發明的污泥減量化汙水處理系統的一些實施方案 099140871 表單編號A0101 第49頁/共79頁 0993446280-0 201221484 ，高濃度污泥反應裝置的污泥濃度為4000mg/L〜 20000mg/L ;例如至少 6000mg/L、至少 8000mg/L、至 少 1 0000mg/L、至少 1 2000mg/L、至少 14000mg/L、至 少 1 5000mg/L、至少 1 6000mg/L或者至少 1 8000mg/L。 [0187] 在一些實施方案中，本發明的污水生物處理裝置可以是 如第11、12或13圖所示流程的裝置，其中污泥消解裝置 包括依次串聯的高濃度污泥反應池、去氧池和厭氧沉澱 池。 [0188] 污泥消解池前優選設置預處理裝置，預處理裝置為至少 一級格柵，格柵是汙水處理廠的第一道處理設施，具體 可設置兩級格柵，首先通過第一級格栅將污水中較大的 懸浮物去除，然後污水再通過第二級格栅進一步去除較 小的懸浮物，第一級格柵的柵條淨距大於第二級格柵的 栅條淨距，如··第一級格柵為粗格柵，栅條淨距20mm， 安裝角度60度，第二級格栅為細格柵，柵條淨距6mm，安 裝角度60度。 [0189] 高濃度污泥反應裝置具體為高濃度污泥反應池，在高濃 度污泥反應池中對預處理後的污水、厭氧沉澱裝置回流 的污泥和由系統末端的沉澱裝置回流的剩餘污泥進行曝 氣混合，採用推流式矩形池型。在沉澱裝置與高濃度污 泥反應裝置之間設置剩餘污泥曝氣池，剩餘污泥曝氣池 與沉澱裝置和高濃度污泥反應裝置之間分別通過剩餘污 泥管連接，回流的剩餘污泥流入剩餘污泥曝氣池中，污 水和厭氧沉澱裝置回流的污泥直接流入高濃度污泥反應 池，然後經過曝氣後的剩餘污泥再流入高濃度污泥反應 099140871 表單編號A0101 第50頁/共79頁 0993446280-0 201221484 池與污水和污泥的混合液充分混合。 [0190] 高濃度污泥反應池在較高的污泥濃度下運行，水力停留 時間短，以兼氧、好氧的方式運行，高濃度污泥反應池 與後續的厭氧沉澱裝置之間還存在污泥迴圈，本發明中 來自厭氧沉澱裝置的污泥向高濃度污泥反應池回流。由 於來自各時段的污水水質水量不均勻且波動性較大，高 濃度污泥反應池還可以起到緩衝的作用，避免衝擊負荷 對生化處理的影響。 Ο [0191] 厭氧沉澱裝置具體為厭氧沉濺池丨厭^沉澱池中的污泥 回流入高濃度污泥反灰池與污水和剩餘污泥共同參與反 應，可採用無i#塞污泥泵實現污泥迴圈。作為優選，高 濃度污泥反應裝置與厭氧沉ϋί裝置之間還包括去氧裝置 ’污水和污泥的混合液進行去氧後再進入厭氧沉澱池， 避免將溶解氧帶入厭氧沉澱池中，對厭氧反應造成影響Sewage below 500mg/L, below 350mg/L, below 30〇mg/L, below 250mg/L ' below 200mg/L, below 150mg/L or below i〇〇mg/L Biological treatment. Of course, in the sewage feed, various pollution 099140871 Form No. A0101 Page 37 / Total 79 Page 0993446280-0 201221484 When the proportion of the dye is unbalanced and the carbon source is lacking, the appropriate carbon source can be supplemented in the sewage feed. For example, such as methanol and other organic nutrients such as starch, molasses, and the like. [0127] The sewage biological treatment method according to the present invention can transfer (four) any sewage biological treatment method (for example, various conventional aerobic sewage biological treatment methods and anaerobic sewage biological treatment methods) for discharging excess sludge as Step (6) of the sewage biological treatment step. In some embodiments, the sewage biological treatment step of step (6) may be according to the wuhrmann process, A 0 « Bardenpho process, ph〇red〇x process, A2/〇 process, inverted A2/0 process, 11 (^ process, Wastewater biological treatment of MUCT process, νιρ process, 0MSA process, JHB process, TNCU process, Dephan〇x process, BCFS process, MSBR process, SBR process, AB process, oxidation ditch process, biofilm process, fluidized bed process or combination thereof Figure 3 is a schematic view showing the process flow of some embodiments of the biological treatment method for sewage according to the present invention, wherein "influent water" represents sewage feed, and "sludge digestion device" represents capable of carrying out sludge treatment according to the present invention. The method (ie, the steps (1) to (5)), the "conventional sewage treatment device represents any suitable sewage treatment device capable of performing the sewage biological biological treatment step of the step (6), and the "water outlet" represents the purified water. "Excess sludge backflow represents the '_agricultural mixture' used as the 'sludge feed of step (1). Figure 4 shows another method of biological treatment of sewage according to the present invention. Schematic diagram of the process flow of some embodiments, wherein each term has the same meaning as the term in Figure 3 'and sludge' represents sludge feed from another source. 099140871 Form No. A0101 Page 38 of 79 0993446280-0 [0128] 201221484 [0130] 013 [0131] FIG. 5 is a flow chart of a conventional oxidation ditch sewage treatment process. The process can be used as the sewage of the step (6) of the sewage biological treatment method of the present invention. The biological treatment step 'the towel' is influent, which may be the supernatant of the step (5) and/or the influent water, the "water" means the purified water, and the "excess sludge" may be used as the sludge of the step (1). Fig. 6 is a flow chart of the conventional SBR sewage treatment process. The process can be used as the sewage biological treatment step of the step (6) of the sewage biological treatment method of the present invention, wherein each term has the same meaning as Fig. 5. SBR (Sequencing Batch React〇r Activaten Sludge Process) is the sequential batch type activated sludge method. The aerobic* pool water enters the bottom of the pool from the water hole into the SBR pool. When the sewage passes through the sludge layer in the SBR pool, the sludge layer Able to filter And the effect of interception reduces the content of suspended solids in the effluent, so that the effluent water quality is superior to the effluent of the ordinary secondary settling tank. The invention also adopts air to control the effluent to prevent the suspended solids during the aeration from entering the effluent and thus can be effectively controlled. The effluent suspended matter. Fig. 7 is a conventional AB method sewage treatment process. The process can be used as the hydrophobic biological treatment step of the step trousers (6) of the sewage biological treatment method of the present invention, wherein each term has the same meaning as the fifth Figure. Figure 8 is a flow chart of the a/ο method of sewage treatment. This process can be used as a step (6) of the sewage biological treatment method of the present invention, wherein each term has the same meaning as in Figure 5. Figure 9 is a flow chart of the A20 wastewater treatment process. This process can be used as a hydrophobic biological treatment step in the step (6) of the sewage biological treatment method of the present invention, wherein each term has the same meaning as in Figure 5. 099140871 Form No. A0101 Page 39 of 79 0993446280-0 [0133] 201221484 [0134] Figure 10 is a flow chart of the MSBR wastewater treatment process. This process can be used as a sewage biological treatment step in the step (6) of the sewage biological treatment method of the present invention, wherein each term has the same meaning as in Figure 5. [0135] In another aspect, the present invention provides a sludge treatment apparatus for the above sludge treatment method, comprising: a first apparatus capable of mixing a sludge feed with a first mixed liquid to obtain a second mixed liquid; a second device capable of performing oxygen supply treatment to obtain a third mixed liquid; a third device capable of performing anoxic treatment on the third mixed liquid to obtain a fourth mixed liquid; capable of separating the fourth mixed liquid to obtain a supernatant a fourth device for the liquid and the first concentrated mixture; a fifth device capable of discharging the supernatant; capable of introducing at least a portion of the first concentrated mixture into the first device and returning the first concentrated mixture not returned to the first device The sixth device in which the amount of sludge is less than the amount of sludge fed by the sludge. [0136] In some embodiments, the first apparatus can be any suitable structure or vessel capable of mixing the sludge feed and mixture. The second device may be the same device as the first device, or a different device, such as a device that is in water communication with the first device, capable of contacting an oxygen-containing gas, such as air, with the mixed liquid, such as aeration with an aeration device. Pool. The third device may be the same device as the first device and the second device, which implements anoxic treatment (running in a batch mode), for example, if aeration is stopped; or the third device and the second device may be different devices For example, a structure or vessel (e.g., a sedimentation tank) capable of substantially avoiding contact of the oxygen-containing gas with the mixture (operating in a continuous or semi-continuous manner) in communication with the second apparatus. The fourth device may be the same device as the first device, the second device, and the third device, or only the same device as the third device, for example, stop 099140871 Form No. A0101 Page 40 / Total 79 Page 0993446280-0 201221484 Separation of the supernatant from the first concentrated mixture (for sequential operation) by, for example, precipitation in the case of aeration and/or agitation; or the fourth device can be independently connected to the third device capable of mixing The liquid is separated into a device for obtaining a supernatant and a first concentrated mixture, such as a separate sedimentation tank, a centrifugal separation device or a filtration separation device (running in a continuous or semi-continuous manner). The fifth device may be any suitable device capable of removing the supernatant from the fourth device, such as a drain, drain, water eliminator or the like. The sixth device may be the same device as the first device, the second device, the third device, and the fourth device (running in a batch mode); or independently capable of transporting at least a portion of the first concentrated mixture from the fourth device to The apparatus of the first apparatus, such as a return line (having a continuous or semi-continuous operation) optionally having a transfer pump and a control valve in communication with the first apparatus and the fourth apparatus. The sixth apparatus also optionally has means for discharging the remainder of the first concentrated mixture, such as a drain or drain having a control valve to control fouling of the first concentrated mixture that has not returned to the first apparatus The amount of mud is less than the amount of sludge fed by the sludge. [0137] In some embodiments, the second device may be an aeration tank, an oxidation ditch, a fluidized bed, a moving bed or membrane apparatus, etc., preferably an aeration tank, more preferably a push-flow rectangular aeration tank. The third device is preferably a sedimentation tank, more preferably a push-flow rectangular sedimentation tank. [0138] According to some embodiments of the sludge treatment apparatus of the present invention, the sludge treatment apparatus further includes an apparatus in communication with the first apparatus capable of oxygenating the sludge feed, such as a sludge pre-aeration apparatus . [0139] According to some embodiments of the sludge treatment apparatus of the present invention, the sludge treatment apparatus further comprises a second apparatus and a third apparatus and is respectively 099140871 Form No. A0101 Page 41 / Total 79 Page 0993446280- 0 201221484 The deoxygenation equipment, for example, connected to its hydraulics, is capable of degassing the degassing tank. [0141] 099140871 According to some embodiments of the sludge treatment apparatus of the present invention, the second apparatus is designed such that the oxygen treatment time can be from 0. 丨 to 〇 2 hours, U 〜 0.3 Hours, 0.3~0'4 hours, 〇4~〇5 hours, "~ 〇.6 hours, 〇.6~°·8 hours, 〇.8 called hours, Bu"hours, U~1.5 hours, hours , 18 to 2 hours, 2 to 2 2 hours, 2. 2 to 2. 5 hours, 2. 5 to 3 hours, and 3, 5 to 4 hours, preferably 1 to 5 to 3 hours. For example, when operating in a continuous mode, the volume of the second device can be determined based on the second mixed liquor level in the second device as the residence time of the second mixture. Some embodiments of the sludge treatment apparatus according to the present invention, wherein the third apparatus is designed such that the anoxic treatment time can be selected from the group consisting of 〇. 8 to 1 hour, i 1.2 hours, 1.2 to 14 hours, 14 to 16 hours, 16 to 18 Hour, 1. 8~2 hours, 2~2. 5 hours, 2, 5 wide 3 hours, 3~3. δ hours, 3·5~4 hours, 4~4. 丨5 hours, 4, 5~5 Hour, 5 to 5. 5 hours and 5. 5 to 6 hours, preferably 3 to 4 Φ. For example, when operating in a continuous mode, the volume of the second device can be determined based on the flow rate of the third mixed liquid in the third device as the residence time of the third mixed liquid. In some cases, the second device and the third device are designed such that the ratio of the oxygen treatment time to the anoxic treatment time can be selected from 1:0. 5~1: ι, 1:1 5, 1:1.5~1: 2, 1:2~1:2.5, 1:2.5~1:3, 1:3~1:3.6, 1:3.6~1:4, 1:4~1:4.5, 1:4.5~1: 5, 1 : 5 〜1 : 5. 5 and 1: 5. 5 〜1 : 6, preferably 1 '· 1 〜1 : 3. Example 0993446280-0 Form bat number A010〗 Page 42 / Total 79 pages 201221484 For example, when operating in a continuous mode, the second device and the third device can be determined according to the ratio of the desired oxygen treatment time to the anoxic treatment time. Volume ratio. [0143] According to some embodiments of the sludge treatment apparatus of the present invention, the sludge treatment apparatus further includes a recovery apparatus capable of collecting and recovering a gaseous phosphorus-containing compound. For example, the recycling device can be in communication with the second device and/or the third device to recover the gaseous phosphorus-containing compound produced in the second device and/or the third device. In some embodiments, the recovery equipment can be a refrigeration unit, a combustion unit, or an adsorption column with a solid or liquid adsorbent, an absorption tank, and the like. [0144] In another aspect, the present invention also provides a sewage biological treatment apparatus for the above sewage biological treatment method, comprising: a first apparatus capable of mixing a sludge feed with a first mixed liquid to obtain a second mixed liquid; a second device capable of performing oxygen treatment on the second mixed liquid to obtain a third mixed liquid; a third device capable of performing anoxic treatment on the third mixed liquid to obtain a fourth mixed liquid; capable of separating the fourth mixed liquid a fourth device for clearing liquid and a first concentrated mixed liquid; a fifth device capable of discharging the supernatant; capable of introducing at least a portion of the first concentrated mixed liquid into the first device and causing the first concentrated mixture not returned to the first device a sixth device capable of controlling the amount of sludge of the liquid to be smaller than the amount of sludge fed by the sludge; capable of subjecting at least a portion of the supernatant discharged from the fifth device to biological treatment of the sewage to obtain a second concentrated mixture and a seventh device for purifying the water; An eighth device for discharging purified water; a ninth device capable of introducing the sewage feed into the first device and/or the seventh device, and optionally capable of mixing at least a portion of the second concentration The tenth device in which the liquid is introduced into the first device 0 099140871 Form No. A0101 Page 43 / Total 79 Page 0993446280-0 201221484 [0146] [0148] [0149] One of the sewage biological treatment devices according to the present invention The seventh device is capable of according to the Wuhrmann process, Α/0_χ vis sc, Bardenpho process, Ph〇redox process, A2/0 process, inverted A2/〇 process, uct process, MUCT process, Wastewater biological treatment equipment for VIP process, process A process, TNCU process, Dephanox process, BCFS process, MSBR process, sbr process, AB process, oxidation ditch process, biofilm process, fluidized bed process or combination thereof. In another aspect, the present invention also provides a sludge reduction sewage treatment system comprising: a conventional sewage treatment device and a sludge digestion device connected to the water inlet thereof, wherein the remaining sludge pipe of the conventional sweat treatment device is connected to Sludge digestion device. According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the sludge digestion device comprises a high-concentration sludge reaction device. According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the sludge digestion device includes a cyanide-sparing device, the water outlet of the high-concentration sludge reaction device, and the inlet of the anaerobic precipitation device The connection of the anaerobic sedimentation device includes a first sludge return port, and the first sludge return pipe is connected to the high concentration sludge reaction device. According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the excess sludge return pipe returns all of the excess sludge to the sludge digestion device. According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the sludge digestion device includes an anaerobic sedimentation device, and the water outlet of the high-concentration sludge reaction device is connected to the water inlet of the anaerobic sedimentation device. , 099140871 Form No. A0101 Page 44 / Total 79 Page 0993446280-0 [0150] 201221484 The anaerobic precipitation device comprises a first sludge return pipe, and the first sludge return pipe is connected to a high-concentration sludge reaction device. The excess sludge return pipe returns all of the excess sludge to the sludge digestion device. Some embodiments of the sludge-reduced sewage treatment system according to the present invention are characterized in that the sludge concentration of the high-concentration sludge reaction device is 4000 mg/L to 20000 mg/L; for example, 6000 mg/L, 8000 mg/ L, 10000 mg/L, 12000 mg/L, 14000 mg/L, 15000 mg/L, 1 6000 mg/L or 18000rag/L. 0〜〜 Oh, the outlet dissolved oxygen is 1mg / L ~ ~ ~ ~ Oh, the outlet dissolved oxygen is lmg / L ~ ~ ~ ~ Oh, the outlet dissolved oxygen is lmg / L ~ 1. 5 mg / L, 1.5 mg / L ~ 2 mg / L, 2 mg / L ~ 2.5 mg / L or 2.5 mg / L ~ 3mg / L. The sludge returning pipe returns 0.44~0. 7Q of the sludge to the high-concentration sludge reaction device. [0154] According to some embodiments of the sludge-reducing sewage treatment system of the present invention, a de-oxygenation device is disposed between the high-concentration sludge reaction device and the anaerobic precipitation device. [0155] Some embodiments of the sludge-reduced sewage treatment system according to the present invention further include an excess sludge aeration tank, the remaining sludge tube of the conventional sewage treatment device being first connected to the remaining sludge aeration tank The excess sludge aeration tank is connected to a high-concentration sludge reaction unit. [0156] According to some embodiments of the sludge-reducing sewage treatment system of the present invention, a pre-treatment device is provided at the water inlet of the sludge digestion device, the 099140871 Form No. A0101, page 45/79, 0993446280- 0 201221484 The pretreatment device is at least a primary grille. [0157] According to some embodiments of the sludge degrading sewage treatment system of the present invention, the pretreatment device is a two-stage grid. [0158] According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the conventional sewage treatment apparatus includes an anaerobic reaction device, a good atmosphere reaction device, and a sink device in series, and the sedimentation device includes a second A sludge return pipe and an excess sludge pipe are connected to the anaerobic reaction device. [0159] According to some embodiments of the sludge-reduced sewage treatment system of the present invention, the aerobic reaction device is an aerobic tank or an oxidation ditch. [0160] According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the conventional sewage treatment apparatus includes an anaerobic reaction device, an anoxic reaction device, an aerobic reaction device, and a sedimentation device, which are sequentially connected in series, and precipitated The apparatus includes a third sludge return pipe and an excess sludge pipe, and the third sludge return pipe is connected to the anoxic reaction device. [0161] According to some embodiments of the sludge reduction sewage treatment system of the present invention, the precipitation device is an SBR pool or a sedimentation tank. According to some embodiments of the sludge-reduced sewage treatment system of the present invention, the SBR pool has a sludge concentration of 2000 mg/L to 4000 mg/L and a dissolved oxygen content of 2 mg/L to 4 mg/L. 5 h〜2. 5 h。 The sluice time is 1. 5 h~2. 5 h. [0030] According to some embodiments of the sludge-reduced sewage treatment system of the present invention, the second sludge return pipe is connected to the anaerobic reactor, and will be 0. 5Q~ 099140871 Form No. A0101 Page 46 of 79 Page 0993446280-0 201221484 [0164] The sludge of 1Q is refluxed to the anaerobic reactor. According to some embodiments of the sludge-reducing sewage treatment system of the present invention, the third sludge return pipe is connected to the anaerobic reactor, and the sludge of 0.5 to 1Q is returned to the anaerobic reactor. [0165] In another aspect, the present invention provides a sludge reduction wastewater treatment method, comprising: [0166] step a) performing a sludge digestion reaction of a mixture of sewage and sludge; 0167] 〇 Step b) The sewage after the sludge digestion reaction is subjected to conventional sewage treatment; [0168] Step C) The treated sewage is discharged, and the excess sludge generated by the conventional sewage treatment is refluxed to participate in the sludge digestion reaction. [0169] Some embodiments of the sludge-reducing sewage treatment method according to the present invention, characterized in that the sludge digestion reaction in the step a) comprises performing a high-concentration sludge reaction on a mixture of sewage and sludge. [0170] According to some embodiments of the sludge-reducing sewage treatment method of the present invention, the sludge digestion reaction in the step a) comprises anaerobic mixture of sewage and sludge after the reaction of the high-concentration sludge Precipitation, anaerobic precipitation of sludge backflow participates in high-concentration sludge reaction. [0171] According to some embodiments of the sludge-reduced sewage treatment method of the present invention, the excess sludge reflux is total reflux. [0172] According to some embodiments of the sludge-reducing sewage treatment method of the present invention, the sludge digestion reaction in the step a) comprises anaerobic mixture of sewage and sludge after the reaction of the high-concentration sludge Precipitation, anaerobic precipitation of sludge backflow participates in high-concentration sludge reaction, the excess sludge reflux is all 099140871 Form No. A0101 Page 47 / Total 79 Page 0993446280-0 201221484 Reflow. According to some embodiments of the sludge-reducing sewage treatment method of the present invention, when the high-concentration sludge is reacted, the sludge concentration is 4000 mg/L to 20000 mg/L; for example, 6000 mg/L, 8000 mg/L, 1 0000 mg / L ' 1 2000 mg / L ' 14000rag / L ' 1 5000mg / L > 1 6000mg / L or 18000mg / L. [0174] The hydraulic retention time of the high-concentration sludge reaction is 1. 5h~3. Oh, the dissolved oxygen at the outlet is 1mg/L~1.5mg, according to the embodiment of the present invention. /L, 1.5 mg / L ~ 2mg / L, 2mg / L ~ 2.5mg / L or 2. 5mg / L ~ 3mg / L. The Reflux ratio of the anaerobic sludge to the high-concentration sludge reaction is 0. 4Q~0. 7Q. According to some embodiments of the sludge-reducing sewage treatment method of the present invention, the mixture of the sewage and the sludge after the high-concentration sludge reaction is first subjected to deoxygenation and then subjected to anaerobic precipitation. According to some embodiments of the sludge-reducing sewage treatment method of the present invention, the excess sludge is first subjected to sludge aeration and then subjected to a high-concentration sludge reaction. [0178] Sludge reduction according to the present invention 2mg/L〜0. 9mg/L。 The dissolved oxygen content of the sludge aeration is 0. 2mg / L~0. 9mg / L. [0179] According to some embodiments of the sludge-reducing sewage treatment method of the present invention, the sewage is subjected to pretreatment before the sludge digestion reaction to remove impurities. 099140871 Form No. A0101 Page 48/79 Page 0993446280-0 201221484 [0180] Some embodiments of a sludge reduction wastewater treatment method according to the present invention [0181], the conventional sewage treatment in the step b) includes The anaerobic reaction, the aerobic reaction and the precipitation, the sewage after the aerobic reaction is discharged after being precipitated, and the generated sludge reflux participates in the anaerobic reaction. According to some embodiments of the sludge-reduced sewage treatment method of the present invention, the conventional sewage treatment in the step b) includes an anaerobic reaction, an anoxic reaction, an aerobic reaction, and precipitation, and the sewage after the aerobic reaction is precipitated. After the discharge, the resulting sludge reflux participates in the anaerobic reaction. The Q4 according to the present invention, the reflux ratio of the produced sludge backflow to participate in the anaerobic reaction is 0. 5Q~1Q ° [0183] Some embodiments of a mud reduction wastewater treatment process using an SBR process. [0184] According to some embodiments of the sludge-reducing sewage treatment method of the present invention, the SBR process employs a sludge concentration of 2000 mg/L to 4000 mg/L and a dissolved oxygen content of 2 mg/L to 4 rag/L. 5 h〜2. 5小时。 The sluice time is 1. 5 h~2. 5 h. [0185] In another aspect, the present invention further provides a sludge-reducing sewage treatment system, comprising: a high-concentration sludge reaction device, an anaerobic sedimentation device, and a conventional sewage treatment device, which are sequentially contiguously connected, The sludge return pipe of the anaerobic precipitation device is connected to a high-concentration sludge reaction device, and the remaining sludge pipe of the conventional sewage treatment device is connected to a high-concentration sludge reaction device. Some embodiments of the sludge-reduced sewage treatment system according to the present invention 099140871 Form No. A0101 Page 49 / Total 79 Page 0993446280-0 201221484 The sludge concentration of the high-concentration sludge reaction device is 4000 mg/L~ 20000 mg / L; for example at least 6000 mg / L, at least 8000 mg / L, at least 1 0000 mg / L, at least 1 2000 mg / L, at least 14000 mg / L, at least 1 5000 mg / L, at least 1 6000 mg / L or at least 1 8000 mg / L. [0187] In some embodiments, the sewage biological treatment device of the present invention may be a device according to the flow shown in Figures 11, 12 or 13 wherein the sludge digestion device comprises a high concentration sludge reaction tank in series, deoxygenated Pool and anaerobic sedimentation tanks. [0188] Before the sludge digestion tank, a pretreatment device is preferably disposed. The pretreatment device is at least a first-stage grid. The grid is the first treatment facility of the sewage treatment plant. Specifically, a two-stage grid can be set, first through the first stage. The grid removes the larger suspended solids in the sewage, and then the sewage further removes the smaller suspended matter through the second-stage grid. The grid spacing of the first-stage grid is greater than the grid-wide spacing of the second-stage grid. For example, the first-stage grille is a coarse grille, the grid strip has a clear distance of 20 mm, the mounting angle is 60 degrees, the second-stage grille is a fine grille, the grid strip has a clear distance of 6 mm, and the mounting angle is 60 degrees. [0189] The high-concentration sludge reaction device is specifically a high-concentration sludge reaction tank, and the pre-treated sewage, the sludge returned from the anaerobic sedimentation device, and the sedimentation device at the end of the system are refluxed in the high-concentration sludge reaction tank. The excess sludge is aerated and mixed, and a push-flow rectangular pool type is adopted. An excess sludge aeration tank is arranged between the sedimentation device and the high-concentration sludge reaction device, and the remaining sludge aeration tank is connected with the sedimentation device and the high-concentration sludge reaction device through the remaining sludge pipes, and the residual sewage is returned. The mud flows into the excess sludge aeration tank, and the sludge returned by the sewage and the anaerobic sedimentation device flows directly into the high-concentration sludge reaction tank, and then the excess sludge after aeration flows into the high-concentration sludge reaction. 099140871 Form No. A0101 50 pages / total 79 pages 0993446280-0 201221484 The pool is thoroughly mixed with the mixture of sewage and sludge. [0190] The high-concentration sludge reaction tank operates at a high sludge concentration, has a short hydraulic retention time, operates in a facultative and aerobic manner, and is also between a high-concentration sludge reaction tank and a subsequent anaerobic precipitation device. There is a sludge loop, and in the present invention, the sludge from the anaerobic sedimentation device is refluxed to the high-concentration sludge reaction tank. Since the water quality and quantity of sewage from various time periods are uneven and fluctuating, the high-concentration sludge reaction tank can also play a buffering role to avoid the impact of impact load on biochemical treatment. 019 [0191] The anaerobic sedimentation device is specifically an anaerobic sedimentation tank, and the sludge in the sedimentation tank is returned to the high-concentration sludge anti-ash tank to participate in the reaction together with the sewage and the excess sludge. The mud pump realizes sludge loop. Preferably, the high-concentration sludge reaction device and the anaerobic sedimentation device further comprise a deoxidizing device mixture of sewage and sludge for deoxidation and then entering the anaerobic sedimentation tank to avoid bringing dissolved oxygen into the anaerobic sedimentation. In the pool, affecting the anaerobic reaction

[0192] Ο 常規汙水處理裝置包括依次串聯的厭氧反應裝置、好氧 反應裝置和沉澱裝置。厭氧池優選採用推流式，池内設 置折流板，也可以採用完全混合式，來自系統末端的沉 澱裝置的污泥回流入厭氧池與污水混合。好氧反應裝置 為好氧池，也可以是其他常規的好氧反應裝置如氧化溝 ，串聯在厭氧池之後。好氧池中設置曝氣裝置，如採用 三葉羅茨鼓風機和He280型動力擴散旋混曝氣裝置。 沉澱裝置具有沉澱功能’沉殿裝置設置污泥回流管和剩 餘污泥管，可以為SBR (Sequencing Batch Reactor 099140871 表單煸號A0101 第51 1/共79頁 0993446280-0 [0193] 201221484 [0194] [0195] [0196] 099140871[0192] A conventional sewage treatment apparatus includes an anaerobic reaction apparatus, an aerobic reaction apparatus, and a sedimentation apparatus which are sequentially connected in series. The anaerobic tank is preferably a push-flow type, and a baffle is provided in the tank, or a fully mixed type, and the sludge from the sedimentation device at the end of the system is returned to the anaerobic tank to be mixed with the sewage. The aerobic reaction unit is an aerobic tank, and may also be other conventional aerobic reaction devices such as oxidation ditch, which are connected in series after the anaerobic tank. Aeration devices are installed in the aerobic tank, such as a three-lobe Roots blower and a He280-type power-diffusion rotary mixing aeration device. The sedimentation device has a sedimentation function. The sinking device is provided with a sludge return pipe and an excess sludge pipe, which can be SBR (Sequencing Batch Reactor 099140871 Form No. A0101 No. 51 1 / Total 79 Pages 0993446280-0 [0193] 201221484 [0194] 0195] [0196] 099140871

Activaten Sludge process)池，也可以為沉澱池。 SBR是序批式活性污泥法，好氡池的人水緊貼池底由過水 洞進入SBR池，污水透過SBR池中的污泥層出水時，涔泥 層能夠起到過濾和截留的剌，降低了出水巾懸浮物的 含量，使得出水水質優於普通二沉池Μ水。本發明還 採用空㈣控制出水，防止曝氣期間的懸浮物進入出水 堰從而可有效地控制出水懸浮物。 SBR池與厭氡池之間連接有污泥回流管路，厭氧池、好氧 池和SBR池组成〇SA (Gxic—SettHng—^㈣工 藝，即好氧-沉澱-厭氧法，是在常規的活性污泥法中設 置一個厭氧段’使微生物交替進人好氧和厭氧環境，細 菌在好氧階段所獲ATP不能立即用於合成新的細胞，而是 錄氧段作為維持細胞生命活動的能量被消耗微生物 分解和合成代謝相對分離，Μ像通常條件下緊密偶聯 ，從而達到污泥減量的效果'0SA工藝能夠使污泥產生量 下降’改善污泥的沉降性能，增加脫除氨氮的能力。 SBR池與高濃度污泥反應池之間連接有剩餘污泥管，產生 的剩餘污泥不外排，而是回流至前端的高濃度污泥反應 池0 為了 SBR池恒水位運行和迴圈連續排水，SBR池設為兩組 並聯運行°從高污泥負荷池到SBR池按照由高到低的位置 依次串聯佈置’使得污水能夠依靠重力自流，減少污水 提升次數’節約電能；且各個處理單元採用組合式連體 結構’多池串聯推流，省去各處理單元之間大量的管路 和儀錶’還使污水在反應裝置中的流動呈現出整體推流 表單編號A0101 第52頁/共79頁 201221484 [0197] Ο [0198] [0199] Ο 099140871 而在不同區域内為完全混合的複雜流態，保證了處理效 果。 作為優選，污泥消解反應包括污水和污泥的混合液進行 高濃度污泥反應，高濃度污泥反應的水力停留時間為 1. 5h〜3. Oh，例如2h或2. 5h，出口溶解氧為lmg/L〜 1.5mg/L、1.5mg/L〜2mg/L、2mg/L〜2.5mg/L或2. 5mg/L〜3mg/L，污泥濃度為4000mg/L〜20000mg/L ，可具體為至少4000mg/L、至少6000mg/L、至少8000mg/L、至少 1 0000mg/L、至少 1 2000mg/L、至少 14000mg/L、至少 1 5000mg/L、至少 1 6000mg/L、至少 18000mg/L或至少 20000mg/L。 污泥消解反應還優選包括厭氧沉澱，對高濃度污泥反應 後的污水與污泥的混合液進行厭氧沉澱，經厭氧沉澱的 污泥回流參與高濃度污泥反應，回流比為0. 4Q〜0. 7Q，例如0· 5 Q或0. 6Q。 .3 [ 污泥和預處理後的污水的混合夜進行污泥消解反應，具 體為：先進入高濃度污泥反應池進行曝氣，同時將污水 與由SBR池回流的剩餘污泥以及厭氧沉殿池回流的污泥充 分混合。作為優選’刺餘污泥先在剩餘污泥曝氣池中進 行曝氣後再進入高濃度污泥反應池。剩餘污泥也可不曝 氣直接進入高濃度污泥反應池。厭氧沉澱池回流的污泥 直接進入高濃度污泥反應池。剩餘污泥優選全部回流至 高濃度污泥反應池，這樣可以達到零排放的效果。在剩 餘污泥曝氣池中溶解氧含量為〇. 2mg/L〜0. 9mg/L，如 0.3mg/L、0. 4mg/L、0. 5mg/L、〇. 6mg/L、0. 7mg/L、 表單编號A0101 第53頁/共79頁 0993446280-0 201221484 0. 8mg/L。污泥與污水混合後，污水中的有機物得到降解 並發生硝化反應，高濃度污泥反應池中水力停留時間為Activaten Sludge process) can also be a sedimentation tank. SBR is a sequential batch activated sludge method. The human water in the good pool is close to the bottom of the pool and enters the SBR pool through the water hole. When the sewage passes through the sludge layer in the SBR pool, the mud layer can be filtered and intercepted.剌, the content of suspended solids in the water towel is reduced, so that the effluent water quality is superior to that of the ordinary secondary sedimentation tank. The invention also adopts the air (four) to control the effluent to prevent the suspended solids during the aeration from entering the effluent enthalpy, thereby effectively controlling the water suspension. A sludge return line is connected between the SBR pool and the anaerobic tank, and the anaerobic tank, the aerobic tank and the SBR pool are composed of 〇SA (Gxic-SettHng-^(4) process, ie aerobic-precipitation-anaerobic method, which is conventional In the activated sludge process, an anaerobic section is set to make microorganisms alternate into aerobic and anaerobic environments. The ATP obtained by the bacteria in the aerobic phase cannot be used immediately to synthesize new cells, but the oxygen segment is used to maintain cell life. The activity energy is relatively separated by the consumption of microbial decomposition and anabolism, and the image is tightly coupled under normal conditions to achieve the effect of sludge reduction. The '0SA process can reduce the sludge production amount' to improve the sedimentation performance of the sludge and increase the removal. The capacity of ammonia nitrogen. The excess sludge pipe is connected between the SBR pool and the high-concentration sludge reaction tank, and the excess sludge generated is not discharged, but is returned to the front end of the high-concentration sludge reaction tank 0 for the SBR pool constant water level operation and Continuous circulation of the loop, the SBR pool is set to run in parallel in two groups. From the high sludge load pool to the SBR pool, the series arrangement from high to low position enables the sewage to rely on gravity to reduce the number of sewage lifts. Energy saving; and each processing unit adopts a combined connected structure 'multi-cell series push flow, eliminating a large number of pipelines and instruments between the processing units' also makes the flow of sewage in the reaction device present the overall push flow form number A0101 page 52 / page 79 201221484 [0197] 01 099140871 and in a different area for a fully mixed complex flow state, to ensure the treatment effect. As a preferred, sludge digestion reaction including sewage and sewage 5小时,出口的溶解氧为1mg/L~ 1.5mg/L, 1.5, the hydraulic retention time of the high-concentration sludge reaction is 1. 5h~3. Oh, for example 2h or 2. 5h, the outlet dissolved oxygen is lmg / L ~ 1.5mg / L, 1.5 Mg/L~2mg/L, 2mg/L~2.5mg/L or 2. 5mg/L~3mg/L, sludge concentration is 4000mg/L~20000mg/L, specifically at least 4000mg/L, at least 6000mg/ L, at least 8000 mg/L, at least 100 mg/L, at least 1 2000 mg/L, at least 14000 mg/L, at least 1 5000 mg/L, at least 1 6000 mg/L, at least 18000 mg/L or at least 20,000 mg/L. It is also preferred to include anaerobic precipitation to anaerobic the mixture of sewage and sludge after the reaction of the high-concentration sludge. The anaerobic precipitation of the sludge is carried out in a high-concentration sludge reaction, and the reflux ratio is 0. 4Q~0. 7Q, for example, 0·5 Q or 0. 6Q. .3 [mixing of sludge and pretreated sewage The sludge digestion reaction is carried out at night, specifically: first entering the high-concentration sludge reaction tank for aeration, and simultaneously mixing the sewage with the excess sludge returned from the SBR pool and the sludge returned from the anaerobic chamber. As a preferred 'sludge sludge, it is first aerated in the excess sludge aeration tank and then enters the high-concentration sludge reaction tank. The excess sludge can also enter the high-concentration sludge reaction tank without aeration. The sludge returned from the anaerobic sedimentation tank directly enters the high-concentration sludge reaction tank. The excess sludge is preferably all refluxed to a high-concentration sludge reaction tank, which achieves a zero-emission effect. The solution of dissolved oxygen in the excess sludge aeration tank is mg. 2mg / L~0. 9mg / L, such as 0.3mg / L, 0. 4mg / L, 0. 5mg / L, 〇. 6mg / L, 0. 7mg/L, Form No. A0101 Page 53 / Total 79 Page 0993446280-0 201221484 0. 8mg/L. After the sludge is mixed with the sewage, the organic matter in the sewage is degraded and nitrification occurs, and the hydraulic retention time in the high-concentration sludge reaction tank is

1. 5h〜3. Oh，如2h或2. 5h，污泥濃度為4000mg/L〜 20000mg/L，可具體為至少 4000mg/L、至少 600 0mg/L 、至少 8000mg/L、至少 10000mg/L、至少 12000mg/L、 至少 1 4000mg/L、至少 1 5000mg/L、至少 1 6000mg/L、 至少1 8000mg/L或至少20000mg/L。有獨立的污泥回流 ’厭氧沉殿池向南濃度污泥反應池回流污泥的回流比為 0. 4Q〜0. 7Q，例如0. 5 Q或0. 6Q，污泥濃度較高，為普 通活性污泥處理工藝的3〜5倍或更多倍，有效增強了該 系統的抗衝擊負荷能力。高濃度的活性污泥能有效分解 有機物，對水質、水量、pH值和有毒物質的衝擊有極好 的緩衝作用，同時也為後段穩定的處理效果提供了更為 可靠的保障。採用鼓風曝氣，出口溶解氧為lmg/L〜 1. 5mg/L 、1.5mg/L〜2mg/L ' 2mg/L~ 2. 5mg/L或 2.5mg/L〜3mg/L ° [0200] 由高濃度污泥反應池流出經去氧後污水進入厭氧沉澱池 ，同時厭氧沉澱池中沉澱的污泥與常規汙水處理產生的 剩餘污泥回流至高濃度污泥反應池，且厭氧沉澱池的回 流污泥為連續迴圈回流。高濃度污泥反應池中的混合污 泥始終經歷好氧、厭氧交替過程，好氧、厭氧微生物都 不能獲得優勢，最大程度的完成了剩餘污泥的水解過程 〇 [0201] 水解可將大分子有機物轉化為可生物降解的小分子有機 物，而在嚴格的厭氧條件下，將水解產生的小分子有機 099140871 表單編號A0101 第54頁/共79頁 0993446280-0 201221484 〇 物（rdcod生物降解）進一步轉化為VFAs (揮發性脂肪 酸），這些都是污泥水解產生出來“潛在”内碳源一有 機碳。有機碳可大幅度提高污水脫除氨氮效率，節省了 外加碳源。城市汙水處理廠由於碳源不足脫除氨氮效果 較差，這是城市汙水處理廠的普遍現象。在碳源豐富的 狀態下會產生能量洩露，即所謂的解偶聯現象，底物利 用率低。由於剩餘污泥回流，污泥停留時間無窮大，在 解偶聯的作用下能夠完成惰性物質的分解，化能自養菌 完成了剩餘污泥無機物消解，化能異養菌完成了剩餘污 泥有機物消解，系統不會出現情性物質的積累，從而實 現城市汙水處理廠剩餘污泥零，排放β經試驗，厭氧沉澱 池回流的污泥和常規汙水處理:產生的乘j餘污泥被大量消 化，能夠達到消長平衡，厭氣沉澱池扣S^R池都不向外排 泥’且反應穩定，達到了污泥的零排放。 [0202] 〇 污水由厭氧沉澱池流出後進入厭，氧池。厭氧沉澱池、厭 氧池和好氧池構成Α2/ύ工藝，污水在厭氧池中與經過常 規汙水處理產生的回流污泥混合，充分脫除氨氮，然後 污泥與污水的現合液一起進入好氧池中，通過好氧菌的 代謝作用將污水中的有機物進一步吸附、氧化和降解， 並發生硝化反應。 [0203] 最後污水經沉澱裝置沉澱後出水，沉澱裝置優選為SBR池 ，SBR池中污泥回流至厭氧池的回流比為〇. 5Q〜1Q，剩 餘污泥回流至高濃度污泥反應池中。由於進入SBR池的污 水已經有效地降解了水中的有機物，水質比較穩定’通 過SBR池的曝氣作用後，污水中有機物的降解更加徹底， 099140871 表單编號A0101 第55頁/共79頁 0993446280-0 201221484 且SBR池在週期靜止沉澱時會產生一個清晰的、高密度的 污泥層’該污泥層可以起到污泥篩檢程式的作用’對改 善出水品質和反硝化具有重要作用。SBR池中的污泥濃度 為2000mg/L〜4000mg/L，溶解氧含量為2mg/L〜4mg/L ，在一週期内SBR池中靜沉時間為lh〜1.5h，優選lh， 靜沉時，污水在池内進行反硝化和沉殿作用’恒水位排 水時間為1. 5h〜2.5h，優選2h。 [0204] 厭氧池、好氧池和Sbr池組成OSA工藝，回流污泥回流到 厭氧池，有效地抑制絲狀菌，防止出現污泥膨脹，改善 了污泥沉降性能，能夠減少污泥產生量。對於好氧微生 物’ ATP形成所需的能量來源於外部有機物基質的氧化過 粒’當好氧微生物處於厭氧條件時，由於有機物質的降 解情況與好氣降解的情況完全不同，戶斤釋放的能量大幅 度減少 巧泥本身沒有足夠的能量用於自身的增長，而 不仔不利用其體内儲存的ATP作為能源來供其正常的生理1. 5h~3. Oh, such as 2h or 2. 5h, sludge concentration is 4000mg / L ~ 20000mg / L, specifically at least 4000mg / L, at least 600 0mg / L, at least 8000mg / L, at least 10000mg / L At least 12000 mg/L, at least 1 4000 mg/L, at least 1 5000 mg/L, at least 1 6000 mg/L, at least 18000 mg/L or at least 20,000 mg/L. 5Q,0. 6Q, the sludge concentration is higher, the returning ratio of the returning sludge is 0. 4Q~0. 7Q, for example, 0. 5 Q or 0. 6Q, the sludge concentration is higher, It is 3 to 5 times or more of the ordinary activated sludge treatment process, which effectively enhances the impact load resistance of the system. The high concentration of activated sludge can effectively decompose organic matter, and has an excellent buffering effect on the impact of water quality, water quantity, pH value and toxic substances, and also provides a more reliable guarantee for the stable treatment effect in the latter stage. Using blast aeration, the outlet dissolved oxygen is 1mg/L~1. 5mg/L, 1.5mg/L~2mg/L '2mg/L~ 2. 5mg/L or 2.5mg/L~3mg/L ° [0200 The effluent from the high-concentration sludge reaction tank flows into the anaerobic sedimentation tank, and the sludge precipitated in the anaerobic sedimentation tank and the excess sludge generated by the conventional sewage treatment are returned to the high-concentration sludge reaction tank, which is irritating. The return sludge of the oxygen precipitation tank is continuously looped back. The mixed sludge in the high-concentration sludge reaction tank always undergoes aerobic and anaerobic alternating processes, and aerobic and anaerobic microorganisms cannot obtain the advantage, and the hydrolysis process of the excess sludge is completed to the utmost extent. [0201] Hydrolysis can be The macromolecular organic matter is converted into a biodegradable small molecule organic substance, and under strict anaerobic conditions, the small molecule organically produced by hydrolysis is 099140871 Form No. A0101 Page 54 / Total 79 Page 0993446280-0 201221484 Booty (rdcod biodegradation Further conversion to VFAs (volatile fatty acids), these are the "potential" internal carbon sources - organic carbon produced by sludge hydrolysis. Organic carbon can greatly improve the efficiency of ammonia removal from wastewater and save on additional carbon sources. Urban sewage treatment plants have a poor effect of removing ammonia nitrogen due to insufficient carbon sources, which is a common phenomenon in urban sewage treatment plants. Energy leakage occurs in a state rich in carbon sources, the so-called uncoupling phenomenon, and the substrate utilization rate is low. Due to the recirculation of excess sludge, the sludge residence time is infinite. Under the action of uncoupling, the decomposition of inert substances can be completed. The autotrophic bacteria complete the disintegration of excess sludge inorganic matter, and the heterotrophic bacteria complete the residual sludge organic matter. Dissolution, the system will not accumulate the accumulation of erotic substances, so that the surplus sludge of the municipal sewage treatment plant will be zero, the emission of β will be tested, the sludge returned by the anaerobic sedimentation tank and the conventional sewage treatment: the resulting excess sludge It is digested in a large amount and can achieve the balance of growth and depletion. The suffocating sedimentation tank deducts the S^R pool and does not discharge the sludge outwardly, and the reaction is stable, achieving zero discharge of sludge. [0202] 污水 The sewage flows out of the anaerobic sedimentation tank and enters the anaerobic pool. The anaerobic sedimentation tank, the anaerobic tank and the aerobic tank constitute a Α2/ύ process, and the sewage is mixed with the return sludge produced by the conventional sewage treatment in the anaerobic tank to fully remove the ammonia nitrogen, and then the sludge and the sewage are combined. The liquid enters the aerobic pool together, and the organic matter in the sewage is further adsorbed, oxidized and degraded by the metabolism of aerobic bacteria, and the nitrification reaction occurs. [0203] Finally, the sewage is precipitated by the sedimentation device, and the sedimentation device is preferably an SBR pool. The reflux ratio of the sludge in the SBR pool to the anaerobic tank is 〇. 5Q~1Q, and the excess sludge is returned to the high-concentration sludge reaction tank. . Since the sewage entering the SBR pool has effectively degraded the organic matter in the water, the water quality is relatively stable. After the aeration of the SBR pool, the degradation of organic matter in the sewage is more thorough, 099140871 Form No. A0101 Page 55 / 79 Page 0993446280- 0 201221484 And the SBR pool will produce a clear, high-density sludge layer during the period of static precipitation. The sludge layer can act as a sludge screening program', which plays an important role in improving the quality of the effluent and denitrification. The sludge concentration in the SBR pool is 2000mg/L~4000mg/L, and the dissolved oxygen content is 2mg/L~4mg/L. The sinking time in the SBR pool is 1h~1.5h, preferably lh, in the first period. 5小时至2.5小时,优选2小时。 The sewage in the pool for denitrification and sinking function 'constant water level drainage time is 1. 5h~2.5h, preferably 2h. [0204] The anaerobic tank, the aerobic tank and the Sbr pool constitute an OSA process, and the return sludge is returned to the anaerobic tank, which effectively inhibits the filamentous bacteria, prevents sludge expansion, improves sludge settling performance, and can reduce sludge. The amount produced. For aerobic microorganisms, the energy required for ATP formation is derived from the oxidized granules of the external organic matrix. When the aerobic microorganisms are under anaerobic conditions, the degradation of organic matter is completely different from that of aerobic degradation. Significantly reduce the mud itself does not have enough energy for its own growth, without using the ATP stored in the body as an energy source for its normal physiology

活動需要。因此，處於此@段的微生物纟田地内_存的ATP 將被大量消紅，i σ, 耗使万泥量呈減少的趨勢。這時若要進行 生物合成:微生物必須進行必要的能量儲存，如果細胞 内沒有足量的ΑΤΡ儲存，細胞自身的合成將不能繼續進行 因此已經>肖耗了大量ΑΤΡ的微生物再進人到營養豐富的 = 生物只能通過細胞的異化作用進行内源消 強對能量㈣求，㈣魏、好㈣交替增 ==起=量_大，產生量減 可生化性。'了水解酸化作用，增加了污水的 099140871 表單編號Α0101 第56夷/共79頁 0993446280-0 201221484 [0205] 因此，根據本發明的污泥處理裝置可以特別有利土 改造已有的各種活性污泥法汙水處理震置。，用於 例如在已右 汙水處理裝置附近增建根據本發明的污泥處理裝置有 已有汙水處理裝置的剩餘污泥作為污泥 將 * ™ ^ ^ ^ „ '弓丨Α該污泥 處理裝置，並且將该污泥處理裝置排出的上清液 水進水的一部分引入已有汙水處理裝置。2作為污 ^樣，利用太 發明的污泥處理裝置可以將已有汙水處理裝置的， ❹ 泥基本上完全消解使得改造後的汙水處理裝置旯=餘4 泥，同時含有大量可生物降解有機物的上清液也=不排 利於已有汙水處理裝置對氮和韻去除從而解決=有 足的問題，這對COD較低的城市生物污水尤為有利不 將污水進料改為從本發明的污泥處理装置弓丨‘''‘ 果Activity needs. Therefore, the ATP in the microbial field in this @ segment will be greatly reddened, i σ, which will reduce the amount of mud. At this time, if biosynthesis is to be carried out: the microorganisms must carry out the necessary energy storage. If there is not enough sputum stored in the cells, the synthesis of the cells themselves will not continue. Therefore, the microorganisms that have consumed a lot of cockroaches are re-entered into the nutrient-rich The organism can only use the alienation of cells to carry out internal weakening of energy (4), (4) Wei, good (four) alternately increase == start = quantity _ large, the amount of production minus biodegradability. 'Hydrochemical acidification, increased sewage 099140871 Form No. 1010101 56 夷 / / 79 pages 0993446280-0 201221484 [0205] Therefore, the sludge treatment device according to the present invention can be particularly advantageous for soil modification of existing activated sludge The sewage treatment is shocked. For example, in the vicinity of the right sewage treatment plant, the sludge treatment device according to the present invention is added with the excess sludge of the existing sewage treatment device as the sludge will be *TM ^ ^ ^ „ ' Processing the device, and introducing a part of the supernatant water discharged from the sludge treatment device into the existing sewage treatment device. 2 As a sewage sample, the existing sewage treatment device can be used by using the sludge treatment device of the invention The mud is basically completely digested so that the modified sewage treatment plant 旯=余 4 mud, and the supernatant containing a large amount of biodegradable organic matter is also not deducted from the existing sewage treatment device to remove nitrogen and rhyme. Solution = There is a problem, which is especially beneficial for urban bio-sewage with lower COD. The sewage feed is not changed from the sludge treatment device of the present invention.

*還可U 利用新建污泥處理裝置中高濃度的污泥來快迷高，〃 解污水進料中的污染物，進—步提高汗水處理效率^肖 里 [0206] 〇 [0207] [0208] [0209] 實施例1 : c; 在本文實施例中，符號t代表噸；⑽代表幹污泥；m3 立方米；d代表天；COD代表化學耗氧量。 表 裝置和設計參數： 根據本發明的污泥處理方法和污水生物處理方法，建設 了汙水處理能力為2〇〇〇〇m3/d的汙水處理廠，其工藝流程 如第11圖所示，其中高濃度污泥反應池（用於給氧處理 )、脫氣池和厭氧沉澱池（用於缺氧處理）構成了污泥 消解裝置（即根據本發明的污泥處理裝置），而厭氧池 099140871 表單編號A0101 第57頁/共79頁 0993446280-0 201221484 、好氧池和SBR池構成了常規汙水處理裝置（即根據本發 明汙水處理裝置中的污水生物處理設備）。來自污泥消 解裝置中厭氧沉澱池的污泥（即第一濃縮混合液，全部 用作第一混合液）、來自常規汙水處理裝置中SBR池的剩 餘污泥（即第二濃縮混合液，全部用作污泥進料）和經 格柵處理後的污水進水（即污水進料）混合得到第二混 合液。第二混合液在高濃度污泥反應池中經曝氣處理後 得到第三混合液。第三混合液進入脫氣池經去氧後進入 厭氧沉澱池，在厭氧沉澱池中經過沉澱處理（缺氧處理 )後得到的第四混合液已同時分離為處於上層的上清液 和處於下層的第一濃縮混合液。第一濃縮混合液作為污 泥回流經污泥回流管返回高濃度污泥反應池。上清液進 入常規汙水處理裝置，經厭氧池、好氧池和SBR池處理後 得到出水（即淨化出水）和剩餘污泥（即第二濃縮混合 液）。剩餘污泥經過剩餘污泥曝氣池曝氣後返回高濃度 污泥反應池。 [0210] 該汙水處理廠自2008年7月至今的運行情況表明，污泥產 率一直保持著基本為OtDS/(萬m3污水·(〇的水準，實現 了污泥的零排放。作為對比，處理類似污水的相鄰城市 汙水處理廠的產泥率通常為（1. 04〜1. 64) tDS/(萬m3污 水·天），平均為1.25七08八萬1113污水.d)。 [0211] 排放的淨化出水的水質可以參考從2008年9月到2009年5 月試驗得到的淨化出水的總量、COD、氨氮監測資料（見 表1)，其中高濃度污泥反應池的平均曝氣時間控制在 0. 2 5〜3. 5小時，厭氧沉澱池的沉澱時間控制在1〜5小 099140871 表單編號A0101 第58頁/共79頁 0993446280-0 201221484 時，曝氣時間與沉澱時間的比值控制在1 : 0. 8〜1 : 5之 間。在整個試驗期間，汙水處理裝置沒有排出任何污泥 [0212] 表1 : 2008年9月到2009年5月期間每月淨化出水的總量 、平均COD和平均氨氮資料*U can also use the high concentration of sludge in the new sludge treatment plant to quickly increase the concentration of pollutants in the sewage feed, and improve the efficiency of sweat treatment. ^肖里[0206] 〇[0207] [0208] Example 1 : c; In the examples herein, the symbol t represents tons; (10) represents dry sludge; m3 cubic meters; d represents days; COD represents chemical oxygen demand. Table device and design parameters: According to the sludge treatment method and the sewage biological treatment method of the present invention, a sewage treatment plant having a sewage treatment capacity of 2〇〇〇〇m3/d is constructed, and the process flow thereof is as shown in FIG. , wherein the high-concentration sludge reaction tank (for oxygen treatment), the degassing tank, and the anaerobic sedimentation tank (for anoxic treatment) constitute a sludge digestion device (ie, the sludge treatment device according to the present invention), and Anaerobic tank 099140871 Form No. A0101 Page 57 / Total 79 Page 0993446280-0 201221484 The aerobic tank and the SBR tank constitute a conventional sewage treatment device (ie, a sewage biological treatment device in the sewage treatment device according to the present invention). Sludge from the anaerobic sedimentation tank in the sludge digestion device (ie, the first concentrated mixture, all used as the first mixture), and the excess sludge from the SBR pool in the conventional sewage treatment device (ie, the second concentrated mixture) , all used as sludge feed) and mixed with the sewage treated sewage (ie sewage feed) to obtain a second mixture. The second mixture is subjected to aeration treatment in a high-concentration sludge reaction tank to obtain a third mixed liquid. The third mixed liquid enters the degassing tank and enters the anaerobic sedimentation tank after deoxidation, and the fourth mixed liquid obtained after the precipitation treatment (anoxic treatment) in the anaerobic sedimentation tank is simultaneously separated into the supernatant in the upper layer and The first concentrated mixture in the lower layer. The first concentrated mixture is returned as a sludge back to the high-concentration sludge reaction tank through the sludge return pipe. The supernatant is passed to a conventional sewage treatment unit, and treated with an anaerobic tank, an aerobic tank, and an SBR tank to obtain effluent (i.e., purified water) and excess sludge (i.e., a second concentrated mixture). The excess sludge is returned to the high-concentration sludge reaction tank after being aerated through the excess sludge aeration tank. [0210] The operation of the sewage treatment plant from July 2008 to the present shows that the sludge yield has been basically maintained at OtDS/(10,000 m3 of sewage (the level of 〇, achieving zero discharge of sludge. As a comparison) The sludge yield of the adjacent urban sewage treatment plants dealing with similar sewage is usually (1. 04~1. 64) tDS/(million m3 sewage·day), with an average of 1.2578 million 11113 sewage.d). [0211] The water quality of the purified effluent discharged can refer to the total amount of purified effluent obtained from September 2008 to May 2009, COD, ammonia nitrogen monitoring data (see Table 1), and the average of the high concentration sludge reaction tank. The aeration time is controlled at 0. 2 5~3. 5 hours, the precipitation time of the anaerobic sedimentation tank is controlled at 1~5 small 099140871 Form No. A0101 Page 58 / Total 79 Page 0993446280-0 201221484, aeration time and precipitation The ratio of time is controlled between 1: 0.8 and 1: 5. During the entire test period, the sewage treatment plant did not discharge any sludge [0212] Table 1: Monthly purification from September 2008 to May 2009 Total effluent, average COD and average ammonia nitrogen data

時間 淨化出水總量 平均COD濃度 平均氨氮濃度 (年/月） (m3/月） (mg/L) (mg/L ) 2008/9 453043 40.10 3.31 2008/10 321173 41.06 3.03 2008/11 375003 37.16 5.24 2008/12 384116 37.39 6.38 2009/1 331662 37.48 6.49 2009/2 377502 38.13 7.16 2009/3 301817 42.21 5.49 2009/4 288624 38.67 1.94 2009/5 72594 40.01 0.38 [0213] 《城鎮汙水處理廠污染物排放標準》GB1 8918-2002中規 定COD的最高允許排放濃度的一級B標準：60mg/L，氨氮 的最高允許排放濃度的一級B標準：水溫>12°C時為 8mg/L，水溫 12°C 時為 1 5 mg/L。 [0214] 由表1的監測資料可以看出，應用了本發明提供的城市汙 水處理系統，排放水中的COD和氨氮無論是氣溫低還是氣 溫高均達到了 GB1891 8-2002—級B標準。 [0215] 在2008年9月到2009年5月試驗中，還觀察到高濃度污泥 0993446280-0 099140871 表單編號A0101 第59頁/共79頁 201221484 反應池中的污泥濃度始終處於相當高的水準，見表2。 [0216] 表2 : 2008年9月到2009年5月期間高濃度污泥反應池中 第二混合液的污泥濃度的月平均值 時間（年/月） 高濃度污泥反應池中 污泥濃度的月平均值 (mg/L) 2008/9 6890 2008/10 8120 2008/11 14080 2008/12 17230 2009/1 18230 2009/2 15980 2009/3 13060 2009/4 12240 2009/5 7850 [0217] 為了進一步考察污泥消解裝置（即污泥處理裝置）的運 行情況，測定了污水進料、第二混合液水相和上清液的 COD、氨氮以及總磷含量，見表3。 [0218] 表3 :在不同時間分別測定的污水進料、第二混合液水相 和上清液的COD、氨氮以及總磷含量值（mg/L) 099140871 表單編號A0101 第60頁/共79頁 0993446280-0 201221484 [0219] 〇 時間 污水進料 第二混合液水相 上清液 (月/日） COD 氨氮 總磷 COD 氨氮 總磷 COD 氨氮 總磷 2010/4/11 618.30 89.93 13.20 509.97 128.31 23.89 350.02 126.99 15.57 2010/4/12 688 70.22 10.21 391 85.96 13.65 348 85.07 8.56 2010/4/13 254 38.6 4.2 275 78.9 12.5 86 52.9 5.02 2010/4/14 314.82 66.25 3.41 154.48 94.78 6.22 109.50 78.31 3.54 2010/4/18 361.34 57.87 18.95 346.11 42.87 18.95 1 13.29 48.90 11.12 由表3可見，從污泥消解裝置排出的上清液中的COD、氨 氮和總攝顯著地比第二混合液水相的相應值低。對於本 實施例的污泥消解裝置而言，污水進料和污泥進料是其 淨輸入，除了上清液之外沒有污泥或其他的固體或液體 輸出，並且污泥消解裝置中也沒有發現污泥的積累，因 此污水進料和污泥進料所帶來的生物體和固體物除了部 分轉化為可隨上清液排出的形式外，其餘部分都在污泥 消解裝置中得到了消解，由此實現了:斜餘t倉泥的減量化 。不受任何理論約束，可以認為消解的生物體和固體物 在污泥消解裝置中轉化為氣體形式而逸出。就整個汙水 處理裝置而言，污水進料中的污染物質（主要以C0D、氨 氮和總磷表示）在汙水處理裝置中轉化為氣態物質而逸 出，因此在得到淨化出水的同時沒有污泥和其他固體或 液體物質排出。 [0220] 實施例2 : [0221] 根據本發明的污泥處理方法和污水生物處理方法，改造 了 一座以MSBR (即A2/0後接SBR)工藝運行的現有汙水 099140871 表單編號A0101 第61頁/共79頁 0993446280-0 201221484 處理廠。改造後的汙水處理廠的汙水處理能力為 20 00 0m3/d，其工藝流程也可以用第11圖表示，其中各 項參數與實施例1的相同。 [0222] 改造後的汙水處理廠已經運行了一年多，污泥產率基本 為OtDS/(萬m3污水*d)，同樣基本實現了污泥的零排放 ，且COD冬季平均排放濃度為24. 3 mg/L，夏季平均排放 濃度為27.56 mg/L，氨氮冬季平均排放濃度為 8. 85mg/L，夏季平均排放濃度為4. 07 mg/L，達到了 GB1 8918-2002 — 級 B 標準。 [0223] 使用本發明提供的污泥處理方法，新建汙水處理系統或 是通過對現有的常規汙水處理裝置進行改造，將高濃度 污泥反應、厭氧沉澱和常規汙水處理工藝結合來處理污 水，均能夠改善污泥的沉降性能，抑制污泥膨脹，實現 剩餘污泥的消解，使得整個汙水處理系統產生的剩餘污 泥減量甚至達到污泥零排放。 - [0224] 以上對本發明所提供的污泥減量化汙水處理系統及方法 進行了詳細介紹。說明書和權利要求中描述方法時用於 指代各個步驟的編號，除非特別指明或經上下文能夠唯 一確定之外，並不代表各個步驟的順序。本文中應用了 具體個例對本發明的原理及實施方式進行了闡述，以上 實施例的說明只是用於幫助理解本發明的方法及其核心 思想。應當指出，對於本技術領域的普通技術人員來說 ，在不脫離本發明原理的前提下，還可以對本發明進行 若干改進和修飾，這些改進和修飾也落入本發明權利要 求的保護範圍内。 099140871 表單編號A010] 第62頁/共79頁 0993446280-0 201221484 【圖式簡單說明】 [0225] ΟTime Purified effluent total average COD concentration Average ammonia nitrogen concentration (year/month) (m3/month) (mg/L) (mg/L) 2008/9 453043 40.10 3.31 2008/10 321173 41.06 3.03 2008/11 375003 37.16 5.24 2008 /12 384116 37.39 6.38 2009/1 331662 37.48 6.49 2009/2 377502 38.13 7.16 2009/3 301817 42.21 5.49 2009/4 288624 38.67 1.94 2009/5 72594 40.01 0.38 [0213] "Emission Standards for Pollutants in Municipal Wastewater Treatment Plants" GB1 The primary B standard for the maximum allowable emission concentration of COD specified in 8918-2002: 60 mg/L, the first B standard for the maximum allowable emission concentration of ammonia nitrogen: water temperature > 8 mg/L at 12 ° C, and water temperature 12 ° C It is 1 5 mg/L. It can be seen from the monitoring data of Table 1 that the urban sewage treatment system provided by the present invention applies the COD and ammonia nitrogen in the discharged water to the GB1891 8-2002-class B standard whether the temperature is low or the gas temperature is high. [0215] In the test from September 2008 to May 2009, high-concentration sludge was also observed. 0993446280-0 099140871 Form No. A0101 Page 59 / Total 79 Page 201221484 The sludge concentration in the reaction tank is always quite high. Level, see Table 2. Table 2: Monthly mean time (year/month) of sludge concentration of the second mixture in the high-concentration sludge reaction tank from September 2008 to May 2009. Sludge in the high-concentration sludge reaction tank Monthly mean of concentration (mg/L) 2008/9 6890 2008/10 8120 2008/11 14080 2008/12 17230 2009/1 18230 2009/2 15980 2009/3 13060 2009/4 12240 2009/5 7850 [0217] Further investigate the operation of the sludge digestion device (ie sludge treatment device), and determine the COD, ammonia nitrogen and total phosphorus content of the sewage feed, the second mixed liquid aqueous phase and the supernatant, as shown in Table 3. Table 3: COD, Ammonia Nitrogen and Total Phosphorus Content (mg/L) of the sewage feed, the second mixed liquid aqueous phase and the supernatant, respectively, measured at different times. 099140871 Form No. A0101 Page 60 of 79 Page 0993446280-0 201221484 [0219] 〇 time sewage feed second mixture aqueous phase supernatant (month/day) COD ammonia nitrogen total phosphorus COD ammonia nitrogen total phosphorus COD ammonia nitrogen total phosphorus 2010/4/11 618.30 89.93 13.20 509.97 128.31 23.89 350.02 126.99 15.57 2010/4/12 688 70.22 10.21 391 85.96 13.65 348 85.07 8.56 2010/4/13 254 38.6 4.2 275 78.9 12.5 86 52.9 5.02 2010/4/14 314.82 66.25 3.41 154.48 94.78 6.22 109.50 78.31 3.54 2010/4/18 361.34 57.87 18.95 346.11 42.87 18.95 1 13.29 48.90 11.12 As can be seen from Table 3, the COD, ammonia nitrogen and total exposure in the supernatant discharged from the sludge digestion unit are significantly lower than the corresponding values of the second mixed liquid aqueous phase. For the sludge digestion apparatus of the present embodiment, the sewage feed and the sludge feed are net inputs, and there is no sludge or other solid or liquid output other than the supernatant, and there is no sludge digestion device. The accumulation of sludge was found, so that the biological and solid materials brought by the sewage feed and sludge feed were partially converted into a form that can be discharged with the supernatant, and the rest were digested in the sludge digestion device. Thus, the realization of the reduction of the sloping t-bark mud is achieved. Without being bound by any theory, it is believed that the digested organisms and solids are converted to gaseous form and escape in the sludge digestion unit. As far as the entire sewage treatment plant is concerned, the pollutants in the sewage feed (mainly represented by COD, ammonia nitrogen and total phosphorus) are converted into gaseous substances in the sewage treatment device and escape, so that there is no pollution at the same time as the purified water is obtained. Mud and other solid or liquid substances are discharged. Example 2: [0221] According to the sludge treatment method and the sewage biological treatment method of the present invention, an existing sewage which is operated by MSBR (ie, A2/0 followed by SBR) process is modified. 099140871 Form No. A0101 No. 61 Page / Total 79 pages 0993446280-0 201221484 Treatment plant. The sewage treatment capacity of the modified sewage treatment plant is 20000 m3/d, and the process flow can also be represented by Fig. 11, wherein each parameter is the same as that of the first embodiment. [0222] The modified sewage treatment plant has been in operation for more than a year. The sludge yield is basically OtDS/(10,000 m3 sewage*d), and the zero discharge of sludge is basically achieved, and the average COD emission concentration in winter is 24. 3 mg / L, the average summer emission concentration is 27.56 mg / L, the average ammonia ammonia concentration in winter is 8. 85mg / L, the average summer emission concentration is 4. 07 mg / L, reached GB1 8918-2002 - Grade B standard. [0223] Using the sludge treatment method provided by the present invention, a new sewage treatment system is newly added or a conventional sewage treatment device is modified to combine high-concentration sludge reaction, anaerobic precipitation and conventional sewage treatment processes. The treatment of sewage can improve the sedimentation performance of the sludge, inhibit the sludge expansion, and realize the digestion of the excess sludge, so that the excess sludge generated by the entire sewage treatment system can even reduce the sludge discharge. [0224] The sludge reduction sewage treatment system and method provided by the present invention are described in detail above. The number of the steps used in the description and the claims are intended to refer to the individual steps, and the order of the individual steps is not to be construed unless the context is specified. The principles and embodiments of the present invention have been described herein with reference to specific examples. The description of the embodiments above is only to aid in understanding the method of the present invention and its core concepts. It should be noted that those skilled in the art can make various modifications and changes to the present invention without departing from the spirit and scope of the invention. 099140871 Form No. A010] Page 62 of 79 0993446280-0 201221484 [Simple Description] [0225] Ο

第1圖為現有技術中傳統活性污泥法的工藝流程示意圖。 第2圖為根據本發明污泥處理方法的一種實施方式的工藝 流程示意圖。 第3圖為根據本發明污水生物處理方法或污泥減量化污水 (生物）處理方法的一種實施方式的工藝流程示意圖。 第4圖示出根據本發明污水生物處理方法或污泥減量化污 水生物處理方法的另一種實施方式的工藝流程的示意圖 〇 第5圖為可用於本發明污水生物處理方法的氧化溝汙水處 理工藝的流程圖。 第6圖為可用於本發明污水生物處理方法的SBR汙水處理 工藝的流程圖。 第7圖為可用於本發明污水生物處理方法的ΑΒ法汙水處理 工藝的流程圖。 第8圖為可用於本發明污水生物處理方法的A/Ο法汙水處 理工藝的流程圖。 第9圖為可用於本發明污水生物處理方法的Α20法汙水處 理工藝的流程圖。 第10圖為可用於本發明污水生物處理方法的MSBR汙水處 理工藝的流程圖。 第11圖示出根據本發明污水生物處理方法的一種實施方 式的工藝流程的示意圖。 第12圖示出根據本發明污水生物處理方法的一種實施方 式的工藝流程的示意圖。 第13圖示出根據本發明污水生物處理方法的一種實施方 099140871 表單編號Α0101 第63頁/共79頁 0993446280-0 201221484 式的工藝流程的不意圖。 【主要元件符號說明】 [0226]無 099140871 表單編號A0101 第64頁/共79頁 0993446280-0Fig. 1 is a schematic view showing the process flow of the conventional activated sludge process in the prior art. Fig. 2 is a schematic view showing the process flow of an embodiment of a sludge treatment method according to the present invention. Fig. 3 is a schematic view showing the process flow of an embodiment of a sewage biological treatment method or a sludge reduction sewage (biological) treatment method according to the present invention. 4 is a schematic view showing a process flow of another embodiment of a sewage biological treatment method or a sludge reduction sewage biological treatment method according to the present invention. FIG. 5 is an oxidation ditch sewage treatment which can be used in the biological biological treatment method of the present invention. Process flow chart. Figure 6 is a flow diagram of an SBR wastewater treatment process that can be used in the sewage biological treatment process of the present invention. Fig. 7 is a flow chart showing the hydrazine sewage treatment process which can be used in the sewage biological treatment method of the present invention. Fig. 8 is a flow chart showing the A/Ο method of sewage treatment which can be used in the sewage biological treatment method of the present invention. Fig. 9 is a flow chart showing the Α20 method sewage treatment process which can be used in the sewage biological treatment method of the present invention. Figure 10 is a flow diagram of a MSBR wastewater treatment process that can be used in the sewage biological treatment process of the present invention. Figure 11 is a schematic view showing the process flow of an embodiment of the biological treatment method for sewage according to the present invention. Fig. 12 is a schematic view showing the process flow of an embodiment of the biological treatment method for sewage according to the present invention. Figure 13 is a schematic illustration of the process flow of a method for treating biological wastewater according to the present invention. 099140871 Form No. 1010101 Page 63 of 79 Form 0993446280-0 201221484. [Main component symbol description] [0226] None 099140871 Form No. A0101 Page 64 of 79 0993446280-0

Claims (1)

201221484 七、申請專利範圍： 1 . 一種污泥處理方法，包括以下步驟： (1 )將來自污水生物處理過程的污泥進料與第一混合液 ^ 混合得到第二混合液； • ( 2 )將第二混合液進行給氧處理得到第三混合液； (3) 將第三混合液進行缺氧處理得到第四混合液； (4) 將第四混合液分離得到上清液和第一濃縮混合液； 以及 (5) 將上清液排出，並且將至少部分第一濃縮混合液返 〇 回步驟（1 )用作第一混合液，其中未返回步驟（1 )的第 一濃縮混合液的污泥量小於污泥進料的污泥量。 2 .如申請專利範圍第1項所述之污泥處理方法，在步驟（5) . 中，將至少60%、優選至少65%、更優選至少70%、更 優選至少75%、更優選至少80%、更優選至少85%、更 優選至少90%、更優選至少93%、更優選至少95%、更 優選至少98%、最優選基本上100%的第一濃縮混合液返 回步驟（1)用作第一混合液，並且任選地將未返回步驟 (1 )的第一濃縮混合液排出。 3 .如申請專利範圍第1至2項中任一項所述之污泥處理方法， 在步驟（1 )中，將有機營養物、污泥進料和第一混合液 混合得到第二混合液，所述有機營養物優選為污水進料。 4 .如申請專利範圍第3項所述之污泥處理方法，其中步驟（1 ' )中污泥進料與污水進料的流量比為1:0. 01〜1:100， 優選1:0. 1〜1:10,更優選為1:0. 5〜1:5。 5 .如申請專利範圍第1至4項中任一項所述之污泥處理方法， 099140871 表單編號Α0101 第65頁/共79頁 0993446280-0 201221484 其中步驟（2)的給氧處理時間為〇1〜4小時，優選〇. 5 〜2小時，更優選〇. 5〜1. 5小時。 .如申請專利範圍第丨至5項中任1所述之污泥處理方法， 其中步驟（3)的缺氡處理時間為〇 8〜6小時，優選 小時，更優選1〜3小時。 ‘如申请專利顧第1至6項中任-項所述之污泥處理方法， 其中給氧處理時間與缺氧處理時間的比為1:〇 5〜1:6， 優選11〜1:3，更優選1:1.5〜1:2，最優選1:2。 .如申凊專利fe圍第1至7項中任一項所述之污泥處理方法， 其中步驟（2)的給氧處理以間歇曝氣或連續曝氣的方式 進行。 9 .如申請專利範圍第丨至8項中任一項所述之污泥處理方法， 其中在步驟（2)中，第三混合液的溶解氧滚度為〇1〜 4mg/L，優選 1. 5〜3mg/L，更優選2〜3mg/L。 如申明專利範圍第1至9項中任—項所述之污泥處理方法， 其中步驟（3 )和步驟（4 ) ¾沉澱方式進行。 11 .如申請專利範園第1至1〇項中任^項辧4之污泥處理方法 ，其中在步驟（1)中，第立混合液的污泥濃度為3〇〇〇〜 30000mg/L，優選3〇〇〇〜2〇〇〇〇mg/L，更優選4〇〇〇〜 150〇〇mg/L 。 12 13 如申凊專利範圍第1至丨丨項中任一項所述之污泥處理方法 還包括回收步驟（2)和/或（3)中產生的氣態含磷化 合物的回收步驟。 一種污水生物處理方法，包括： (1 )將來自污水生物處理過程的污泥進料和第一混合液 混合得到第二混合液； 099140871 表單編號 A0101 g 66 I/* 79 I 0993446280-0 201221484201221484 VII. Patent application scope: 1. A sludge treatment method comprising the following steps: (1) mixing a sludge feed from a sewage biological treatment process with a first mixed liquid to obtain a second mixed liquid; (2) The second mixture is subjected to oxygen treatment to obtain a third mixture; (3) the third mixture is subjected to anoxic treatment to obtain a fourth mixture; (4) the fourth mixture is separated to obtain a supernatant and a first concentration Mixing liquid; and (5) discharging the supernatant, and returning at least a portion of the first concentrated mixture back to step (1) for use as the first mixed liquid, wherein the first concentrated mixed liquid of step (1) is not returned The amount of sludge is less than the amount of sludge fed by the sludge. 2. The sludge treatment method according to claim 1, wherein in the step (5), at least 60%, preferably at least 65%, more preferably at least 70%, more preferably at least 75%, more preferably at least 80%, more preferably at least 85%, more preferably at least 90%, more preferably at least 93%, more preferably at least 95%, more preferably at least 98%, most preferably substantially 100% of the first concentrated mixture is returned to step (1) Used as the first mixed liquid, and optionally discharges the first concentrated mixed liquid that has not returned to the step (1). 3. The sludge treatment method according to any one of claims 1 to 2, wherein in step (1), the organic nutrient, the sludge feed and the first mixture are mixed to obtain a second mixture. The organic nutrient is preferably a sewage feed. The ratio of the sludge feed to the sewage feed in the step (1 ') is 1:0. 01~1:100, preferably 1:0. 1〜1:10, more preferably 1:0. 5~1:5. 5. The sludge treatment method according to any one of claims 1 to 4, 099140871 Form No. 1010101, page 65/79, 0993446280-0 201221484 wherein the oxygen treatment time of the step (2) is 〇 5〜1. 5小时。 1~4 hours, preferably 〇. 5~2 hours, more preferably 〇. 5~1. 5 hours. The sludge treatment method according to any one of claims 1 to 5, wherein the defect treatment time of the step (3) is 〇 8 to 6 hours, preferably hours, more preferably 1 to 3 hours. The sludge treatment method according to any one of the preceding claims, wherein the ratio of the oxygen treatment time to the anoxic treatment time is 1: 〇5~1:6, preferably 11~1:3 More preferably, it is 1:1.5 to 1:2, and most preferably 1:2. The sludge treatment method according to any one of items 1 to 7, wherein the oxygen supply treatment of the step (2) is carried out by intermittent aeration or continuous aeration. The sludge treatment method according to any one of the preceding claims, wherein in the step (2), the dissolved oxygen rolling degree of the third mixed liquid is 〇1 to 4 mg/L, preferably 1 5~3mg/L, more preferably 2~3mg/L. The sludge treatment method according to any one of claims 1 to 9, wherein the step (3) and the step (4) are carried out in a precipitation manner. 11. The method for treating sludge according to any one of items 1 to 1 of the patent application, wherein in the step (1), the sludge concentration of the first mixture is 3 〇〇〇 to 30000 mg/L. Preferably, it is 3 〇〇〇 to 2 〇〇〇〇 mg/L, more preferably 4 〇〇〇 to 150 〇〇 mg/L. The sludge treatment method according to any one of claims 1 to 3, further comprising the step of recovering the gaseous phosphorus-containing compound produced in the steps (2) and/or (3). A sewage biological treatment method comprising: (1) mixing a sludge feed from a sewage biological treatment process with a first mixed liquid to obtain a second mixed liquid; 099140871 Form No. A0101 g 66 I/* 79 I 0993446280-0 201221484 14 15 (2)將第二混合液進行給氧處理得到第三混合液； ⑴將第三混合液進行缺氧處理得到第四混合液； ⑷將第喊合液分離㈣上清液和第—濃縮混合液； ⑴將上清輯出，並絲至少部分第n混合液返 畔驟⑴时第—混合液’其中未返回步驟⑴的第 —濃縮混合液的污泥量小於污泥進料的污泥量； (6)將至少部分步驟⑴的上清液和任選的部分污水進 料進行污水生物處料到第二㈣混合液和淨化出水；以 ⑺將淨化出水排出，並且耗地將至少部分步驟⑷ 的第二濃縮混合液返回步驟)用作污泥進料； 其中將污水進料在㈣⑴中與污泥進料和第—混合液 混合得到第二混合液和/或在步驟⑷巾與所述至少部分 步驟（5)的上清液一起進行污水生物處理，優選將至少 部分污水進料在步驟⑴中與污泥進料和第—混合液混 合得到第二混合液，更優選將全部污水進料在步驟（1 ) 中與污泥進料和第一混合液混合得到第二混合液。 如申請專鄉时13項所収污水生物處理方法，在步驟 (5)中，將至少60%、優選至少65%、更優選至少7〇% 更優選至少75%、更優選至少8〇%、更優選至少π% 、更優選至少90%、更優選至少93%、更優選至少95% 、更優選至少98%、最優選基本上ι〇0%的第一濃縮混合 液返回步驟（1)用作第一混合液，並且任選地將未返回 步驟〇)的第一濃縮混合液排出。 如申請專利範圍第13至14項中任一項所述之污水生物處 099140871 理方法，其中步驟（2)的給氧處理時間為〇. 1〜4小時， 表單編號A0101 第67頁/共79頁 0993446280-0 201221484 優選0. 5〜2小時，更優選〇. 5〜1. 5小時。 16 ·如申請專利範圍第13至15項中任一項所述之污水生物處 理方法’其中步驟（3)的缺氧處理時間為0. 8〜6小時， 優選1〜4小時，更優選1〜3小時。 17 -Λ, ’如申請專利範圍第13至16項所述之污水生物處理方法， 其中給氧處理時間與缺氧處理時間的比為1:〇. 5〜1:6， 優選1:1〜1:3,更優選1:1. 5〜1:2’最優選1:2。 8 .如申凊專利範圍第13至17項中任一項所述之污水生物處 理方法，其中步驟（2)的給氧處理以間歇曝氣或連續曝 氣的方式進行。 19 ·如申請專利範圍第13至18項中任一項所述之污水生物處 理方法，其中在步驟（2)中，第三.混合液的溶解氧濃度 為〇. 1〜4mg/L，優選1. 5〜3mg/L，更優選2〜3mg/L。 20 .如申請專利範圍第13至19項中任一項所述之污水生物處 理方法，其中步驟（3)和步驟（4)以沉澱方式進行。 21 ·如申請專利範圍第13至2〇項令任一項所述之污水生物處 理方法，其中在步驟⑴中，第二混合液的污泥濃度為 3000〜30000mg/L，優選3000〜2〇〇〇〇mg/L，更優選 4000〜150〇〇mg/L 〇 22 .如巾請專利範圍第13至21項中任—項所述之污水生物處 理方法，還包括回收步驟⑴和/或（3)中產生的氣態 含磷化合物的回收步驟。 23 . 如申請專利範_13至22項中任_賴述之污水生物處 理方法，其中步驟⑺中返回步驟（1)用作污泥進料的 第一濃縮混β液占第一潰縮混合液的比例為1〜1 〇⑽優 選约80〜〗00%，更優選約丨〇〇%。 099140871 表單編號Α0101 第68頁/共79頁 0993446280-0 201221484 24 . 25 . ❹ 26 . Ο 27 . 如申請專利範圍第13至23項中任一項所述之污水生物處 理方法，其中步驟（7)中返回步驟（1 )的第二濃縮混合 液占步驟（1)的污泥進料的比例為1〜100%，優選約80 〜100%，更優選約100%。 如申請專利範圍第13至24項中任一項所述之污水生物處 理方法，其中步驟（6 )是選自根據Wuhrmann工藝、A/0 工藝、Bardenpho工藝、Phoredox工藝、A2/0工藝、倒 置A2/0工藝、UCT工藝、MUCT工藝、VIP工藝、0WASA工 藝、JHB工藝、TNCU工藝、Dephanox工藝、BCFS工藝、 MSBR工藝、SBR工藝、AB工藝、氧化溝工藝、生物膜工藝 、流動床工藝或其組合的污水生物處理步驟。 一種用於如申請專利範圍第1至12項中任一項的污泥處理 方法的污泥處理裝置，包括：能夠將污水進料、污泥進料 與第一混合液混合得到第二混合液的第一設備；能夠將第 二混合液進行給氧處理得到第三混合液的第二設備；能夠 將第三混合液進行缺氧處理得到第四混合液的第三設備； 能夠將第四混合液分離得到上清液和第一濃縮混合液的第 四設備；能夠將上清液排出的第五設備；能夠將至少部分 第一濃縮混合液作為第一混合液引入第一設備並且使未返 回第一設備的第一濃縮混合液的污泥量小於污泥進料的污 泥量的第六設備。 如申請專利範圍第26項所述之污泥處理裝置，其中第二設 備經設置使得給氧處理時間為0. 1〜4小時，優選0.5〜2 小時，更優選〇. 5〜1. 5小時。 如申請專利範圍第26至27項中任一項所述之污泥處理裝 置，其中第三設備經設置使得缺氧處理時間為0. 8〜6小 099140871 表單編號A0101 第69頁/共79頁 0993446280-0 28 . 201221484 時，優選1〜4小時，更優選1〜3小時。 29 .如申請專利範圍第26至28項中任一項所述之污泥處理裝 置，其中第二設備和第三設備經設置使得給氧處理時間與 缺氧處理時間的比為1:0. 5〜1:6，優選1:1〜1:3 ’更優 選1:1. 5〜1:2，最優選1:2。 30 .如申請專利範圍第26至29項中任一項所述之污泥處理裝 置，其中第二設備是曝氣池。 31 .如申請專利範圍第26至30項中任一項所述之污泥處理裝 置，其中第三設備和第四設備是沉澱池。 32 .如申請專利範圍第26至31項中任一項所述之污泥處理裝 置，其中所述污泥處理裝置還包括能夠收集並回收氣態含 填化合物的回收設備。 33 . —種用於如申請專利範圍第13至15項中任一項的污水生 物處理方法的污水生物處理裝置，包括：能夠將污泥進料 與第一混合液混合得到第二混合液的第一設備；能夠將第 二混合液進行給氧處理得到第三混合液的第二設備；能夠 將第三混合液進行缺氧處理得到第四混合液的第三設備； 能夠將第四混合液分離得到上清液和第一濃縮混合液的第 四設備；能夠將上清液排出的第五設備；能夠將至少部分 第一濃縮混合液作為第一混合液引入第一設備並且使未返 回第一設備的第一濃縮混合液的污泥量小於污泥進料的污 泥量的第六設備；能夠將至少部分第五設備排出的上清液 進行污水生物處理得到第二濃縮混合液和淨化出水的第七 設備；能夠將淨化出水排出的第八設備；能夠將污水進料 引入第一設備和/或第七設備的第九設備；以及任選的能 夠將至少部分第二濃縮混合液引入第一設備的第十設備。 099140871 表單編號 A0101 第 70 頁/共 79 頁 0993446280-0 201221484 34 .如申請專利範圍第33項所述之污水生物處理裝置’其中第 二設備經設置使得給氧處理時間為〇. 1〜4小時’優選〇. 5 〜2小時’更優選〇. 5〜1. 5小時。 35 .如申請專利範圍第33至34項中任一項所述之污水生物處 理裝置’其中第三設備經設置使得缺氧處理時間為0. 8〜 6小時，優選1〜4小時，更優選1〜3小時。 36 .如申請專利範圍第33至35項中任一項所述之污水生物處 理裝置’其中第二設備和第三設備經設置使得給氧處理時 〇 37 . 38 . ' 39 .14 15 (2) The second mixture is subjected to oxygen treatment to obtain a third mixture; (1) the third mixture is subjected to anoxic treatment to obtain a fourth mixture; (4) the first liquid is separated (4) and the first solution is separated. Concentrating the mixture; (1) arranging the supernatant, and at least part of the nth mixture is returned to the side (1), the first mixture is not returned to the first concentrated mixture of step (1), the amount of sludge is less than the sludge feed The amount of sludge; (6) at least part of the supernatant of step (1) and optionally part of the sewage feed is discharged into the second (four) mixture and purified water; (7) the purified water is discharged, and the consumption will be At least part of the second concentrated mixture returning step (4) is used as a sludge feed; wherein the sewage feed is mixed with the sludge feed and the first mixed liquid in (4) (1) to obtain a second mixed liquid and/or in step (4) The towel is subjected to sewage biological treatment together with the supernatant of the at least part of the step (5), preferably at least part of the sewage feed is mixed with the sludge feed and the first mixed liquid in the step (1) to obtain a second mixed liquid, more preferably Feed all the sewage in step (1) Mixing with the sludge feed and the first mixture to obtain a second mixture. If the sewage biological treatment method is 13 in the application for the hometown, in the step (5), at least 60%, preferably at least 65%, more preferably at least 7%, more preferably at least 75%, more preferably at least 8%, more Preferably at least π%, more preferably at least 90%, more preferably at least 93%, more preferably at least 95%, more preferably at least 98%, most preferably substantially 〇0% of the first concentrated mixture is returned to step (1) for use as The first mixed liquid, and optionally the first concentrated mixed liquid that has not returned to step 〇). The method of treating a sewage biological unit according to any one of claims 13 to 14, wherein the oxygen supply treatment time of the step (2) is 〇. 1 to 4 hours, the form number A0101, page 67/total 79 5〜1. 5小时。 The page 0993446280-0 201221484 is preferably 0. 5~2 hours, more preferably 〇. 5~1. 5 hours. The anaerobic treatment time of the step (3) is 0. 8~6 hours, preferably 1 to 4 hours, more preferably 1 ~3 hours. 17 - Λ, 'The sewage biological treatment method according to claim 13 to 16, wherein the ratio of the oxygen treatment time to the anoxic treatment time is 1: 〜. 5~1:6, preferably 1:1~ 1:3, more preferably 1:1. 5~1:2' is most preferably 1:2. The sewage biological treatment method according to any one of claims 13 to 17, wherein the oxygen supply treatment of the step (2) is carried out by intermittent aeration or continuous aeration. The biological treatment method for sewage according to any one of claims 13 to 18, wherein in the step (2), the dissolved oxygen concentration of the third mixture is 〇. 1 to 4 mg/L, preferably 1. 5 to 3 mg/L, more preferably 2 to 3 mg/L. The sewage biological treatment method according to any one of claims 13 to 19, wherein the step (3) and the step (4) are carried out in a precipitation manner. The sewage biological treatment method according to any one of claims 13 to 2, wherein in the step (1), the sludge concentration of the second mixed liquid is 3000 to 30000 mg/L, preferably 3000 to 2 Torr. 〇〇〇mg/L, more preferably 4000~150〇〇mg/L 〇22. The biological treatment method for sewage according to any one of the items of the present invention, including the recycling step (1) and/or The recovery step of the gaseous phosphorus-containing compound produced in (3). 23. The sewage biological treatment method according to any one of the patents _13 to 22, wherein the returning step (1) in the step (7) is used as the first concentrated mixed β liquid of the sludge feed to occupy the first crush mixing The ratio of the liquid is 1 to 1 Torr (10), preferably about 80 to 00%, more preferably about 丨〇〇%. 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 The ratio of the second concentrated mixture returned to the step (1) to the sludge feed of the step (1) is from 1 to 100%, preferably from about 80 to 100%, more preferably about 100%. The sewage biological treatment method according to any one of claims 13 to 24, wherein the step (6) is selected from the group consisting of a Wuhrmann process, an A/0 process, a Bardenpho process, a Phoredox process, an A2/0 process, and an inversion. A2/0 process, UCT process, MUCT process, VIP process, 0WASA process, JHB process, TNCU process, Dephanox process, BCFS process, MSBR process, SBR process, AB process, oxidation ditch process, biofilm process, fluidized bed process or Its combined sewage biological treatment step. A sludge treatment apparatus for a sludge treatment method according to any one of claims 1 to 12, comprising: capable of mixing a sewage feed, a sludge feed, and a first mixed liquid to obtain a second mixed liquid a first device capable of subjecting the second mixed liquid to oxygen treatment to obtain a third mixed liquid; a third device capable of performing anoxic treatment on the third mixed liquid to obtain a fourth mixed liquid; capable of fourth mixing a fourth device for separating the supernatant and the first concentrated mixture; a fifth device capable of discharging the supernatant; capable of introducing at least a portion of the first concentrated mixture as the first mixed liquid into the first device and returning without returning The sixth apparatus in which the amount of sludge of the first concentrated mixture of the first apparatus is smaller than the amount of sludge of the sludge feed. 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 5 . The sludge treatment device according to any one of claims 26 to 27, wherein the third device is set such that the anoxic treatment time is 0. 8~6 small 099140871 Form No. A0101 Page 69 of 79 0993446280-0 28 . In 201221484, it is preferably 1 to 4 hours, more preferably 1 to 3 hours. The sludge treatment device according to any one of claims 26 to 28, wherein the second device and the third device are arranged such that the ratio of the oxygen treatment time to the anoxic treatment time is 1:0. 5~1:6, preferably 1:1~1:3' is more preferably 1:1. 5~1:2, most preferably 1:2. The sludge treatment device according to any one of claims 26 to 29, wherein the second device is an aeration tank. The sludge treatment device according to any one of claims 26 to 30, wherein the third device and the fourth device are sedimentation tanks. The sludge treatment device according to any one of claims 26 to 31, wherein the sludge treatment device further comprises a recovery device capable of collecting and recovering a gaseous filler compound. A sewage biological treatment apparatus for a sewage biological treatment method according to any one of claims 13 to 15, comprising: capable of mixing a sludge feed with a first mixed liquid to obtain a second mixed liquid a first device; a second device capable of performing oxygen supply treatment to obtain a third mixed liquid; a third device capable of performing anoxic treatment on the third mixed liquid to obtain a fourth mixed liquid; capable of applying the fourth mixed liquid a fourth device for separating the supernatant and the first concentrated mixed solution; a fifth device capable of discharging the supernatant; capable of introducing at least a portion of the first concentrated mixed liquid as the first mixed liquid into the first device and returning to the first device The sixth device for the sludge of the first concentrated mixture of the device is smaller than the sludge for the sludge feed; the supernatant discharged from at least a portion of the fifth device can be biologically treated by the sewage to obtain the second concentrated mixture and purified a seventh device for effluent; an eighth device capable of discharging purified water; a ninth device capable of introducing sewage into the first device and/or the seventh device; and optionally capable of The second portion was concentrated mixture was introduced into the tenth device of the first device. 099140871 Form No. A0101 Page 70 of 79 0993446280-0 201221484 34. The sewage biological treatment device of claim 33, wherein the second device is set such that the oxygen treatment time is 〇. 1~4 hours 5〜1. 5小时。 Preferably, 〇. 5~1. 5 hours. The effluent biological treatment device of any one of the above-mentioned claims, wherein the third device is set such that the anoxic treatment time is 0.8 to 6 hours, preferably 1 to 4 hours, more preferably 1 to 3 hours. 36. The sewage biological treatment device of any one of claims 33 to 35 wherein the second device and the third device are arranged such that when oxygen is treated 〇 37 . 40 . 間與缺氧處理時間的比為1:0 5〜1:6,優選1:1〜1:3, 更優選1:1. 5〜1:2 ’最優選1:2。 如申請專利範圍第33至36項中任一項所述之污水生物處 理裝置，其中第二設備是曝氣池。 如申請專利範圍第33至37項中任'二項'所述'之污水生物處 理裝置，其中第三設備和第四設備是沉澱池。 如申请專利範圍第33至38項中任一項所述之污水生物處 理裝置’其中所述污泥處-毅凌還包括能夠收集並回收氣 態含磷化合物的回收設傭。 如申請專利範圍第33至39項中任—項所述之污水生物處 理裝置’其中第七設備是能夠根據Wuhrm麵工藝、A/〇 工藝、Bartienph0工藝、ph〇red〇x工藝、A2/〇工藝倒 置A2/0工藝、UCT工藝、MUCT工藝、工藝㈣^工 藝JHB工藝、TNCU工藝、Dephanox工藝、BCFS工藝、 MSBR工藝、SBR工藝、AB工藝、氧化溝工藝、生物膜工藝 、流動床I藝或其組合的進行污水生物處理的設備。 099140871 41 . -種一種降低來自污水生物處理過程的污泥中碳、氮和填 含量的方法’包括將污泥作為污泥進料通過根據如申請專 表單編號A0101 第71頁/共79頁 0993446280-0 201221484 利範圍第1至12項中任一項的污泥處理方法來降低其中碳 、氮和麟的含量。 42 . 一種降低污水中碳、氮和磷含量的方法，包括將污水作為 污水進料通過根據如申請專利範圍第13至25項中任一項 的污水生物處理方法來降低其中碳、氮和磷的含量。 43 . 一種回收來自污水生物處理過程的污泥中磷的方法，包括 (i )將污泥作為污泥進料通過根據如申請專利範圍第1至 12項中任一項的污泥處理方法將其中的含磷化合物，特別 是以溶液形式存在的含填化合物，轉化為氣態含填化合物 而逸出，和（ii)回收步驟（i)中逸出的氣態含磷化合 物。 44 . 一種回收污水中磷的方法，包括（i )將污水作為污水進 料通過根據如申請專利範圍第13至25項中任一項的污水 生物處理方法將其中的含磷化合物，特別是以溶液形式存 在的含填化合物，轉化為氣態含填化合物而逸出，和（i i )回收步驟（i )中逸出的氣態含磷化合物。 099140871 表單編號A0101 第72頁/共79頁 0993446280-040. The ratio of the time to the anoxic treatment time is 1:0 5~1:6, preferably 1:1~1:3, more preferably 1:1. 5~1:2 ‘most preferably 1:2. The sewage biological treatment device of any one of claims 33 to 36, wherein the second device is an aeration tank. A sewage biological treatment apparatus according to any of the above-mentioned claims, wherein the third apparatus and the fourth apparatus are sedimentation tanks. The sewage biological treatment apparatus of any one of claims 33 to 38, wherein the sludge portion - Yi Ling also includes a recovery commission capable of collecting and recovering a gaseous phosphorus-containing compound. The sewage biological treatment device as described in any one of claims 33 to 39, wherein the seventh device is capable of according to the Wuhrm surface process, the A/〇 process, the Bartienph0 process, the ph〇red〇x process, A2/〇 Process Inversion A2/0 Process, UCT Process, MUCT Process, Process (4)^Process JHB Process, TNCU Process, Dephanox Process, BCFS Process, MSBR Process, SBR Process, AB Process, Oxidation Ditch Process, Biofilm Process, Flow Bed I Art A device for biological treatment of sewage, or a combination thereof. 099140871 41 . - A method for reducing the carbon, nitrogen and filling content of sludge from biological treatment of sewage 'including the use of sludge as sludge feed according to the application form No. A0101, page 71 / page 79, 0993446280 The method of sludge treatment according to any one of items 1 to 12, wherein the content of carbon, nitrogen and lin is reduced. 42. A method for reducing carbon, nitrogen and phosphorus in sewage, comprising reducing sewage, carbon and nitrogen by using sewage as a sewage feed through a biological treatment method for sewage according to any one of claims 13 to 25. The content. 43. A method of recovering phosphorus from a sludge from a biological treatment process of sewage, comprising: (i) passing the sludge as a sludge feed through a sludge treatment method according to any one of claims 1 to 12 The phosphorus-containing compound, particularly the filler-containing compound present in the form of a solution, is converted to a gaseous-containing compound to escape, and (ii) the gaseous phosphorus-containing compound evolved in the step (i) is recovered. A method for recovering phosphorus in a sewage, comprising: (i) passing the sewage as a sewage feed to a phosphorus-containing compound according to the biological treatment method of sewage according to any one of claims 13 to 25, in particular The contained compound in the form of a solution is converted to a gaseous contained compound to escape, and (ii) the gaseous phosphorus-containing compound evolved in the step (i) is recovered. 099140871 Form No. A0101 Page 72 of 79 0993446280-0
TW099140871A 2010-11-25 2010-11-25 Method and apparatus for sludge treatment and use thereof in sewage biotreatment TWI445673B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
TW099140871A TWI445673B (en) 2010-11-25 2010-11-25 Method and apparatus for sludge treatment and use thereof in sewage biotreatment

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
TW099140871A TWI445673B (en) 2010-11-25 2010-11-25 Method and apparatus for sludge treatment and use thereof in sewage biotreatment

Publications (2)

Publication Number Publication Date
TW201221484A true TW201221484A (en) 2012-06-01
TWI445673B TWI445673B (en) 2014-07-21

Family

ID=46724940

Family Applications (1)

Application Number Title Priority Date Filing Date
TW099140871A TWI445673B (en) 2010-11-25 2010-11-25 Method and apparatus for sludge treatment and use thereof in sewage biotreatment

Country Status (1)

Country Link
TW (1) TWI445673B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI571442B (en) * 2015-07-08 2017-02-21 Lin Zhi-Yan Biological sludge lysis reaction system

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106396327B (en) * 2015-08-03 2019-03-22 林知谚 Biological sludge lysis reaction system
EP3681843A4 (en) 2017-09-14 2021-06-09 Evoqua Water Technologies LLC Simultaneous nitrification/denitrification (sndn) in sequencing batch reactor applications

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TWI571442B (en) * 2015-07-08 2017-02-21 Lin Zhi-Yan Biological sludge lysis reaction system
US10207944B2 (en) 2015-07-08 2019-02-19 Chang-Ching Lin Biosludge treatment system

Also Published As

Publication number Publication date
TWI445673B (en) 2014-07-21

Similar Documents

Publication Publication Date Title
JP5685265B2 (en) Sludge treatment method using sludge biological treatment method, and sludge treatment apparatus and apparatus
CN106745743B (en) Sewage nitrogen and phosphorus removal system
CN104961306B (en) A kind of processing method of vaccary breeding wastewater
CN101759323A (en) Treatment combined process for pig farm waste water with high nitrogen content
CN106430845A (en) Kitchen garbage wastewater treatment apparatus
CN110395851B (en) High-altitude town sewage treatment method based on nitrogen and phosphorus capture and completely autotrophic nitrogen removal
CN103803711A (en) Method for treating ammonia-nitrogen wastewater by using immobilized microorganism
CN103241908A (en) Large-scale pig farm wastewater treatment method
Ren et al. Anammox-mediated municipal solid waste leachate treatment: A critical review
CN109867352B (en) Method for realizing autotrophic deep denitrification of nitrogen-containing wastewater by utilizing anaerobic MBR (membrane bioreactor)
CN113716689B (en) Mixed nutrition type denitrification method based on sulfur reduction and sulfur autotrophic denitrification
Pelaz et al. Recirculation of gas emissions to achieve advanced denitrification of the effluent from the anaerobic treatment of domestic wastewater
CN202729946U (en) Two-stage anoxic/oxic (A/O)-membrane biological reactor (MBR) nitrogen and phosphorus removal device
TW201221484A (en) Method and apparatus for sludge treatment and use thereof in sewage biotreatment
CN116693112A (en) Treatment method of landfill leachate with low carbon nitrogen ratio
KR100375413B1 (en) Removal Methods of Nitrogen and phosphorus in wastewater using external carbon source
CN113526668A (en) Device and method for simultaneously realizing urban sewage treatment and excess sludge reduction
Inamori et al. Domestic sewage treatment using an anaerobic biofilter with an aerobic biofilter
CN112010429A (en) Biological autotrophic nitrogen removal integrated artificial wetland system
CN110697991A (en) Garbage leachate biological treatment process and system
Do et al. Wastewater treatment by Sequencing Batch Reactor (SBR) without releasing excess sludge
CN216890529U (en) Integrated sewage treatment equipment
CN216005573U (en) Portable and movable black and odorous water body purification device
Nguyen et al. Constructed wetlands and oxidation pond systems
KR20130003238A (en) The method and treatment process of wastewater containing organic matter and nitrogen compounds-livestock wastewater, digestive wastewater, food wastewater

Legal Events

Date Code Title Description
MM4A Annulment or lapse of patent due to non-payment of fees