WO2021258505A1 - 一种利用城市污水有机碳源的磷去除与回收方法 - Google Patents

一种利用城市污水有机碳源的磷去除与回收方法 Download PDF

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WO2021258505A1
WO2021258505A1 PCT/CN2020/106692 CN2020106692W WO2021258505A1 WO 2021258505 A1 WO2021258505 A1 WO 2021258505A1 CN 2020106692 W CN2020106692 W CN 2020106692W WO 2021258505 A1 WO2021258505 A1 WO 2021258505A1
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phosphorus
sewage
recovery
organic carbon
carbon source
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French (fr)
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毕贞
黄勇
潘杨
李祥
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苏州科技大学
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B25/00—Phosphorus; Compounds thereof
    • C01B25/003—Phosphorus
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1278—Provisions for mixing or aeration of the mixed liquor
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/308—Biological phosphorus removal
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/18—PO4-P
    • 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

Definitions

  • the invention relates to the field of sewage treatment, in particular to a phosphorus removal and recovery method using urban sewage organic carbon sources.
  • phosphorus recovery concepts and technologies As the main substrate for phosphorus recovery, the phosphorus content in urban sewage can meet human phosphorus demand by 15-20%. At this stage, the phosphorus recovery projects of domestic and foreign municipal sewage plants mainly focus on the surplus sludge of the Enhanced Biological Phosphorus Removal (EBPR) process, enriching phosphorus from the sludge concentration fermentation supernatant and press filtrate, and then extracting and recovering through multiple steps. phosphorus.
  • EBPR-based phosphorus recovery process generally has the problems of large organic carbon consumption, low phosphorus recovery rate, complex recovery process, and large sludge output.
  • the biofilm phosphorus recovery technology utilizes the phosphorus absorption and release effects of the polyphosphorus biofilm under the alternate aerobic and anaerobic environment to achieve the removal and enrichment of phosphate, and to obtain a phosphorus concentrated solution.
  • the biofilm method combines phosphorus removal and enrichment, and only needs to meet the carbon source required for the growth of phosphorus-accumulating microorganisms.
  • the biofilm method can simultaneously complete the removal and recovery of phosphorus in the mainstream process.
  • the removed phosphorus goes directly into the concentrated solution to be recovered, which avoids the loss of phosphorus in the recovery process and simplifies the recovery. step. Because of its low carbon source demand and high phosphorus recovery rate, it has the advantages and development potential for achieving high phosphorus enrichment in low-phosphorus and low-carbon wastewater.
  • the current biofilm phosphorus recovery process adopts the mode of "aerobic treatment first, then anaerobic treatment", that is, after the sewage enters the main reactor, the phosphorus is transferred from the water phase to the biofilm by aerobic treatment, and the water is treated. Discharge the system; then introduce the recovered liquid and add a concentrated carbon source, accept the phosphorus released by the biofilm in an anaerobic environment, and the recovered liquid is discharged into the collection tank. After many cycles of operation, a phosphorus-rich recovery liquid is obtained. With the continuous increase of the phosphorus concentration in the recovery solution, the phosphorus release ability of the polyphosphate biofilm under high-concentration phosphorus stress environment has become a key issue that limits the concentration of the phosphorus recovery solution.
  • the concentration of organic carbon source (COD) in urban sewage in my country is generally in the range of about 150-400 mg/L, so this part of organic carbon can be directly used for phosphorus recovery in biofilms, which can greatly reduce the carbon source input in the phosphorus recovery process. The amount is increased, and the organic carbon source is used in situ at the same time.
  • the object of the present invention is to provide a phosphorus removal and recovery method using the organic carbon source of urban sewage.
  • a method for removing and recovering phosphorus from an organic carbon source of urban sewage which includes a biofilm reactor containing a polyphosphorus biofilm, an aeration device and a recovery tank arranged in the biofilm reactor, and includes the following steps:
  • step (c) Discharging part of the sewage treated in step (b) into a recovery tank for storage as a recovery liquid;
  • step (d) Turn on the aeration device, and perform aerobic aeration treatment on the remaining part of the sewage after step (b) in the biofilm reactor, so that the phosphorus in it is absorbed by the polyphosphorus biofilm until the phosphorus concentration Meet the emission requirements;
  • step (e) Turn off the aeration device, and discharge all the sewage processed in step (d);
  • step (f) Return the recovered liquid to the biofilm reactor, and start a new cycle from step (a); when the phosphorus concentration in the recovered liquid reaches the phosphorus recovery process requirements, a phosphorus recovery liquid is obtained;
  • Steps (a)-(f) are an operation cycle, during which the sewage treated by the biofilm reactor in step (d) of each operation cycle is continuously discharged; after a plurality of the operation cycles, the recovered liquid
  • the concentration of intermediate phosphorus meets the requirements of the phosphorus recovery process, and a batch of phosphorus recovery liquid is obtained. So far, it is a phosphorus concentration cycle.
  • the recovered liquid returned to the biofilm reactor in step (f) in the previous operation cycle, and the sewage that entered the biofilm reactor in step (a) in the next operation cycle The volume ratio is 1:1-2.5.
  • the phosphorus recovery liquid meets the requirements of the phosphorus recovery process, and a batch of phosphorus recovery liquid is obtained.
  • the phosphorus recovery liquid can be recovered by various existing chemical crystalline phosphorus recovery methods. , Prepare and produce phosphorus products; then inject new sewage into the biofilm reactor, and start a new operation cycle from step (a).
  • the phosphorus concentration reaches the requirements of the phosphorus recovery process, and a batch of phosphorus recovery liquid is obtained. This is a phosphorus concentration cycle. Repeating the phosphorus concentration cycle affects the sewage Perform continuous processing.
  • step (a) when step (a) is repeated, new sewage will be injected, and there is no need to add a new organic carbon source.
  • the concentration of the organic carbon source in the urban sewage is 150-400 mg/L.
  • step (b) the anaerobic stirring treatment time is 2-12 hours.
  • step (d) during the aerobic aeration treatment, the treatment time is 2-12 hours, and the concentration of dissolved oxygen is less than 8 mg/L.
  • the present invention uses the organic carbon source of municipal sewage to remove and recover phosphorus.
  • the organic carbon source contained in the municipal sewage is used in the biofilm reactor to effectively remove the phosphorus in the sewage without any need.
  • all the phosphorus removed from the urban sewage enters the phosphorus recovery solution to achieve simultaneous removal and recovery of phosphorus; at the same time, the obtained phosphorus recovery solution can be prepared and produced by various existing chemical crystalline phosphorus recovery methods. product.
  • in-situ utilization of the organic carbon source in the sewage is also carried out, which greatly reduces the carbon source input cost in the phosphorus recovery process.
  • Figure 1 is a schematic diagram of the process of the present invention.
  • the concentration of organic carbon source (COD) in urban sewage in my country is generally in the range of about 150-400 mg/L, and the concentration of phosphorus is 3-8 mg/L.
  • the invention relates to a method for synchronously removing and recovering phosphorus, which can directly use this part of the organic carbon source of urban sewage in the recovery of biological membrane phosphorus, greatly reducing the amount of carbon source added in the phosphorus recovery process, and at the same time contribute to the organic carbon
  • the source is used in situ, which is convenient for energy saving and environmental protection.
  • the sewage referred to in the present invention is urban sewage.
  • a phosphorus removal and recovery method using the organic carbon source of urban sewage As shown in Figure 1, it is a continuous operation process.
  • the equipment involved is: a biofilm reactor containing polyphosphorus biofilm 1. It is installed in the biofilm reactor The stirring device in 1 2, the polyphosphorus biofilm suspended filler carrier 3, the aeration device 4 and the recovery tank 5 arranged in the biofilm reactor 1.
  • the biofilm reactor for treating urban sewage is not particularly limited, and a biofilm reactor well known to those skilled in the art that can be used for sewage treatment by the sequencing batch biofilm method may be used.
  • the preparation method of the polyphosphorus biofilm is not limited, and any common method in the prior art can be used, as long as the cultivation of the polyphosphorus biofilm can be realized.
  • the following is an example of a culture method: mixed culture of activated sludge and suspended filler carrier, and alternately treated by anaerobic stirring and aerobic aeration, polyphosphate microorganisms adhere to the surface of the suspended filler carrier to form a polyphosphate biofilm suspended filler carrier 3.
  • the biofilm reactor 1 is also equipped with a stirring device 2 to enhance the mass transfer effect between the urban sewage and the polyphosphorus biofilm on the surface of the polyphosphorus biofilm suspended filler carrier 3 , So that the polyphosphate biofilm can maximize its effect.
  • the present invention is a phosphorus removal and recovery method using urban sewage organic carbon source, including the following steps:
  • step (c) Discharging part of the sewage treated in step (b) into a recovery tank for storage as a recovery liquid;
  • step (d) Turn on the aeration device, and perform aerobic aeration treatment on the remaining part of the sewage after step (b) in the biofilm reactor for 2-12 hours, and the dissolved oxygen concentration is less than 8mg/L, so that the phosphorus in it will be polymerized. Phosphorus biofilm absorbs until the phosphorus concentration reaches the emission requirement (phosphorus concentration ⁇ 0.5mg/L).
  • step (e) Turn off the aeration device, and discharge all the sewage processed in step (d);
  • step (f) Return the recovered liquid to the biofilm reactor, and start a new cycle from step (a); when the phosphorus concentration in the recovered liquid reaches the phosphorus recovery process requirement, the phosphorus recovery liquid is obtained.
  • the concentration of the organic carbon source in the urban sewage of the present invention is 150-400 mg/L.
  • Steps (a)-(f) are an operation cycle during which the sewage treated by the biofilm reactor in step (d) of each operation cycle is continuously discharged; after multiple operation cycles, the phosphorus concentration in the recovered liquid reaches the phosphorus recovery Process requirements, obtain a batch of phosphorus recovery liquid, so far is a phosphorus concentration cycle. At this time, the phosphorus concentration in the phosphorus recovery solution is relatively high.
  • the phosphorus recovery solution can use various existing chemical crystallization phosphorus recovery methods for phosphorus recovery to prepare and produce phosphorus products; then new sewage is injected into the biofilm reactor, from Step (a) starts a new operation cycle. At this time, when step (a) is repeated, new sewage will be injected, and there is no need to add a new organic carbon source; the phosphorus in urban sewage can be removed and recovered, which will greatly improve the efficiency of treatment and save time .
  • Steps (a)-(f) after multiple cycles of operation the phosphorus concentration reaches the phosphorus recovery process requirements, and a batch of phosphorus recovery liquid is obtained. So far, it is a phosphorus concentration cycle, and the wastewater is continuously treated by repeating the phosphorus concentration cycle.
  • the volume ratio of the recovered liquid returned to the biofilm reactor in step (f) in the previous operation cycle and the sewage entering the biofilm reactor in step (a) in the next operation cycle is 1:1 to 2.5.
  • the aim is to enable the organic carbon source in the sewage to be fully used for the removal and recovery of phosphorus, and to increase the concentration of phosphorus in the recovered liquid.
  • the temperature and pH value in the biofilm reactor 1 of the present invention do not need to be adjusted manually, which greatly reduces manpower and has high application value.
  • Example 1 The COD concentration of urban sewage in Example 1 is 150 mg/L.
  • the urban sewage in this example is to be removed and recovered using the phosphorus removal and recovery method of the present invention using the organic carbon source of urban sewage as described above, so that the concentration of recovered liquid phosphorus is More than 150mg/L.
  • the volume ratio of the recovered liquid returned to the biofilm reactor in the previous operation cycle step (f) and the sewage entering the biofilm reactor in the next operation cycle step (a) is 1:2.0-2.5.
  • the oxygen stirring time is 8-12h, and the aerobic aeration treatment time of step (d) is 8-12h.
  • Example 2 The COD concentration of urban sewage is 300 mg/L.
  • the urban sewage in this example is to be removed and recovered using the phosphorus removal and recovery method of the present invention using the organic carbon source of urban sewage as described above, so that the concentration of liquid phosphorus is recovered Over 150mg/L, the volume ratio of the recovered liquid returned to the biofilm reactor in step (f) of the previous operation cycle and the sewage entering the biofilm reactor in step (a) of the next operation cycle is 1:1.5-2.0, step
  • the anaerobic stirring time of (b) is 6-10h, and the aerobic aeration treatment time of step (d) is 6-10h.
  • Example 3 The COD concentration of urban sewage is 400 mg/L.
  • the urban sewage in this example is to be removed and recovered using the phosphorus removal and recovery method of the present invention using the organic carbon source of urban sewage as described above, so as to recover the concentration of liquid phosphorus Over 150mg/L, the volume ratio of the recovered liquid returned to the biofilm reactor in step (f) of the previous operation cycle and the sewage entering the biofilm reactor in step (a) of the next operation cycle is 1:1.0-1.5, step The anaerobic stirring time of (b) is 2-6h, and the aerobic aeration treatment time of step (d) is 2-6h.
  • the anaerobic stirring time in step (b) and the aerobic aeration treatment time in step (d) are both the time used in a single operation cycle. It can be seen from Examples 1-3 that for municipal sewage with a higher COD concentration, the volume ratio of sewage entering the biofilm reactor in step (a) can be correspondingly smaller, and the time for anaerobic stirring treatment and aerobic aeration treatment It can also be shortened appropriately. For municipal wastewater with a low COD concentration, in order to achieve better phosphorus removal and recovery effects, the volume ratio of wastewater entering the biofilm reactor in step (a) should be a larger value, and the anaerobic stirring treatment and treatment should be appropriately extended. The time of aerobic aeration treatment.
  • the invention utilizes the organic carbon source contained in the urban sewage to effectively remove the phosphorus in the sewage without adding an organic carbon source at all, and all the phosphorus removed in the urban sewage enters the phosphorus recovery liquid, thereby achieving simultaneous removal and recovery of phosphorus; at the same time; ,
  • the obtained phosphorus recovery liquid can be prepared and produced by various existing chemical crystalline phosphorus recovery methods.
  • in-situ utilization of the organic carbon source in the sewage is also carried out, which greatly reduces the carbon source input cost in the phosphorus recovery process.

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Abstract

一种利用城市污水有机碳源的磷去除与回收方法，步骤如下：首先向生物膜反应器中注满污水；在厌氧条件下搅拌，使聚磷生物膜利用污水中的有机碳源进行释磷；经上述处理后的污水一部分排入回收罐储存，作为回收液；打开曝气装置，对厌氧处理后的污水剩余部分进行好氧曝气处理，使磷被聚磷生物膜吸收，至磷浓度达到排放要求，关闭曝气装置，排出污水；将回收液返回生物膜反应器，同时加入污水注满反应器，多次循环以上步骤；待回收液磷浓度达到磷回收工艺要求时，得到磷回收液。本发明在生物膜反应器中利用污水中的有机碳源将磷去除并浓缩形成磷回收液，可供现有工艺制备磷产品；既同步实现磷的去除和回收，又避免在磷回收工艺中额外投加有机碳源。

Description

一种利用城市污水有机碳源的磷去除与回收方法
本申请要求于2020年6月23日提交中国专利局、申请号为202010579041.6、发明名称为“一种利用城市污水有机碳源的磷去除与回收方法”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本发明涉及污水处理领域，具体涉及一种利用城市污水有机碳源的磷去除与回收方法。
背景技术
资源稀缺与环境污染的矛盾正推动着磷回收理念和技术的快速发展。作为磷回收的主要基质，城市污水中磷含量能满足人类15-20％的磷需求。现阶段，国内外城市污水厂磷回收项目主要以强化生物除磷(EBPR)工艺的剩余污泥为对象，从污泥浓缩发酵上清液及压滤液中富集磷，再经多步提取回收磷。基于EBPR的磷回收工艺普遍存在有机碳消耗大、磷回收率低、回收工艺复杂、污泥产量大的问题。
现有技术中生物膜磷回收技术是在好氧、厌氧交替环境下，利用聚磷生物膜的吸磷、释磷作用，实现磷酸盐的去除与富集、并得到磷浓缩液。生物膜法将磷去除与富集相结合，只需满足聚磷微生物生长所需碳源。与传统EBPR磷回收工艺相比，生物膜法可在主流工艺中将磷的去除与回收同步完成，被去除的磷直接进入浓缩液被回收，避免了磷在回收过程中的损失、简化了回收步骤。因其碳源需求低、磷回收率高的特点，使之具有针对低磷低碳污水实现磷高倍富集的优势和发展潜力。
现阶段的生物膜磷回收工艺均采用“先好氧处理、再厌氧处理”的模式，即污水进入主反应器后，先经好氧处理将磷从水相转移至生物膜、处理水被排出***；再引入回收液并投加浓缩碳源，在厌氧环境下接纳生物膜释放的磷、回收液再被排入收集罐。经过多次循环操作，得到富磷回收液。随着回收液中磷浓度不断增加，聚磷生物膜在高浓度磷胁迫环境下的释磷能力成为了限制磷回收液浓度的关键问题。又因在这种工艺模式下，污水中的有机碳在好氧阶段被消耗，因此须在厌氧阶段外加浓缩碳源(COD浓 度由几百～上千毫克每升不等)以获得高浓度磷回收液。
综上所述，开发新的生物膜磷回收工艺模式，尽可能以最少的碳源消耗为代价将城市污水中含量仅为数毫克每升的磷酸盐富集至满足磷回收要求的较高浓度水平是十分必要的。我国城市污水中有机碳源(COD)浓度普遍在150-400mg/L左右的范围内，那么可以将这部分有机碳直接用于生物膜磷回收，既可以大大降低磷回收工艺中的碳源投加量，同时又对有机碳源进行了原位利用。
发明内容
有鉴于此，本发明的目的是提供一种利用城市污水有机碳源的磷去除与回收方法。
为达到上述目的，本发明采用的技术方案是：
一种利用城市污水有机碳源的磷去除与回收方法，其包括含有聚磷生物膜的生物膜反应器、设置在所述生物膜反应器内的曝气装置、回收罐，包括如下步骤：
(a)向所述生物膜反应器中加入污水至所述生物膜反应器注满；
(b)在厌氧条件下搅拌，使得所述聚磷生物膜利用所述污水中的有机碳源进行释磷；
(c)将经过步骤(b)处理后的污水一部分排入回收罐储存，作为回收液；
(d)打开曝气装置，对所述生物膜反应器中经过步骤(b)处理后的污水剩余部分进行好氧曝气处理，使其中的磷被所述聚磷生物膜吸收，直至磷浓度达到排放要求；
(e)关闭曝气装置，将经过步骤(d)处理后的污水全部排出；
(f)将所述回收液返回至所述生物膜反应器，从步骤(a)开始新的循环；待所述回收液中磷浓度达到磷回收工艺要求时，得到磷回收液；
步骤(a)-(f)为一个操作循环，期间每个操作循环步骤(d)中经所述生物膜反应器处理后的污水不断排放；经过多个所述操作循环后，所述回收液中磷浓度达到磷回收工艺要求，得到一批磷回收液，至此为一个 磷浓缩周期。
具体的，上一个所述操作循环中步骤(f)中返回所述生物膜反应器的所述回收液、下一个操作循环中步骤(a)中进入所述生物膜反应器的所述污水的体积比为1:1-2.5。
具体的，经过多个所述操作循环后，所述磷回收液达到磷回收工艺要求，得到一批磷回收液，所述磷回收液可采用现有的各种化学结晶磷回收方法进行磷回收，制备和生产磷产品；再向所述生物膜反应器中注入新的污水，从步骤(a)开始进行新的操作循环。
具体的，所述步骤(a)-(f)经多次操作循环后，磷浓度达到磷回收工艺要求，得到一批磷回收液，至此为一个磷浓缩周期，重复所述磷浓缩周期对污水进行连续处理。
具体的，重复进行步骤(a)时，会注入新的污水，且无需额外加入新的有机碳源。
具体的，所述城市污水中有机碳源的浓度为150-400mg/L。
具体的，步骤(b)中，所述厌氧搅拌处理时间为2-12h。
具体的，步骤(d)中，所述好氧曝气处理时，处理时间为2-12h，溶解氧的浓度<8mg/L。
与现有技术相比，本发明一种利用城市污水有机碳源的磷去除与回收方法，在生物膜反应器中利用城市污水中含有的有机碳源将污水中的磷进行有效去除，完全无需外加有机碳源，城市污水中被去除的磷全部进入磷回收液，实现磷的去除和回收同步进行；同时，得到的磷回收液可采用现有的各种化学结晶磷回收方法制备和生产磷产品。此外，还对污水中有机碳源进行原位利用，大大降低了磷回收过程中碳源投加成本。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附 图。
附图1为本发明的流程示意图。
附图中涉及的附图标记和组成部分说明：1、生物膜反应器；2、搅拌装置；3、聚磷生物膜悬浮填料载体；4、曝气装置；5、回收罐。
具体实施方式
我国城市污水中有机碳源(COD)浓度普遍在150-400mg/L左右的范围内，磷浓度为3-8mg/L。本发明涉及了一种同步去除和回收磷的方法，可以将城市污水的这部分有机碳源直接用于生物膜磷回收，大大降低磷回收工艺中的碳源投加量，同时又对有机碳源进行了原位利用，节能环保方便。本发明中所指代的污水均为城市污水。
下面将通过具体实施方式对本发明的技术方案进行清楚、详细地描述。显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有作出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
一种利用城市污水有机碳源的磷去除与回收方法，如附图1所示为连续运行工序，涉及使用的装置有：含有聚磷生物膜的生物膜反应器1、设置在生物膜反应器1内的搅拌装置2、聚磷生物膜悬浮填料载体3、设置在生物膜反应器1内的曝气装置4、回收罐5。
在本发明中，对处理城市污水的生物膜反应器没有特别限定，采用本领域技术人员熟知的可以用于序批式生物膜法污水处理的生物膜反应器即可。
聚磷生物膜的制备方法不做限定，现有技术中常见的方法均可，只要能够实现聚磷生物膜的培养即可。下面举例一种培养方法：将活性污泥与悬浮填料载体混合培养，经厌氧搅拌和好氧曝气交替处理，聚磷微生物附着在悬浮填料载体表面，形成聚磷生物膜悬浮填料载体3。
为了能够让去除及回收磷更加充分彻底，生物膜反应器1中还设置了搅拌装置2，从而能够强化城市污水与聚磷生物膜悬浮填料载体3表面的聚磷生物膜之间的传质效果，使得聚磷生物膜最大化发挥其作用。
本发明一种利用城市污水有机碳源的磷去除与回收方法，包括如下步骤：
(a)向生物膜反应器1中加入污水至生物膜反应器1注满；
(b)在厌氧条件下搅拌2-12h，使得聚磷生物膜利用污水中的有机碳源进行释磷；
(c)将经过步骤(b)处理后的污水一部分排入回收罐储存，作为回收液；
(d)打开曝气装置，对生物膜反应器中经过步骤(b)处理后的污水剩余部分进行好氧曝气处理2-12h，溶解氧的浓度<8mg/L，使其中的磷被聚磷生物膜吸收，直至磷浓度达到排放要求(磷浓度<0.5mg/L)。
(e)关闭曝气装置，将经过步骤(d)处理后的污水全部排出；
(f)将回收液返回至生物膜反应器，从步骤(a)开始新的循环；待回收液中磷浓度达到磷回收工艺要求时，得到磷回收液。
本发明城市污水中有机碳源的浓度为150-400mg/L。
步骤(a)-(f)为一个操作循环，期间每个操作循环步骤(d)中经生物膜反应器处理后的污水不断排放；经过多个操作循环后，回收液中磷浓度达到磷回收工艺要求，得到一批磷回收液，至此为一个磷浓缩周期。此时磷回收液中的磷浓度较高，磷回收液可采用现有的各种化学结晶磷回收方法进行磷回收，制备和生产磷产品；再向生物膜反应器中注入新的污水，从步骤(a)开始进行新的操作循环。此时，重复进行步骤(a)时，会注入新的污水，且无需额外加入新的有机碳源；即可对城市污水中的磷进行去除及回收，这样将大大提高处理的效率，节省时间。
步骤(a)-(f)经多次操作循环后，磷浓度达到磷回收工艺要求，得到一批磷回收液，至此为一个磷浓缩周期，重复磷浓缩周期对污水进行连续处理。
上一个操作循环中步骤(f)中返回生物膜反应器的回收液、下一个操作循环中步骤(a)中进入生物膜反应器的污水的体积比为1:1-2.5。通过合理设置回收液与添加污水的体积比，旨在能够使污水中的有机碳源能够充 分被用于磷的去除与回收，提高回收液中磷的浓度。
本发明的生物膜反应器1中的温度及pH值无需进行人为调控，大大减少了人力，具有较高的应用价值。
以下将举出实施例，以更充分地说明本申请的技术方案。
实施例1城市污水COD浓度为150mg/L，要将该实施例中的城市污水采用本发明如上所述利用城市污水有机碳源的磷去除与回收方法进行磷去除及回收，使得回收液磷浓度超过150mg/L。上一操作循环步骤(f)中返回生物膜反应器的回收液、下一操作循环步骤(a)中进入生物膜反应器的污水的体积比为1:2.0-2.5，步骤(b)的厌氧搅拌时间为8-12h，步骤(d)的好氧曝气处理时间为8-12h。
实施例2城市污水COD浓度为300mg/L，要将该实施例中的城市污水采用本发明如上所述利用城市污水有机碳源的磷去除与回收方法进行磷去除及回收，使得回收液磷浓度超过150mg/L，上一操作循环步骤(f)中返回生物膜反应器的回收液、下一操作循环步骤(a)中进入生物膜反应器的污水的体积比为1:1.5-2.0，步骤(b)的厌氧搅拌时间为6-10h，步骤(d)的好氧曝气处理时间为6-10h。
实施例3城市污水COD浓度为400mg/L，要将该实施例中的城市污水采用本发明如上所述利用城市污水有机碳源的磷去除与回收方法进行磷去除及回收，使得回收液磷浓度超过150mg/L，上一操作循环步骤(f)中返回生物膜反应器的回收液、下一操作循环步骤(a)中进入生物膜反应器的污水的体积比为1:1.0-1.5，步骤(b)的厌氧搅拌时间为2-6h，步骤(d)的好氧曝气处理时间为2-6h。
以上实施例中，步骤(b)的厌氧搅拌时间和步骤(d)的好氧曝气处理时间均为在单个操作循环周期内的所用时间。从实施例1-3可以看出，对于COD浓度较高的城市污水，步骤(a)中进入生物膜反应器的污水体 积比例可以相应较小，厌氧搅拌处理和好氧曝气处理的时间也可适当缩短。而对于COD浓度较低的城市污水，为了达到较好的磷去除与回收效果，则步骤(a)中进入生物膜反应器的污水体积比例应采用较大值，并适当延长厌氧搅拌处理和好氧曝气处理的时间。
本发明利用城市污水中含有的有机碳源将污水中的磷进行有效去除，完全无需外加有机碳源，城市污水中被去除的磷全部进入磷回收液，实现磷的去除和回收同步进行；同时，得到的磷回收液可采用现有的各种化学结晶磷回收方法制备和生产磷产品。此外，还对污水中有机碳源进行原位利用，大大降低了磷回收过程中碳源投加成本。
对所公开的实施例的上述说明，使本领域专业技术人员能够实现或使用本发明。对这些实施例的多种修改对本领域的专业技术人员来说将是显而易见的，本文中所定义的一般原理可以在不脱离本发明的精神或范围的情况下，在其它实施例中实现。因此，本发明将不会被限制于本文所示的这些实施例，而是要符合与本文所公开的原理和新颖特点相一致的最宽的范围。

Claims (8)

  1. 一种利用城市污水有机碳源的磷去除与回收方法，其特征在于，其包括含有聚磷生物膜的生物膜反应器、设置在所述生物膜反应器内的曝气装置、回收罐，包括如下步骤：
    (a)向所述生物膜反应器中加入污水至所述生物膜反应器注满；
    (b)在厌氧条件下搅拌，使得所述聚磷生物膜利用所述污水中的有机碳源进行释磷；
    (c)将经过步骤(b)处理后的污水一部分排入回收罐储存，作为回收液；
    (d)打开曝气装置，对所述生物膜反应器中经过步骤(b)处理后的污水剩余部分进行好氧曝气处理，使其中的磷被所述聚磷生物膜吸收，直至磷浓度达到排放要求；
    (e)关闭曝气装置，将经过步骤(d)处理后的污水全部排出；
    (f)将所述回收液返回至所述生物膜反应器，从步骤(a)开始新的循环；待所述回收液中磷浓度达到磷回收工艺要求时，得到磷回收液；
    步骤(a)-(f)为一个操作循环，期间每个操作循环步骤(d)中经所述生物膜反应器处理后的污水不断排放；经过多个所述操作循环后，所述回收液中磷浓度达到磷回收工艺要求，得到一批磷回收液，至此为一个磷浓缩周期。
  2. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法，其特征在于：上一个所述操作循环中步骤(f)中返回所述生物膜反应器的所述回收液、下一个操作循环中步骤(a)中进入所述生物膜反应器的所述污水的体积比为1:1-2.5。
  3. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法，其特征在于：经过多个所述操作循环后，所述磷回收液达到磷回收工艺要求，得到一批磷回收液，所述磷回收液可采用现有的各种化学结晶磷回收方法进行磷回收，制备和生产磷产品；再向所述生物膜反应器中注入新的污水，从步骤(a)开始进行新的操作循环。
  4. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法， 其特征在于：所述步骤(a)-(f)经多次操作循环后，磷浓度达到磷回收工艺要求，得到一批磷回收液，至此为一个磷浓缩周期，重复所述磷浓缩周期对污水进行连续处理。
  5. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法，其特征在于：重复进行步骤(a)时，会注入新的污水，且无需额外加入新的有机碳源。
  6. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法，其特征在于：所述城市污水中有机碳源的浓度为150-400mg/L。
  7. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法，其特征在于：步骤(b)中，所述厌氧搅拌处理时间为2-12h。
  8. 根据权利要求1所述利用城市污水有机碳源的磷去除与回收方法，其特征在于：步骤(d)中，所述好氧曝气处理时，处理时间为2-12h，溶解氧的浓度<8mg/L。
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6875357B1 (en) * 2000-03-15 2005-04-05 Aqua-Aerobic Systems, Inc. Process and apparatus for treatment of waste water
CN101891345A (zh) * 2010-07-13 2010-11-24 重庆大学 强化低碳源城市污水低氧同步脱氮除磷污水处理装置及方法
CN106565016A (zh) * 2016-10-19 2017-04-19 青岛大学 旁流除磷实现无剩余污泥排放的城市污水脱氮除磷的装置和方法
CN107311308A (zh) * 2016-04-26 2017-11-03 苏州科技学院 一种生物膜法同步去除与富集磷的工艺
CN110668560A (zh) * 2019-10-28 2020-01-10 苏州科技大学 连续型生物脱氮磷回收***及工艺

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10256884A1 (de) * 2002-12-05 2004-06-17 Henkel Kgaa Verfahren zur Phosphatierung von Metalloberflächen mit verbesserter Phosphat-Rückgewinnung
CN100586879C (zh) * 2007-12-14 2010-02-03 郑俊 采用交替式曝气的生物滤池生物除磷工艺
CN101654312B (zh) * 2009-07-17 2012-02-01 东华大学 连续运行强化生物膜除磷的装置和方法
CN104944704B (zh) * 2015-06-23 2017-05-31 北京工业大学 一种无外加碳源实现低碳氮比城市污水同步脱氮除磷的装置和方法
CN106565056A (zh) * 2016-10-25 2017-04-19 西安建筑科技大学 一种强化污水生物除磷且回收污水中磷酸盐资源的方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6875357B1 (en) * 2000-03-15 2005-04-05 Aqua-Aerobic Systems, Inc. Process and apparatus for treatment of waste water
CN101891345A (zh) * 2010-07-13 2010-11-24 重庆大学 强化低碳源城市污水低氧同步脱氮除磷污水处理装置及方法
CN107311308A (zh) * 2016-04-26 2017-11-03 苏州科技学院 一种生物膜法同步去除与富集磷的工艺
CN106565016A (zh) * 2016-10-19 2017-04-19 青岛大学 旁流除磷实现无剩余污泥排放的城市污水脱氮除磷的装置和方法
CN110668560A (zh) * 2019-10-28 2020-01-10 苏州科技大学 连续型生物脱氮磷回收***及工艺

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