WO2021012440A1 - 一种同步回收水和电能的污水处理装置及方法 - Google Patents

一种同步回收水和电能的污水处理装置及方法 Download PDF

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Publication number
WO2021012440A1
WO2021012440A1 PCT/CN2019/113192 CN2019113192W WO2021012440A1 WO 2021012440 A1 WO2021012440 A1 WO 2021012440A1 CN 2019113192 W CN2019113192 W CN 2019113192W WO 2021012440 A1 WO2021012440 A1 WO 2021012440A1
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Prior art keywords
water
membrane
draw
electric energy
sewage treatment
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PCT/CN2019/113192
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English (en)
French (fr)
Inventor
王新华
孟曼丽
刘舒悦
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江南大学
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Application filed by 江南大学 filed Critical 江南大学
Priority to US16/944,255 priority Critical patent/US11208341B2/en
Publication of WO2021012440A1 publication Critical patent/WO2021012440A1/zh

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
    • 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
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems

Definitions

  • the invention relates to a sewage treatment device and method for synchronous recovery of water and electric energy, and belongs to the field of sewage treatment.
  • MBRs Membrane bioreactors
  • OMBR Forward Osmosis Membrane Bioreactor
  • FO forward osmosis
  • FO forward osmosis
  • OMBR can be divided into submerged OMBR (FO membrane module inside the bioreactor) and external OMBR (FO membrane module outside the bioreactor).
  • the submerged OMBR has a small footprint and reduces the circulation pump of the mud-water mixture, but the FO membrane module is not easy to disassemble and the membrane pollution control effect is slightly poor.
  • the external OMBR is easy to disassemble and has good hydraulic conditions, making it easier to control membrane fouling, but it increases the floor space.
  • the driving force of the FO membrane is the osmotic pressure difference.
  • the FO process does not need to apply external pressure as the driving force.
  • Water molecules can spontaneously penetrate from the raw material liquid part with high water chemical potential to the draw liquid part with low water chemical potential.
  • FO membranes have a smaller tendency to membrane fouling. Because the FO membrane has better retention of pollutants, the effluent quality of OMBR is better than that of traditional MBR and can be directly reused. It is precisely due to the characteristics of better effluent water quality and smaller membrane pollution that OMBR has received more and more attention.
  • the current commercial FO film includes two layers, one is the active layer that plays a trapping role, and the other is the support layer that plays a supporting role.
  • the active layer is relatively thin and dense, with strong anti-fouling ability, while the support layer is thick and porous, which is prone to membrane fouling. Therefore, there are two membrane orientations during the operation of the FO membrane, one is the active layer facing the raw material liquid (AL-FS), and the other is the support layer facing the raw material liquid (AL-DS).
  • AL-FS membrane Compared with AL-DS, AL-FS membrane has a smaller fouling tendency, but the membrane flux is smaller.
  • the salt difference energy is the energy generated when different solutions are mixed. Compared with solar energy and wind energy, it is less affected by gas phase and geographical conditions, and it is stored in the ocean. huge.
  • salt difference energy in the FO process because the amount of permeated water produced in the FO sewage treatment process is too small, the corresponding power density (equal to the pressure on the draw side multiplied by the water production) is small, and it is difficult to recover the salt difference energy.
  • Pressure retarded permeation (PRO) is a new type of membrane process that uses salt difference energy to produce productivity.
  • PRO Compared with the FO membrane, PRO applies an external pressure less than the osmotic pressure difference on the side of the draw liquid, which increases the power density generated during the osmosis process, so that the salt difference energy can be recovered.
  • water flows from the feed liquid (low salinity) side to the draw liquid (high salinity) side through the semi-permeable membrane. Since the volume of the draw liquid side of the PRO component is constant, the mixed draw liquid and The feed liquid has a higher pressure than the original draw liquid, which can drive the turbine to generate electricity during the flow out.
  • the main processing objects of PRO are river water, lake water, sea water and other surface water, which lacks application in sewage treatment.
  • the concentration of pollutants in the feed liquid during the PRO operation and its post-treatment are not involved.
  • the extraction liquid of the existing OMBR needs to be recovered by reverse osmosis, membrane distillation and other technologies during operation, and the energy consumption is high, which affects the economic feasibility of the technology.
  • salt difference energy in the FO process, because the amount of permeated water produced in the FO sewage treatment process is too small, the corresponding power density (equal to the pressure on the draw side multiplied by the water production) is small, and it is difficult to recover the salt difference energy.
  • the existing PRO When the existing PRO is running, it is actually a concentration process for the feed liquid, that is, water penetrates the FO membrane into the draw liquid and pollutants are trapped on the side of the feed liquid, which results in the presence of carbon and nitrogen in the feed liquid. Enrichment of pollutants such as phosphate, phosphorus, and complex follow-up treatment.
  • the present invention provides a process that combines the production capacity of OMBR and PRO, and establishes a new sewage treatment technology based on the simultaneous recovery of water and electric energy. On the basis of retaining the advantages of OMBR, additional electric energy is obtained and the post-treatment of the draw liquid is reduced. Energy consumption.
  • the first object of the present invention is to provide a sewage treatment device that synchronously recovers water and electric energy.
  • the device includes a water inlet tank, a bioreactor, an FO membrane module, a turbine, a drawn liquid tank, and a drawn liquid recovery system;
  • the pool is connected to the bioreactor.
  • the FO membrane module includes a draw fluid channel, a feed fluid channel, and an FO membrane.
  • the FO membrane separates the draw fluid channel and the feed fluid channel.
  • the inlet of the feed fluid channel and The outlets of the feed liquid channels are all connected to the bioreactor, the draw liquid pool is connected to the inlet of the draw liquid channel, the outlet of the draw liquid channel is connected to the draw liquid pool through a turbine, and the draw liquid pool is recovered with the draw liquid The system is connected.
  • a pump is installed on the pipeline connecting the intake pool and the bioreactor.
  • a pump is installed on the pipeline connecting the bioreactor and the inlet of the feed liquid channel.
  • a high-pressure pump is installed on the pipeline connecting the drawing liquid pool and the inlet of the drawing liquid channel.
  • an aeration pipe is installed at the lower part of the bioreactor, and one end of the air pump is connected with the aeration pipe.
  • the drawn liquid recovery system includes a conductivity meter, a high-pressure pump, and a reverse osmosis component, wherein the drawn liquid pool, the high-pressure pump, the reverse osmosis component, and the drawn liquid pool are connected in sequence to form a cycle, so
  • the conductivity meter is connected with the high-pressure pump and controls the opening and closing of the high-pressure pump.
  • the detection end of the conductivity meter is located inside the dipping liquid pool.
  • the membrane assembly is made of stainless steel or organic plastic material, and the FO membrane assembly further includes a gasket located on one side of the FO membrane.
  • the FO membrane is any one of a cellulose acetate (CTA) membrane, a polyamide (TFC) membrane, an aquaporin membrane or a polyethersulfone resin (PES) membrane.
  • CTA cellulose acetate
  • TFC polyamide
  • PES polyethersulfone resin
  • the FO film includes a support layer and an active layer, and the active layer faces the draw liquid.
  • the second object of the present invention is to provide a sewage treatment method that simultaneously recovers water and electric energy, and the method uses the above sewage treatment device to treat sewage.
  • the sewage is urban sewage
  • the water quality indicators are: COD: 200-500 mg/L, NH 4 + -N: 20-50 mg/L, TN: 30-50 mg/L L, TP: 2-7 mg/L.
  • the method specifically includes the following steps:
  • the circulation rate of the mud-water mixture is 0.1-0.5 L/min.
  • the inoculated sludge has an SS of 3-9 g/L of activated sludge.
  • the draw solution is a 0.5-4M NaCl, MgCl 2 , KCl, CaCl 2 solution.
  • the pressure applied on the side of the draw fluid channel is less than the osmotic pressure on both sides of the FO membrane.
  • the pressure applied on the side of the drawing fluid channel is 4-8 bar.
  • the concentration of the draw solution when the concentration of the draw solution is too low, it means that the osmotic pressure difference of the FO membrane is smaller than the pressure applied on the side of the draw solution channel.
  • the present invention combines the productivity advantages of OMBR and PRO, uses biological treatment and FO membrane to intercept and recycle sewage, and the mixed draw solution with higher pressure drives the turbine to rotate during the outflow process to generate electricity.
  • a new type of sewage treatment device and method for synchronous recovery of water and electric energy is obtained, which makes energy utilization more fully.
  • the concentrated water obtained by the FO membrane of the present invention does not need to be incinerated or further chemically treated, but only needs to be returned to the bioreactor, and the carbon, nitrogen, phosphorus and other pollutants can be removed through the action of biology, which solves the existing PRO
  • the method of the present invention is more economical and environmentally friendly.
  • Fig. 1 is a schematic structural diagram of an embodiment of a sewage treatment device for synchronous recovery of water and electric energy of the present invention
  • 1 inlet pool
  • 2 peristaltic pump
  • 3 bioreactor
  • 4 air pump
  • 5 peristaltic Pump
  • 6 FO membrane module
  • 7 turbine
  • 8 high pressure pump
  • 9 drawing liquid pool
  • 10 conductivity meter
  • 11 high pressure pump
  • 12 reverse osmosis module.
  • the device of the present invention includes an inlet tank 1, a bioreactor 3, an FO membrane module 6, a turbine 7, a draw liquid tank 9 and a draw Liquid recovery system.
  • the inlet pool 1 is connected to the bioreactor 3 through the peristaltic pump 2.
  • the FO membrane module 6 includes a draw fluid channel, a feed fluid channel, a gasket and an FO membrane.
  • the gasket and the FO membrane are placed in parallel and the two will draw fluid channel and inlet
  • the feed liquid channel is separated, the inlet of the feed liquid channel and the outlet of the feed liquid channel are both connected to the bioreactor 3
  • the draw liquid pool 9 is connected to the inlet of the draw liquid channel through the high-pressure pump 8
  • the outlet of the draw liquid channel passes through the turbine 7 is connected to the draw liquid pool 9
  • the draw liquid recovery system includes a conductivity meter 10, a high-pressure pump 11 and a reverse osmosis component 12, and the draw liquid pool 9, a high pressure pump 11, a reverse osmosis component 12 and a draw liquid pool 9 are connected in sequence
  • the conductivity meter 10 is connected to the high-pressure pump 11 to control the opening and closing of the high-pressure pump.
  • the detection end of the conductivity meter 10 is located inside the dipping liquid pool 9.
  • an aeration pipe is installed at the lower part of the bioreactor 3, and one end of the air pump is connected with the aeration pipe.
  • the membrane module is made of stainless steel or organic plastic material
  • the FO membrane is a cellulose acetate (CTA) membrane, a polyamide (TFC) membrane, a water channel protein membrane or a polyethersulfone resin (PES) membrane.
  • CTA cellulose acetate
  • TFC polyamide
  • PES polyethersulfone resin
  • the operating principle of the above device is as follows: the municipal sewage is used as the feed water. After the municipal sewage enters the bioreactor and is mixed with the activated sludge, the mixed mud-water mixture is pumped into the feed liquid channel of the FO membrane through the pump, and the draw liquid passes through the high pressure
  • the pump enters the draw fluid channel in the membrane module, and uses the osmotic pressure difference on both sides of the FO membrane to make water flow from the feed fluid channel to the draw fluid channel; at the same time, a certain pressure is applied to the draw fluid channel side, and the diluted draw fluid passes through the turbine And push the turbine to rotate, and then generate electricity; when the concentration of the draw solution is too low, the draw solution recovery system is activated, the draw solution is concentrated through the reverse osmosis component and recovered to obtain water.
  • the active layer In view of the structure of FO (one layer is the active layer that plays a role of retention, and the other layer is the support layer that plays a supporting role.
  • the active layer is thin and dense, and has strong anti-pollution ability, while the support layer is thick and porous, easy to produce Membrane fouling), and the FO membrane in the present invention faces activated sludge containing various pollutants.
  • the OMBR of this embodiment adopts the AL-FS orientation (the active layer faces the feed liquid) during operation.
  • the influent water is municipal sewage.
  • the SS (suspended solids) in the bioreactor is 3 g/L activated sludge, the draw fluid is 2 M NaCl, the pressure applied on the draw fluid side is 6 bar, and the membrane orientation is AL-FS (active layer toward the feed fluid), Run for 24 h.
  • Effluent water quality COD: 10 ⁇ 2.45 mg/L, NH 4 + -N: 4.41 ⁇ 0.40 mg/L, TN: 4.49 ⁇ 0.53 mg/L, TP: 0; average water flux is 7.79 LMH, average power density It is 1.4 W/m 2 .
  • the influent water is municipal sewage, water quality: COD: 350 ⁇ 12.2 mg/L, NH 4 + -N: 24.88 ⁇ 1.50 mg/L, TN: 38.24 ⁇ 1.68 mg/L, TP: 2.08 ⁇ 0.13 mg/L.
  • the SS in the bioreactor is 3 g/L activated sludge, the draw solution is 2 M NaCl, the pressure applied on the draw solution side is 6 bar, the membrane orientation is AL-DS (active layer toward the draw solution), and it runs for 4 hours.
  • Effluent water quality COD: 10 ⁇ 1.51 mg/L, NH 4 + -N: 5.12 ⁇ 0.90 mg/L, TN: 5.53 ⁇ 1.21 mg/L, TP: 0.
  • the average water flux is 12.19 LML, and the average power density is 2.2 W/m 2 .
  • the membrane orientation is AL-DS
  • the average water flux under the same conditions is 12.19 LMH
  • the average power density is 2.2 W/m 2 , which are both 1.57 times that of Example 2.
  • the water flux and power density were always higher than those of Example 2.
  • AL-FS when AL-DS is running, the degree of contamination of the FO membrane is similar to that in Example 2, and there is no obvious blockage. It can be seen that when the membrane orientation is AL-DS, the optimal operating effect can be obtained.
  • the influent water is municipal sewage, water quality: COD: 330 ⁇ 10.1 mg/L, NH 4 + -N: 24.88 ⁇ 1.50 mg/L, TN: 38.24 ⁇ 1.68 mg/L, TP: 2.08 ⁇ 0.13 mg/L.
  • the SS in the bioreactor is 3 g/L activated sludge, the draw fluid is 2 M NaCl, the pressure applied on the draw fluid side is 0 bar, the membrane orientation is AL-DS (active layer toward the draw fluid), and it runs for 4 hours.
  • Effluent water quality COD: 12 ⁇ 2.45 mg/L, NH 4 + -N: 5.11 ⁇ 0.30 mg/L, TN: 4.63 ⁇ 0.38 mg/L, TP: 0.
  • the average water flux is 13.54 LMH, and the average power density is 0 W/m 2 .

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

一种同步回收水和电能的污水处理装置及方法，方法包括以下步骤：以城市污水作为进水，将泥水混合液作为进料液，通过蠕动泵（2）进入FO膜组件（6）的进料液通道，以盐水作为汲取液，通过高压泵（8）进入FO膜组件（6）的汲取液通道。利用FO膜两侧的渗透压差，使水从进料液侧流向汲取液侧，混合后的汲取液具有较高的压力，在流出的过程中推动涡轮机（7）转动，进而产生电能。稀释后的汲取液通过汲取液回收系统，获得回用水，同时浓缩后的汲取液继续用于FO膜，能够使得能源利用更加充分。

Description

一种同步回收水和电能的污水处理装置及方法 技术领域
本发明涉及一种同步回收水和电能的污水处理装置及方法，属于污水处理领域。
 背景技术
膜生物反应器（MBRs）作为一种生物处理与膜分离技术相结合的新型污水处理技术，具有出水水质好且稳定、占地面积小、剩余污泥产量低等优势，在城市污水和工业废水处理领域得到了广泛应用，被誉为21世纪最有发展前途的水处理技术之一。然而，MBR还存在出水水质有待进一步提升、能耗较高、膜污染严重等问题。
正渗透膜生物反应器（OMBR）是国外学者于2008年提出的一种新型MBR替代工艺。它使用新型正渗透（FO）膜替代传统MBR中压力驱动式膜分离过程，是一种将生物处理和FO膜组合而成的新型工艺。根据FO膜组件与生物反应器的相对位置关系，OMBR可以分为浸没式OMBR（FO膜组件在生物反应器内）和外置式OMBR（FO膜组件在生物反应器外）。浸没式OMBR占地面积小，减少了泥水混合液的循环泵，但是FO膜组件不容易拆卸且膜污染控制效果略差。外置式OMBR便于拆卸且水力学条件好，更容易控制膜污染，但是增加了占地面积。FO膜的推动力是渗透压差，FO过程不需施加外加压力作为驱动力，水分子能够自发地从水化学势高的原料液部分渗透到水化学势低的汲取液部分。与压力驱动过程相比，FO膜具有更小的膜污染趋势。由于FO膜对污染物的截留性能更好，OMBR的出水水质优于传统MBR，可以直接进行回用。正是由于出水水质更好、膜污染趋势更小等特点，OMBR已经受到了越来越多的关注。
目前商用的FO膜包括两层，一层是起到截留作用的活性层，一层是起到支撑作用的支撑层。活性层比较薄且致密，抗污染能力较强，而支撑层较厚且多孔，易于产生膜污染。因此，在FO膜运行过程中存在两种膜朝向，一种是活性层朝向原料液（AL-FS），一种是支撑层朝向原料液（AL-DS）。与AL-DS相比，AL-FS膜污染趋势更小，但是膜通量更小。现有的OMBR运行时，考虑到FO膜面向的是含有各种污染物的活性污泥，为了减缓膜污染，一般采用AL-FS朝向。
事实上，在OMBR运行过程中，FO膜两侧存在盐差能，盐差能是不同溶液混合时产生的能量，与太阳能和风能相比，受气相和地理条件影响小，且在海洋中储量巨大。虽然FO过程中存在盐差能，但由于FO污水处理过程中产生的渗透水量太少，相应的功率密度（等于汲取液侧的压力乘以产水量）较小，盐差能的回收困难。压力延滞渗透(PRO)是利用盐差能进行产能的新型膜工艺。与FO膜相比，PRO在汲取液一侧施加小于渗透压差的外加压力，增加了渗透过程中产生的功率密度，从而可以回收盐差能。具体来说，在PRO中，水从进料液（低盐度）一侧通过半渗透膜流向汲取液（高盐度）一侧，由于PRO组件汲取液侧容积一定，混合后的汲取液和进料液与原本的汲取液相比具有更高的压力，可在流出的过程中推动涡轮机发电。目前，PRO主要处理对象为河水、湖水、海水等地表水，缺少在污水处理中的应用。此外，由于地表水中的污染物浓度较低，PRO运行过程中进料液中污染物的浓缩及其后处理都未涉及到。
 技术问题
现有的OMBR在运行时汲取液需要采用反渗透、膜蒸馏等技术进行回收，能耗较高，影响了技术的经济可行性。虽然FO过程中存在盐差能，但由于FO污水处理过程中产生的渗透水量太少，相应的功率密度（等于汲取液侧的压力乘以产水量）较小，盐差能的回收困难。
现有的PRO在运行时，对于进料液实际上是一个浓缩过程，即水透过FO膜进入汲取液而污染物被截留在进料液一侧，这就导致进料液存在碳、氮、磷等污染物的富集问题以及后续处理复杂的问题。
 技术解决方案
为了解决上述问题，本发明提供了结合OMBR和PRO产能的工艺，建立了基于同步回收水和电能的新型污水处理技术，在保留OMBR优点的基础上，获取额外的电能，降低汲取液后处理的能耗。
本发明的第一个目的是提供一种同步回收水和电能的污水处理装置，所述装置包括进水池、生物反应器、FO膜组件、涡轮机、汲取液池和汲取液回收系统；所述进水池与生物反应器相连，所述FO膜组件包括汲取液通道、进料液通道和FO膜，所述FO膜将汲取液通道和进料液通道隔开，所述进料液通道的入口和进料液通道的出口均与生物反应器相连，所述汲取液池与汲取液通道的入口相连，所述汲取液通道的出口通过涡轮机与汲取液池相连，所述汲取液池与汲取液回收系统相连。
在本发明的一种实施方式中，所述进水池与生物反应器相连的管道上安装有泵。
在本发明的一种实施方式中，所述生物反应器与进料液通道的入口相连的管道上安装有泵。
在本发明的一种实施方式中，所述汲取液池与汲取液通道的入口相连的管路上安装有高压泵。
在本发明的一种实施方式中，所述生物反应器的下部安装有曝气管，气泵一端与曝气管连接。
在本发明的一种实施方式中，所述汲取液回收系统包括电导率仪、高压泵和反渗透组件，其中，汲取液池、高压泵、反渗透组件和汲取液池依次连接构成循环，所述电导率仪与高压泵连接，并控制高压泵的开启和关闭，所述电导率仪的检测端位于汲取液池内部。
在一种实施方式中，所述膜组件由不锈钢或者有机塑料材质加工而成，所述FO膜组件还包括垫片，位于FO膜的一侧。
在本发明的一种实施方式中，所述FO膜是醋酸纤维（CTA）膜、聚酰胺（TFC）膜、水通道蛋白膜或聚醚砜树脂（PES）膜中的任一种。
在本发明的一种实施方式中，所述FO膜包括支撑层和活性层，所述活性层朝向汲取液。
本发明的第二个目的是提供一种同步回收水和电能的污水处理的方法，所述方法是利用上述污水处理装置进行处理污水。
在本发明的一种实施方式中，所述污水为城市污水，水质指标为：COD：200-500 mg/L，NH 4 +-N：20-50 mg/L，TN：30-50 mg/L，TP：2-7 mg/L。
在本发明的一种实施方式中，所述方法，具体包括以下步骤：
1）以城市污水作为进水，进入生物反应器内与活性污泥混合后，经由泵将混合得到的泥水混合物泵入FO膜的进料液通道，汲取液通过高压泵进入膜组件中的汲取液通道，利用FO膜两侧的渗透压差，使水从进料液通道流向汲取液通道；
2）同时在汲取液通道侧施加一定的压力，稀释后的汲取液通过涡轮机并推动涡轮机转动，进而产生电能；当汲取液浓度过低时，汲取液回收系统启动，汲取液经过反渗透组件进行浓缩并回收得到水。
在本发明的一种实施方式中，所述泥水混合液循环速率为0.1-0.5 L/min。
在本发明的一种实施方式中，所述接种污泥为SS为3-9 g/L的活性污泥。
在本发明的一种实施方式中，所述汲取液为0.5-4M的NaCl、MgCl 2、KCl、CaCl 2溶液。
在本发明的一种实施方式中，所述在汲取液通道侧施加的压力小于FO膜两侧的渗透压。
在本发明的一种实施方式中，所述在汲取液通道侧施加的压力为4-8 bar。
在本发明的一种实施方式中，所述当汲取液浓度过低时是指FO膜的渗透压差小于汲取液通道侧施加的压力时。
 有益效果
（1）本发明通过将OMBR和PRO的产能优势相结合，利用生物处理和FO膜截留回收污水的同时，具有较高压力的混合后的汲取液在流出的过程中推动涡轮机转动产电，构建得到了同步回收水和电能的新型污水处理装置和方法，使得能源利用更加充分。
（2）本发明的FO膜得到的浓水无需进行焚烧或进一步化学处理，只需回流至生物反应器，则可通过生物的作用除去碳、氮、磷等污染物，解决了现有的PRO在运行时的碳、氮、磷等污染物的富集问题，本发明方法处理更加经济、环保。
 附图说明
图1为本发明的同步回收水和电能的污水处理装置的一种实施方式的结构示意图；图中，1—进水池，2—蠕动泵，3—生物反应器，4—气泵，5—蠕动泵，6—FO膜组件，7—涡轮机，8—高压泵，9—汲取液池，10—电导率仪，11—高压泵，12—反渗透组件。
 本发明的实施方式
下面结合实施例，对本发明的具体实施方式作进一步详细描述。以下实施例用于说明本发明，但不用来限制本发明的范围。
实施例1
结合图1，具体介绍一下本发明的一种同步回收水和电能的污水处理装置，本发明的装置包括进水池1、生物反应器3、FO膜组件6、涡轮机7、汲取液池9和汲取液回收系统。进水池1通过蠕动泵2与生物反应器3相连，FO膜组件6包括汲取液通道、进料液通道、垫片和FO膜，垫片和FO膜平行安放且二者将汲取液通道和进料液通道隔开，进料液通道的入口和进料液通道的出口均与生物反应器3相连，汲取液池9通过高压泵8与汲取液通道的入口相连，汲取液通道的出口通过涡轮机7与汲取液池9相连，所述汲取液回收系统包括电导率仪10、高压泵11和反渗透组件12，且汲取液池9、高压泵11、反渗透组件12和汲取液池9依次连接构成循环，电导率仪10与高压泵11连接，用于控制高压泵的开启和关闭，电导率仪10的检测端位于汲取液池9的内部。
进一步的，所述生物反应器3下部安装有曝气管，气泵一端与曝气管连接。
进一步的，所述膜组件由不锈钢或者有机塑料材质加工而成，所述FO膜是醋酸纤维（CTA）膜、聚酰胺（TFC）膜、水通道蛋白膜或聚醚砜树脂（PES）膜中的任一种。
上述装置的运行原理为：以城市污水作为进水，城市污水进入生物反应器内与活性污泥混合后，经由泵将混合得到的泥水混合物泵入FO膜的进料液通道，汲取液通过高压泵进入膜组件中的汲取液通道，利用FO膜两侧的渗透压差，使水从进料液通道流向汲取液通道；同时在汲取液通道侧施加一定的压力，稀释后的汲取液通过涡轮机并推动涡轮机转动，进而产生电能；当汲取液浓度过低时，汲取液回收系统启动，汲取液经过反渗透组件进行浓缩并回收得到水。
实施例2
利用图1所示的装置处理城市污水。
鉴于FO的结构（一层是起到截留作用的活性层，一层是起到支撑作用的支撑层。活性层比较薄且致密，抗污染能力较强，而支撑层较厚且多孔，易于产生膜污染），以及本发明中FO膜面向的是含有各种污染物的活性污泥，为了减缓FO膜污染，本实施例的OMBR运行时采用AL-FS朝向（活性层朝向进料液）。
进水为城市污水，水质：COD：350±12.2 mg/L，NH 4 +-N：24.88±1.50 mg/L，TN：38.24±1.68 mg/L，TP：2.08±0.13 mg/L。生物反应器中SS（悬浮固体）为3 g/L的活性污泥，汲取液为2 M NaCl，汲取液侧施加的压力为6bar，膜朝向为AL-FS（活性层朝向进料液），运行24 h。
出水水质：COD：10±2.45 mg/L，NH 4 +-N：4.41±0.40 mg/L，TN：4.49±0.53 mg/L，TP：0；平均水通量为7.79 LMH，平均产电功率密度为1.4 W/m 2。
可见，按照通常的做法（即FO膜朝向为AL-FS）最终得到的平均水通量仅为7.79 LML，平均产电功率密度仅为1.4 W/m 2。
实施例3
为了进一步提高平均产电功率，发明人尝试采用非常规的FO膜朝向，即AL-DS（活性层朝向汲取液），进行试验。
本实施例方法中，进水为城市污水，水质：COD：350±12.2 mg/L，NH 4 +-N：24.88±1.50 mg/L，TN：38.24±1.68 mg/L，TP：2.08±0.13mg/L。生物反应器中SS为3 g/L的活性污泥，汲取液为2 M NaCl，汲取液侧施加的压力为6bar，膜朝向为AL-DS（活性层朝向汲取液），运行4h。
出水水质：COD：10±1.51 mg/L，NH 4 +-N：5.12±0.90 mg/L，TN：5.53±1.21 mg/L，TP：0。平均水通量为12.19 LML，平均产电功率密度为2.2 W/m 2。
可以发现，将活性层朝向汲取液时（膜朝向为AL-DS），相同条件下的平均水通量为12.19 LMH，平均产电功率密度为2.2 W/m 2，均为实施例2的1.57倍。此外，运行的24h过程中，水通量和功率密度始终高于实施例2的膜通量和功率密度。与AL-FS相比，AL-DS朝向运行时，FO膜的污染程度与实施例2中的相似，并未产生明显的堵塞。可见，膜朝向为AL-DS时，能够获得最优的运行效果。
实施例4
本实施例方法中，进水为城市污水，水质：COD：330±10.1 mg/L，NH 4 +-N：24.88±1.50 mg/L，TN：38.24±1.68 mg/L，TP：2.08±0.13mg/L。生物反应器中SS为3 g/L的活性污泥，汲取液为2 M NaCl，汲取液侧施加的压力为0 bar，膜朝向为AL-DS（活性层朝向汲取液），运行4h。
出水水质：COD：12±2.45 mg/L，NH 4 +-N：5.11±0.30 mg/L，TN：4.63±0.38 mg/L，TP：0。平均水通量为13.54 LMH，平均产电功率密度为0 W/m 2。
可以发现，当汲取液侧不施加压力时，虽然通量也很稳定，但不产电。通过对膜面污染物的分析发现，加压运行后的膜面污染物为0.78 g/m 2，而不加压运行的膜面污染物为1.52g/m 2。可见，加压运行后的膜面污染物明显减少，这表明加压运行较不加压运行的膜污染更轻。
虽然本发明已以较佳实施例公开如上，但其并非用以限定本发明，任何熟悉此技术的人，在不脱离本发明的精神和范围内，都可做各种的改动与修饰，因此本发明的保护范围应该以权利要求书所界定的为准。

Claims (20)

  1. 一种同步回收水和电能的污水处理方法，其特征在于，所述方法是利用同步回收水和电能的污水处理装置处理污水；所述同步回收水和电能的污水处理装置包括进水池、生物反应器、FO膜组件、涡轮机、汲取液池和汲取液回收系统；所述进水池与生物反应器相连，所述FO膜组件包括汲取液通道、进料液通道和FO膜，所述FO膜将汲取液通道和进料液通道隔开，所述进料液通道的入口和进料液通道的出口均与生物反应器相连，所述汲取液池与汲取液通道的入口相连，所述汲取液通道的出口通过涡轮机与汲取液池相连，所述汲取液池与汲取液回收系统相连；
    所述方法，具体包括以下步骤：
    1）以城市污水作为进水，进入生物反应器内与活性污泥混合后，经由泵将混合得到的泥水混合物泵入FO膜的进料液通道，汲取液通过高压泵进入膜组件中的汲取液通道，利用FO膜两侧的渗透压差，使水从进料液通道流向汲取液通道；
    2）同时在汲取液通道侧施加一定的压力，稀释后的汲取液通过涡轮机并推动涡轮机转动，进而产生电能；当汲取液浓度过低时，汲取液回收系统启动，汲取液经过反渗透组件进行浓缩并回收得到水；其中，进水为城市污水，水质：COD：350±12.2 mg/L，NH 4 +-N：24.88±1.50 mg/L，TN：38.24±1.68 mg/L，TP：2.08±0.13mg/L；生物反应器中SS为3 g/L的活性污泥，汲取液为2 M NaCl，汲取液侧施加的压力为6bar，膜的活性层朝向汲取液，运行4h。
  2. 一种同步回收水和电能的污水处理装置，其特征在于，所述装置包括进水池、生物反应器、FO膜组件、涡轮机、汲取液池和汲取液回收系统；所述进水池与生物反应器相连，所述FO膜组件包括汲取液通道、进料液通道和FO膜，所述FO膜将汲取液通道和进料液通道隔开，所述进料液通道的入口和进料液通道的出口均与生物反应器相连，所述汲取液池与汲取液通道的入口相连，所述汲取液通道的出口通过涡轮机与汲取液池相连，所述汲取液池与汲取液回收系统相连。
  3. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述进水池与生物反应器相连的管道上安装有泵。
  4. 根据权利要求2任一所述的一种同步回收水和电能的污水处理装置，其特征在于，所述生物反应器与进料液通道的入口相连的管道上安装有泵。
  5. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述汲取液池与汲取液通道的入口相连的管路上安装有高压泵。
  6. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述生物反应器的下部安装有曝气管，气泵一端与曝气管连接。
  7. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述汲取液回收系统包括电导率仪、高压泵和反渗透组件，其中，汲取液池、高压泵、反渗透组件和汲取液池依次连接构成循环，所述电导率仪与高压泵连接，所述电导率仪的检测端位于汲取液池内部。
  8. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述FO膜组件由不锈钢或者有机塑料材质加工而成，所述FO膜组件还包括垫片，位于FO膜的一侧。
  9. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述FO膜是醋酸纤维膜、聚酰胺膜、水通道蛋白膜或聚醚砜树脂膜中的任一种。
  10. 根据权利要求2所述的一种同步回收水和电能的污水处理装置，其特征在于，所述FO膜包括支撑层和活性层，所述活性层朝向汲取液。
  11. 一种同步回收水和电能的污水处理的方法，其特征在于，所述方法是利用权利要求2~10任一所述的污水处理装置处理污水。
  12. 根据权利要求11所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述污水为城市污水。
  13. 根据权利要求12所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述城市污水的水质指标为：COD：200-500 mg/L，NH 4 +-N：20-50 mg/L，TN：30-50 mg/L，TP：2-7 mg/L。
  14. 根据权利要求11~13任一所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述方法，具体包括以下步骤：
    以城市污水作为进水，进入生物反应器内与活性污泥混合后，经由泵将混合得到的泥水混合物泵入FO膜的进料液通道，汲取液通过高压泵进入膜组件中的汲取液通道，利用FO膜两侧的渗透压差，使水从进料液通道流向汲取液通道；同时在汲取液通道侧施加一定的压力，稀释后的汲取液通过涡轮机并推动涡轮机转动，进而产生电能；当汲取液浓度过低时，汲取液回收系统启动，汲取液经过反渗透组件进行浓缩并回收得到水。
  15. 根据权利要求14所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述泥水混合液循环速率为0.1-0.5 L/min。
  16. 根据权利要求14所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述接种污泥为SS为3-9 g/L的活性污泥。
  17. 根据权利要求14所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述汲取液为0.5-4M的NaCl、MgCl 2、KCl、CaCl 2溶液。
  18. 根据权利要求14所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述在汲取液通道侧施加的压力小于FO膜两侧的渗透压。
  19. 根据权利要求14所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述在汲取液通道侧施加的压力为4-8 bar。
  20. 根据权利要求14所述的一种同步回收水和电能的污水处理的方法，其特征在于，所述当汲取液浓度过低时是指FO膜的渗透压差小于汲取液通道侧施加的压力时。
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