WO2019119756A1 - 一种餐厨厌氧废水半短程硝化启动方法 - Google Patents

一种餐厨厌氧废水半短程硝化启动方法 Download PDF

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WO2019119756A1
WO2019119756A1 PCT/CN2018/092179 CN2018092179W WO2019119756A1 WO 2019119756 A1 WO2019119756 A1 WO 2019119756A1 CN 2018092179 W CN2018092179 W CN 2018092179W WO 2019119756 A1 WO2019119756 A1 WO 2019119756A1
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reactor
semi
short
nitrification
kitchen
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English (en)
French (fr)
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张周
阮文权
赵明星
缪恒锋
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江南大学
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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
    • C02F3/02—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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
    • 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
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • 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
    • C02F2209/02—Temperature
    • 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
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • 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
    • C02F2209/38—Gas flow rate
    • 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 a semi-short-length nitrification starting method for a kitchen anaerobic wastewater, belonging to the field of kitchen wastewater treatment.
  • kitchen waste is a major component of urban domestic waste, accounting for about 37-62% of urban domestic waste. According to statistics from the Institute of Solid Waste Pollution Control and Resource Reconstruction of Tsinghua University, China's cities produce more than 60 million tons of kitchen waste per year. Kitchen waste is mainly composed of organic substances such as starch, food cellulose and animal fat. Therefore, kitchen waste is a misplaced resource.
  • the utilization of kitchen waste resources can solve the problem of “garbage pigs” caused by improper disposal of kitchen waste and the return of the “ditch oil” to the table to endanger human health.
  • Kitchen waste will inevitably be produced in the process of kitchen waste.
  • anaerobic digestion is used to remove a large amount of organic matter from the kitchen waste water.
  • the kitchen waste water after anaerobic digestion has high COD and high NH 4 + -N.
  • Low C/N and other characteristics, if the traditional denitrification process will inevitably lead to long processing flow, high operating costs, and because of its C / N imbalance, denitrification process carbon source is insufficient, resulting in low TN removal rate, difficult to meet standard emissions.
  • the short-cut nitrification process can control the nitrification process in the NO 2 - -N stage and accumulate a large amount of nitrite.
  • Semi-short-length nitrification can be combined with denitrification or anaerobic ammonium oxidation to form a better combination of biological denitrification, especially for the treatment of high NH 4 + -N and low C / N wastewater.
  • how to control the nitrification process in the NO 2 - -N stage, accumulating a large amount of nitrite is the research focus.
  • the current research on short-cut nitrification technology is mainly to control DO concentration, FA concentration, temperature and pH.
  • a wastewater such as kitchen waste water with a COD concentration higher than 1500 mg/L, a NH 4 + -N concentration higher than 1000 mg/L and a lower C/N
  • the semi-short-length nitrification process needs to be properly diluted to gradually increase the substrate concentration.
  • a chemical inhibitor such as potassium chlorate (KClO 3 ) is needed to inhibit the activity of nitrite oxidizing bacteria (NOB) to achieve the start-up and operation of the semi-short-length nitrification reaction.
  • the object of the present invention is to provide a method for starting a semi-short-length nitrification process for anaerobic wastewater of a kitchen, to provide an appropriate influent water for the anaerobic ammonium oxidation process, and to solve the problem of low TN removal rate of the anaerobic wastewater of the kitchen.
  • a first object of the present invention is to provide a semi-short-length nitrification reactor comprising a reactor body, an aeration device, a temperature on-line monitor, a DO online monitor, a pH on-line analyzer, and a PLC control system;
  • the monitor, the DO online monitor, and the pH on-line analyzer respectively extend into the reactor through the probe, and the other end is connected to the PLC control system;
  • the bottom of the reactor body is provided with an aeration device, the aeration device is disposed on the reactor body
  • the external air pump is connected; the air pump is also connected to the PLC control system;
  • the heating device is connected to the side wall of the reactor, and the heating device is connected to the PLC control system;
  • the stirring device is arranged inside the reactor, and the stirring device is connected with the PLC control system.
  • the agitation device is a precision agitator.
  • the PLC control system is also connected to the remote monitoring system and exchanges data information and control information with the remote monitoring system via a wired network.
  • a drain valve and a mud discharge valve are further disposed on a sidewall of the reactor body; the sludge discharge valve is disposed at a bottom of the reactor; the drain valve is disposed at an upper portion of the reactor body .
  • the bottom of the reactor is provided with an air inlet, the air inlet is connected to the air pump through a pipeline, and a gas flow meter is arranged between the air inlet and the air pump.
  • the reactor is made of stainless steel.
  • the heating device is a silicone heating belt.
  • an asbestos layer is further disposed on the outer side of the silica gel heating belt.
  • a second object of the present invention is to provide a method for starting a semi-short-length nitrification process for a kitchen anaerobic wastewater, which is to inoculate sludge with aerobic sludge in the process of kitchen waste water treatment, and to treat kitchen waste.
  • the oxygen wastewater is used as the influent water, and the reactor is used to control the reactor DO to start the semi-short-length nitrification process at 0.5-0.6 mg/L.
  • the operating cycle of the reactor includes a water infusion phase, a continuous agitation and aeration phase, a stationary precipitation phase, and a transient drainage phase.
  • the starting process specifically includes the following steps:
  • Dilution rate of anaerobic wastewater in the kitchen diluted 5 to 0 times, gradually increasing the influent ammonia nitrogen concentration in stages; after 5 times dilution, the COD is 356-487 mg/L, and the NH 4 + -N is 156-262 mg/L. After dilution 2 times, COD 645 ⁇ 842mg / L, NH 4 + -N 553 ⁇ 731mg / L; undiluted kitchen anaerobic raw water COD is 1510 ⁇ 2130mg / L, NH 4 + - N is 983 ⁇ 1510mg / L , the pH of the reactor water is controlled to be maintained at 7-8 by sodium bicarbonate;
  • the SBR operation mode is adopted.
  • the operation cycle includes: 8 to 10 minutes of influent water, continuous aeration and aeration for 6 to 8 hours, static precipitation for 2 to 3 hours, drainage for 8 to 15 minutes, and hydraulic retention time (HRT) of 8 to 10 hours.
  • the step is specifically:
  • the three different dilution rates of the kitchen anaerobic wastewater are: diluted 5 times, 2 times, 0 times to gradually increase the influent ammonia nitrogen concentration; after 5 times dilution, the COD is 356 ⁇ 487 mg / L, NH 4 + -N is 156 ⁇ 262mg / L; diluted 2 times, COD 645 ⁇ 842mg / L, NH 4 + -N 553 ⁇ 731mg / L; undiluted kitchen anaerobic raw water COD is 1510 ⁇ 2130mg / L, NH 4 + -N is 983 ⁇ 1510mg / L, the pH of the reactor water is controlled to be maintained at 7 ⁇ 8 by sodium bicarbonate;
  • the test adopts SBR operation mode.
  • the operation cycle includes: water inflow for 10 min, continuous stirring and aeration for 8 h, static sedimentation for 2 h, drainage for 10 min, hydraulic retention time (HRT) for 10 h, two cycles per day, each cycle
  • the water intake and displacement are both 5L.
  • the temperature of the startup process is controlled at 30 ⁇ 1 ° C, and the temperature is stabilized by the on-line temperature control system and the heating device.
  • the continuous agitation and aeration stage control DO is between 0.5 and 0.6 mg/L.
  • the method of the invention utilizes a semi-short-length nitrification reactor independently designed and developed, and the DO concentration of the system is linked with the air pump to limit the DO concentration in the system, and simultaneously control the reaction temperature and pH to obtain a better nitrite nitrogen. Accumulated, the ratio of ammonia nitrogen and nitrite nitrogen in the effluent is suitable for anaerobic ammonium oxidation process.
  • the concentration of DO By controlling the concentration of DO, enriching a large amount of AOB, eliminating NOB, using this technology to control ammonia nitrogen in the nitrite stage, controlling effluent nitrite nitrogen and
  • the ammonia-nitrogen molar ratio provides favorable conditions for the subsequent treatment process, which saves a large amount of carbon source and energy compared to conventional nitrification and denitrification. Since the influent COD of the final stage of the reactor is 1510-2130 mg/L and the NH 4 + -N is 983-1510 mg/L, the semi-short-length nitrification process initiated by the method of the invention has high ammonia nitrogen and COD load, and can be better. Treatment of high concentration ammonia nitrogen wastewater.
  • the semi-short-length nitrification process initiated by the method of the present invention is stable in operation and can maintain a high nitrosation rate for a long time.
  • the nitrite nitrogen to ammonia nitrogen molar ratio is suitable for the hydration demand of the anaerobic ammonium oxidation process.
  • Figure 1 is a schematic view showing the structure of a semi-short-length nitrification reactor of the present invention; wherein; 1, an air pump; 2, a gas flow meter; 3, an aeration device; 4, a temperature online monitor; 5, a precision agitator; Monitor; 7, pH on-line analyzer; .8, heating device; 9, PLC control system; 10, remote monitoring system; 11, drain valve; 12, mud valve;
  • Figure 2 shows the trend of trinitrogen evolution during startup
  • Figure 3 shows the trend of COD change during startup
  • Figure 4 shows the effect of DO concentration on the operating efficiency of a semi-short-length nitrification system.
  • the difference in concentration of nitrite nitrogen and nitrate nitrogen in the influent and water, respectively, is mg/L.
  • the semi-short-length nitrification reactor is a stainless steel tubular structure.
  • the other end of the air pump 1 is connected to the PLC control system 9; a gas flow meter 2 is arranged between the air inlet and the air pump 1; an aeration device 3 is arranged at the bottom of the reactor, and the air is passed by the air pump 1 The gas flow meter 2 reaches the aeration device 3 provided at the bottom of the reactor, and is aerated by the air pump 1 during the aeration period to provide dissolved oxygen inside the system.
  • the side wall of the reactor is provided with a drain valve 11 and a mud discharge valve 12, and the mud discharge valve 12 is disposed in the near bottom region; after the end of each cycle, the drain valve is used for drainage, and at the same time, the reactor is regularly drained.
  • the top of the reactor is equipped with a precision stirrer. The power of the stirrer is constant at 100W and the speed is 0-300rpm.
  • the reactor is also equipped with a temperature online monitor 4, a DO online monitor 6, and a pH online analyzer 7, which are respectively arranged in the reactor.
  • the internal probe connection monitors the internal parameters of the reactor; the temperature online monitor 4, the DO online monitor 6, and the pH online analyzer 7 are also respectively connected with the PLC control system 9 to transmit signals to the PLC control system 9; DO The probe transmits the DO concentration in the reactor to the PLC control system 9, and the PLC control system feeds back to the air pump 1 to form a linkage to more accurately control the DO concentration in the system;
  • the reactor is provided with a heating and insulating belt 8 along the sidewall;
  • the heating The heat insulating tape 8 is a silica gel heating belt, and the heating and heat insulating tape 8 is connected with the PLC control system 9 and is linked with the temperature online monitor 4, and the temperature of the reactor is monitored by the temperature online monitor 4, and the temperature information is transmitted to the PLC control system.
  • the heating state of the heating and heat insulating belt 8 is adjusted by the PLC control system, that is, when the temperature exceeds the set temperature, the heating and insulating belt 8 stops heating; when the temperature is lower than the set temperature, 8 starts heating with thermal insulation.
  • An asbestos layer is placed on the periphery of the heating belt for heat preservation, and the heat preservation area is 0.25 m 2 .
  • the PLC control system 9 is also connected to the remote monitoring system 10, transmits real-time data of the reactor to the remote monitoring system 10 through wired data transmission, or transmits the control operation of the remote monitoring system 10 to the PLC control system to implement feedback control.
  • the sludge was inoculated into the semi-short-length nitrification reactor, and the sludge was inoculated from the aerobic tank sludge in the A 3 /O 3 process of the kitchen waste water treatment plant.
  • the sludge concentration was 6 g/L, and the sludge after inoculation was strong in the reactor.
  • the SBR operation mode is adopted, and the operation cycle includes water inflow for 10 min, continuous stirring and aeration for 8 h, static precipitation for 2 h, and drainage for 10 min. It runs two cycles a day, each with a water intake and displacement of 5L. At the beginning of the cycle, 5L of water enters the reactor through the peristaltic pump, and at the same time, the precision stirring device is started, so that the muddy water is fully mixed. When the water inlet phase is completed, the air pump is turned on to aerate the reactor to control the DO concentration and the reactor temperature. And stirring speed. After 8 hours, the stirring and aeration devices were turned off at the same time, and the static sedimentation stage was entered. After standing for 2 hours, the drainage valve 12 was used to drain 5 L. The sludge discharge frequency was 1 time/week during the test period.
  • the semi-short-length nitrification start-up process of anaerobic wastewater in kitchen is divided into three stages.
  • the first stage dilutes the influent water by 5 times. After the effluent sub-digestibility and ammonia-nitrogen conversion rate are stable for 3 to 5 cycles, the second stage is entered. In the stage, the influent water is diluted twice, and the effluent sub-digestibility and ammonia-nitrogen conversion rate are stabilized for 3 to 5 cycles, and then enter the third stage.
  • the temperature of the reactor is controlled to 30 ⁇ 1°C throughout the process, and the DO concentration in the aeration phase is controlled to 0.5-0.6mg/L.
  • the kitchen wastewater was diluted 5 times as the reactor water.
  • the diluted COD was 356-487 mg/L, with an average of 404 mg/L and NH 4 + -N 156. ⁇ 262 mg / L, an average of 199 mg / L.
  • the conversion of NH 4 + -N in the first 6 cycles showed a downward trend (Fig. 1), indicating that low dissolved oxygen hindered the ammoxidation, and the accumulation of NO 2 - -N in the effluent did not completely convert to NO as in the whole process.
  • the COD removal rate is kept at a high level, and the activity of the heterotrophic bacteria is inhibited as the reactor is oxygen-limited.
  • the effluent COD value showed an upward trend, while the COD removal rate remained at about 60% (Fig. 2).
  • the NO 3 - -N in the effluent showed a downward trend, while NO 2 - - N has a steady upward trend, and the nitrosation rate of the whole process has increased significantly, gradually increasing to over 80%.
  • the COD removal rate decreased significantly, which may be due to the sudden increase of COD load, the failure of heterotrophic bacteria to adapt, and the low COD removal rate.
  • the removal rate of COD has a tendency to rise slowly, and finally it is maintained at about 63%.
  • the undiluted kitchen waste water was directly added to the reaction system, the COD was 1510-2130 mg/L, and the NH 4 + -N was 983-1510 mg/L.
  • the NH 4 + -N conversion rate is basically maintained above 60%
  • the effluent NO 3 - -N continues to decline
  • the NO 2 - -N concentration continues to rise
  • the nitrosation rate also rises, basically maintaining at 90%.
  • the effluent COD removal rate is maintained between 60% and 70%
  • the effluent nitrite nitrogen to ammonia nitrogen molar ratio is 1.0 to 1.3:1, which satisfies the influent requirements for subsequent treatment. At this point the semi-short-length nitrification system has been successfully started.
  • the DO concentration is lower than 0.5mg/L, the system COD removal rate is lower, the sub-digestibility is low, and the molar ratio of effluent nitrite nitrogen to ammonia nitrogen is 1:2 ⁇ 1:4; the aeration time increases, and the same amount of NH 4 is oxidized.
  • the + -N rate is slower and the startup time required is longer.
  • the too low DO concentration inhibits the growth of AOB while suppressing NOB, so the nitrosation rate also decreases.
  • DO is higher than 0.6mg/L
  • the system COD removal rate increases, the nitrosation rate decreases, the effluent cannot reduce the ammonia nitrogen oxidation control in the nitrous acid phase, and a large part of the nitrite nitrogen is oxidized to nitrate nitrogen;
  • the concentration may damage the stability of the system.
  • the DO concentration is higher than 1.0 mg/L, the DO concentration no longer becomes the influencing factor of NOB inhibition. As the NOB activity gradually recovers, NO 3 - -N is further oxidized to NO 3 by NOB. — N, the reaction system was destroyed.

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Abstract

一种餐厨厌氧废水半短程硝化启动方法，针对废水高氨氮、低C/N比特性，通过短程硝化反应器，利用AOB和NOB氧饱和常数的区别，通过限制反应器内部DO浓度来富集AOB，同时控制温度、碱度等其他条件获得亚硝酸盐的积累，达到了快速启动半短程硝化工艺，出水满足后续厌氧氨氧化工艺进水的需求。还公开了一种半短程硝化反应器。

Description

一种餐厨厌氧废水半短程硝化启动方法 技术领域
本发明涉及一种餐厨厌氧废水半短程硝化启动方法，属于餐厨污水处理领域。
背景技术
随着经济的快速增长、城市进程的加快，城市餐厨垃圾的产生量持续增长，由此对环境造成的污染也日益严重，餐厨垃圾的减量化、无害化、资源化处置已经成为当今研究的热点。餐厨垃圾是城市生活垃圾的主要组成部分，占城市生活垃圾的比例约为37～62％。据清华大学固体废物污染控制及资源化研究所的统计数据表明，我国城市每年产生餐厨垃圾6000万吨以上。餐厨垃圾以淀粉类、食物纤维素、动物脂肪类等有机物质为主要成分。所以餐厨垃圾是一种放错了位置的资源，餐厨垃圾资源化利用可以解决餐厨垃圾因处置不当引起的“垃圾猪”问题及“地沟油”回流餐桌危害人体健康的问题。
餐厨垃圾在处理过程中必然会产生餐厨废水，通常采用厌氧消化手段去除餐厨废水中大量的有机物，经过厌氧消化处理后的餐厨废水具有高COD、高NH 4 +-N、低C/N等特点，如果采用传统脱氮工艺必然导致处理流程长，运行费用高，而且会因为其C/N失衡，反硝化过程碳源不足，导致TN去除率低，难以达标排放。近年来随着一些新型脱氮工艺的兴起，如厌氧氨氧化工艺、短程硝化反硝化工艺等，对于这种高COD、高NH 4 +-N、低C/N废水有了一些较好的处置方法。相比传统脱氮工艺，新型生物脱氮工艺在能源、碳源、占地面积等方面较传统脱氮工艺有着明显的优势。
短程硝化工艺可以将硝化过程控制在NO 2 --N阶段，积累大量的亚硝酸盐。半短程硝化可与反硝化或者厌氧氨氧化组成新的组合工艺，能够较好的进行生物脱氮，特别适用于高NH 4 +-N、低C/N废水的处理。不论短程硝化与反硝化还是厌氧氨氧化工艺，如何将硝化过程控制在NO 2 --N阶段，积累大量的亚硝酸盐都是研究重点。当前针对短程硝化技术的研究主要是控制DO浓度、FA浓度、温度和pH等来实现。但针对如餐厨废水此类COD浓度高于1500mg/L、NH 4 +-N浓度高于1000mg/L且C/N较低的废水启动半短程硝化工艺需要进行适当稀释，逐步提高基质浓度，或需要外加化学抑制剂如氯酸钾(KClO 3)来抑制亚硝酸盐氧化细菌(NOB)活性，实现半短程硝化反应的启动和运行。
发明内容
本发明的目的是要提供一种餐厨厌氧废水半短程硝化工艺启动方法，为厌氧氨氧化工艺提供适宜的进水，解决餐厨厌氧废水TN去除率低等问题。
本发明的第一个目的是提供一种半短程硝化反应器，包括反应器本体、曝气装置、温度在线监测仪、DO在线监测仪、pH在线测定仪；和PLC控制***；所述温度在线监测仪、DO在线监测仪、pH在线测定仪分别通过探头伸入至反应器内部，另一端均与PLC控制***连接；反应器本体的底部设置曝气装置，曝气装置与设置在反应器本体外部的空气泵连接；空气泵还与PLC控制***连接；反应器侧壁设置加热装置，所述加热装置与PLC控制***连接；反应器内部设置搅拌装置，所述搅拌装置与PLC控制***连接。
在本发明的一种实施方式中，所述搅拌装置为精密搅拌器。
在本发明的一种实施方式中，所述PLC控制***还与远程监控***连接，并通过有线网络与远程监控***交换数据信息和控制信息。
在本发明的一种实施方式中，所述反应器本体的侧壁上还设置排水阀和排泥阀；所述排泥阀设置在近反应器底部；所述排水阀设置于反应器本体上部。
在本发明的一种实施方式中，反应器底部设有进气口，进气口通过管道与空气泵连接，进气口和空气泵之间设置气体流量计。
在本发明的一种实施方式中，所述反应器由不锈钢材质制成。
在本发明的一种实施方式中，所述加热装置为硅胶加热带。
在本发明的一种实施方式中，所述硅胶加热带外侧还设置石棉层。
本发明的第二个目的是提供一种餐厨厌氧废水半短程硝化工艺的启动方法，所述方法是以餐厨废水处理过程中的好氧污泥为接种污泥，以餐厨垃圾厌氧废水作为进水，应用所述的反应器控制反应器DO在0.5～0.6mg/L进行半短程硝化工艺的启动。
在本发明的一种实施方式中，反应器的运行周期包括进水阶段、连续搅拌并曝气阶段、静置沉淀阶段和瞬时排水阶段。
在本发明的一种实施方式中，所述启动过程具体包括如下步骤：
1)接种来源于餐厨废水处理工艺、污泥浓度为4～6g/L并经过强曝气的好氧池污泥，DO浓度控制在6～8mg/L；
2)餐厨厌氧废水稀释率为：稀释5～0倍，分阶段逐步提高进水氨氮浓度；稀释5倍后，COD为356～487mg/L，NH 4 +-N为156～262mg/L；稀释2倍后，COD 645～842mg/L，NH 4 +-N 553～731mg/L；不稀释餐厨厌氧原水COD为1510～2130mg/L，NH 4 +-N为983～1510mg/L，通过碳酸氢钠控制反应器进水pH保持在7～8；
3)采用SBR运行方式，运行周期包括：进水8～10min、连续搅拌并曝气6～8h、静置沉淀2～3h、排水8～15min，水力停留时间(HRT)为8～10h。
在本发明的一种实施方式中，所述步骤具体为：
1)接种餐厨废水处理工艺中好氧池污泥，污泥浓度为6g/L，取出的好氧污泥需进行强曝气1d，DO浓度控制在6～8mg/L，污泥具有完全硝化能力；
2)将餐厨厌氧废水设置3种不同的稀释率分别为：稀释5倍、2倍、0倍以逐步提高进水氨氮浓度；稀释5倍后，COD为356～487mg/L，NH 4 +-N为156～262mg/L；稀释2倍后，COD 645～842mg/L，NH 4 +-N 553～731mg/L；不稀释餐厨厌氧原水COD为1510～2130mg/L，NH 4 +-N为983～1510mg/L，通过碳酸氢钠控制反应器进水pH保持在7～8；
3)试验采用SBR运行方式，运行周期包括：进水10min、连续搅拌并曝气8h、静置沉淀2h、排水10min，水力停留时间(HRT)为10h，每天运行两个周期，每个周期的进水量和排水量均为5L。
在本发明的一种实施方式中，启动过程的温度控制在30±1℃，通过在线温度控制***和加热装置进行联动，保持反应器内部温度稳定。
在本发明的一种实施方式中，连续搅拌并曝气阶段控制DO在0.5～0.6mg/L。
有益效果：(1)经本发明通过限制***的DO浓度，使***中NOB受到抑制，AOB得到富集，能够快速实现半亚硝化***的启动，稳定后***NH 4 +-N转化率为60％左右，亚硝化率达到90％以上，出水COD去除率保持在60％～70％之间，出水亚硝态氮与氨氮摩尔比为1.0～1.3:1，满足厌氧氨氧化进水要求，对餐厨厌氧废水深度脱氮处理提供基础条件。
(2)本发明的方法利用自主设计研发的半短程硝化反应器，将***DO浓度和空气泵形成联动，限制***中的DO浓度，同时控制反应温度和pH，获得较好的亚硝态氮累计，出水氨氮和亚硝酸盐氮比例适合厌氧氨氧化工艺，利用DO浓度的控制，富集大量AOB，淘汰NOB，采用此技术将氨氮控制在亚硝酸盐阶段，控制出水亚硝态氮与氨氮摩尔比为后续处理工艺提供有利条件，此方法相对于传统硝化反硝化可节省大量碳源和能源。由于反应器最后阶段进水COD为1510～2130mg/L，NH 4 +-N为983～1510mg/L，本发明所述方法启动的半短程硝化工艺具有较高的氨氮和COD负荷，能够较好的处理高浓度氨氮废水。通过反应器运行效果见本发明所述方法启动的半短程硝化工艺运行稳定，能够长期保持较高的亚硝化率，出水亚硝态氮与氨氮摩尔比适合厌氧氨氧化工艺的进水需求。
附图说明
图1为本发明的半短程硝化反应器结构示意图；其中；1，空气泵；2，气体流量计；3，曝气装置；4，温度在线监测仪；5，精密搅拌器；6，DO在线监测仪；7，pH在线测定仪；.8，加热装置；9，PLC控制***；10，远程监控***；11，排水阀；12，排泥阀；
图2为启动过程中三氮变化趋势；
图3为启动过程中COD变化趋势；
图4为DO浓度对半短程硝化***运行效能的影响。
具体实施方式
Figure PCTCN2018092179-appb-000001
式中:
Figure PCTCN2018092179-appb-000002
分别为进出水亚硝态氮和硝态氮的浓度差，mg/L。
实施例1
半短程硝化反应器为不锈钢筒状结构，设计参数：底部直径(φ)×高(H)＝30cm×30cm，有效容积为15L，反应器底部的侧壁上设有进气口，进气口通过管道与空气泵1连接，空气泵1的另一端连接PLC控制***9；进气口和空气泵1之间设置气体流量计2；反应器底部设置曝气装置3，空气由空气泵1通过气体流量计2到达反应器底部设置的曝气装置3，在曝气时间段采用空气泵1进行曝气，为***内部提供溶解氧。所述曝气装置3是由16个微孔曝气头组成，通过通气管道由反应器底部中心位置向四周均匀发散分布，每个曝气头直径(φ)＝2cm。反应器侧壁设置排水阀11和排泥阀12，排泥阀12设置于近底部区域；每周期结束后由排水阀进行排水，同时，反应器定时排泥。反应器顶部设有精密搅拌器，搅拌器功率恒定为100W，转速0～300rpm，反应器还设有温度在线监测仪4、DO在线监测仪6、pH在线测定仪7，分别与设置在反应器内部的探头连接，对反应器内部各参数进行监测；温度在线监测仪4、DO在线监测仪6、pH在线测定仪7还分别与PLC控制***9连接，将信号传输至PLC控制***9；DO探头将反应器内的DO浓度传递至PLC控制***9，PLC控制***反馈给空气泵1形成联动，以便更加精确的控制***内DO浓度；反应器沿侧壁设置加热保温带8；所述加热保温带8为硅胶加热带，加热保温带8与PLC控制***9连接，并与温度在线监测仪4形成联动，通过温度在线监测仪4监测反应器内部温度,将温度信息传输至PLC控制***，再经PLC控制***调节加热保温带8的加热状态，即当温度超过设定温度时，加热保温带8停止加热；当温度低于设定温度时，加热保温带8开始加热。硅胶加热带通过玻璃胶固定于池体不锈钢板，分布方式为据池体底部5、15、25cm处四周布置，加热带总功率为3×100W＝300W。在加热带***设置石棉层进行保温，保温面积为0.25m 2。
PLC控制***9还与远程监控***10连接，通过有线数据传输将反应器的实时数据传输至远程监控***10，或将远程监控***10的控制操作传输至PLC控制***，实现反馈控制。
实施例2
向半短程硝化反应器接种污泥，接种污泥来自餐厨废水处理厂A 3/O 3工艺中好氧池污泥，污泥浓度为6g/L，接种后的污泥在反应器中强曝气1d，DO控制在6～8mg/L，温度控制30±1℃，让污泥具有完全硝化能力。
采用SBR运行方式，运行周期包括进水10min、连续搅拌并曝气8h、静置沉淀2h、排水10min。每天运行两个周期，每个周期的进水量和排水量均为5L。周期开始时将5L进水通过蠕动泵进入反应器，并同时开始精密搅拌装置，使得泥水充分混合，当完成进水阶段后，开启空气泵对反应器进行曝气，控制DO浓度、反应器温度和搅拌速度。8h后对同时关闭搅拌和曝气装置，进入静置沉淀阶段，静置2h后，通过排水阀12进行排水5L。试验阶段排泥频率为1次/周。
餐厨厌氧废水半短程硝化启动过程分为3个阶段，第一阶段将进水稀释5倍，出水亚消化率和氨氮转化率连续3～5个周期稳定后，进入第二阶段；第二阶段将进水稀释2倍，出水亚消化率和氨氮转化率连续3～5个周期稳定后，进入第3阶段。整个过程反应器温度控制30±1℃，曝气阶段DO浓度控制0.5～0.6mg/L。启动初期为了让污泥具有较好的适应性，将餐厨废水稀释5倍作为反应器进水，稀释后的COD为356～487mg/L，平均为404mg/L，NH 4 +-N为156～262mg/L，平均为199mg/L。前6个周期NH 4 +-N转化率呈下降趋势(图1)，说明低的溶解氧阻碍了氨氧化作用，同时出水有NO 2 --N的积累，并没有如全程硝化完全转化成NO 3 --N，且前6个周期出水中的NO 3 --N浓度有小幅上升，但随着反应的进行，氨氮的转化率基本维持在60％左右，出水中NO 3 --N出现下降，亚硝化率不断上升，说明由于硝化细菌氧饱和常数高于亚硝化细菌的氧饱和常数，在较低DO环境下，硝化细菌的活性受到较大抑制，生长速率较慢，NO 2 --N转化成NO 3 --N的过程受到抑。由于反应器运行初期接种的污泥是经过强曝气的污泥异养菌活性较好，COD去除率保持在较高水平，随着对反应器进行限氧，抑制了异养菌的活性，在第10～24个周期，出水COD值明显呈现上升趋势，同时COD去除率维持在60％左右(图2)。
启动初期维持24个周期后，进入活性提高期，开始减小对餐厨废水的稀释率，稀释2倍后餐厨废水水质为COD 645～842mg/L，NH 4 +-N 553～731mg/L。在活性提高期，NH 4 +-N转化率基本维持在60％左右。较低的DO环境致使硝酸细菌不能适应，其活性逐渐受到抑制，逐步被淘汰出整个亚硝化***，进入第二个阶段以后出水中的NO 3 --N有下降的趋势，而NO 2 --N有平稳上升的趋势，整个过程亚硝化率上升明显，逐步增加至80％以上。活性提高期的前几个周期中COD去除率有明显下降，可能是由于COD负荷突然增加，异养菌未能适应，造成COD去除率低的现象。但随着反应器的运行，COD去除率有缓慢上升 的趋势，最后也基本维持在63％左右。
第三阶段将不经稀释的餐厨废水直接加入反应***中，COD为1510～2130mg/L，NH 4 +-N为983～1510mg/L。在这个过程中NH 4 +-N转化率基本维持在60％以上，出水NO 3 --N继续下降，而NO 2 --N浓度继续上升，亚硝化率也随之上升，基本保持在90％以上，出水COD去除率保持在60％～70％之间，出水亚硝态氮与氨氮摩尔比为1.0～1.3:1，满足后续处理的进水要求。此时半短程硝化***已成功启动。
实施例3
具体实施方式同实施例2，区别在于，控制不同DO浓度，研究DO浓度对于反应体系的影响，在SBR工艺成功实现稳定NO 2 --N积累后，改变***中的DO浓度，考察不同DO浓度下亚硝化***运行效能的影响。此阶段进水COD浓度平均为1874mg/L、NH 4 +-N、NO 2 --N、NO 3 --N平均值为1231mg/L、2mg/L和29mg/L，设置6个不同的DO浓度阶段。
DO浓度低于0.5mg/L，***COD去除率较低，亚消化率低，出水亚硝态氮与氨氮摩尔比为1:2～1:4；曝气时间增加，氧化相同量的NH 4 +-N速率变慢，所需要的启动时间更长。但是过低的DO浓度在抑制NOB的同时也抑制了AOB的生长，所以亚硝化率也随之下降。
当DO高于0.6mg/L，***COD去除率增加，亚硝化率降低，出水不能降氨氮氧化控制在亚硝态氮阶段，一大部分亚硝态氮会被氧化至硝态氮；提高DO浓度可能会破坏***的稳定性，当DO浓度高于1.0mg/L时，DO浓度不再成为抑制NOB的影响因子，随着NOB活性逐渐恢复，NO 3 --N被NOB进一步氧化成NO 3 —N，反应***遭到破坏。
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 (10)

  1. 一种半短程硝化反应器，其特征在于，包括反应器本体、曝气装置、温度在线监测仪、DO在线监测仪、pH在线测定仪和PLC控制***；所述温度在线监测仪、DO在线监测仪、pH在线测定仪的一端分别通过探头伸入至反应器本体内部，另一端均与PLC控制***连接；反应器本体的底部设置曝气装置，曝气装置与设置在反应器本体外部的空气泵连接；所述空气泵还与PLC控制***连接；反应器侧壁设置加热装置，所述加热装置与PLC控制***连接；反应器内部设置搅拌装置，所述搅拌装置与PLC控制***连接。
  2. 根据权利要求1所述的一种半短程硝化反应器，其特征在于，所述加热装置为硅胶加热带。
  3. 根据权利要求2所述的一种半短程硝化反应器，其特征在于，所述硅胶加热带外还设置石棉层。
  4. 根据权利要求1所述的一种半短程硝化反应器，其特征在于，反应器本体的底部设有进气口，进气口通过管道与空气泵连接，进气口和空气泵之间设置气体流量计。
  5. 根据权利要求4所述的一种半短程硝化反应器，其特征在于，反应器本体的侧壁上还设置排水阀和排泥阀；所述排泥阀设置在近反应器底部；所述排水阀设置于反应器本体上部。
  6. 根据权利要求1～5任一所述的一种半短程硝化反应器，其特征在于，所述PLC控制***还与远程监控***连接，并通过有线网络与远程监控***交换数据信息和控制信息。
  7. 一种餐厨厌氧废水半短程硝化工艺的启动方法，其特征在于，以餐厨废水处理过程中的好氧污泥为接种污泥，以餐厨垃圾厌氧废水作为进水，应用权利要求1～5任一所述的反应器进行半短程硝化工艺的启动。
  8. 根据权利要求7所述的方法，其特征在于，控制反应器DO在0.5～0.6mg/L；启动过程的温度控制在29～31℃。
  9. 根据权利要求7所述的方法，其特征在于，反应器的运行周期包括进水阶段、连续搅拌并曝气阶段、静置沉淀阶段和瞬时排水阶段。
  10. 根据权利要求7～9任一所述的方法，其特征在于，所述启动过程具体包括如下步骤：
    1)接种来源于餐厨废水处理工艺、污泥浓度为4～6g/L并经过强曝气的好氧池污泥，DO浓度控制在6～8mg/L；
    2)餐厨厌氧废水稀释率为：稀释5～0倍，分阶段逐步提高进水氨氮浓度；第一阶段稀释后，COD为356～487mg/L，NH 4 +-N为156～262mg/L；第二阶段稀释后，COD 645～842mg/L，NH 4 +-N 553～731mg/L；不经过稀释的餐厨厌氧原水COD为1510～2130mg/L，NH 4 +-N为983～1510mg/L，通过碳酸氢钠控制反应器进水pH保持在7～8；
    3)采用SBR运行方式，运行周期包括：进水8～10min、连续搅拌并曝气6～8h、静置沉淀2～3h、排水8～15min，水力停留时间(HRT)为8～10h。
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