WO2018028059A1 - 有机废水的处理方法以及有机废水处理系统 - Google Patents

有机废水的处理方法以及有机废水处理系统 Download PDF

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WO2018028059A1
WO2018028059A1 PCT/CN2016/104543 CN2016104543W WO2018028059A1 WO 2018028059 A1 WO2018028059 A1 WO 2018028059A1 CN 2016104543 W CN2016104543 W CN 2016104543W WO 2018028059 A1 WO2018028059 A1 WO 2018028059A1
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fermentation
nitrogen
organic wastewater
anaerobic fermentation
wastewater
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English (en)
French (fr)
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陈银广
任洪强
郑雄
黄海宁
刘辉
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Tongji University
Nanjing University
Nanjing Tech University
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Tongji University
Nanjing University
Nanjing Tech University
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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
    • 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
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • 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
    • C02F3/28—Anaerobic digestion processes

Definitions

  • the invention belongs to the technical field of wastewater treatment, and relates to a method for treating organic wastewater and an organic wastewater treatment system.
  • Organic wastewater usually contains carbon, nitrogen, phosphorus and other pollutants.
  • Carbon pollutants are generally expressed by COD.
  • Nitrogen pollutants are mostly nitrate nitrogen.
  • Phosphorus pollutants are generally referred to as soluble phosphates. These pollutants must be removed and discharged. It can only be discharged after the standard.
  • Traditional anaerobic digestion techniques primarily convert organic matter to methane, and additional carbon sources are required to remove nitrogen and phosphorus.
  • the present invention is directed to the deficiencies of the prior art, and the main object is to provide a method for treating organic wastewater.
  • Another object of the present invention is to provide an organic wastewater treatment system capable of realizing the above-described method for treating organic wastewater.
  • the solution of the present invention is:
  • a method for treating organic wastewater comprising the steps of:
  • the mixture is subjected to denitrification and dephosphorization treatment, and then precipitated to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the organic wastewater may be protein-containing wastewater
  • the pH of the anaerobic fermentation may be 9 ⁇ 0.5, preferably 9, and the anaerobic fermentation may be performed for 1 hour to 24 days, preferably 12 hours. day.
  • the organic wastewater needs to be inoculated with anaerobic fermentation microorganisms before the anaerobic fermentation, which comes from the waste sludge produced by the protein processing plant when discharging the protein-containing wastewater.
  • the inoculum of the waste sludge is 5 ⁇ 1% of the volume of the organic wastewater.
  • the organic wastewater may be a carbohydrate-containing wastewater, and the pH of the anaerobic fermentation is 8 ⁇ 0.5.
  • the time for anaerobic fermentation may be from 0.5 hours to 16 days, preferably 8 days.
  • the organic wastewater needs to be inoculated with anaerobic fermentation microorganisms before the anaerobic fermentation, which is derived from the waste sludge produced by the carbohydrate processing plant when discharging the carbohydrate-containing wastewater.
  • the inoculum of the waste sludge is 3.8 ⁇ 1% of the volume of the organic wastewater.
  • the fermentation broth in the step (1) may contain 70% by weight or more of propionic acid and contains 30% by weight or less of acetic acid.
  • the pH of the nitrogen and phosphorus removal treatment is 7.5 ⁇ 0.5, preferably 7.5.
  • the mixed liquid in the step (4) is mixed with a part of the precipitate before the denitrification and dephosphorization treatment, and the organic wastewater in the step (1) is mixed with the remaining portion of the precipitate before the anaerobic fermentation.
  • a portion of the precipitate may comprise from 0.5 to 50% by weight of the total precipitate.
  • An organic wastewater treatment system for realizing the above-mentioned method for treating organic wastewater comprising:
  • An anaerobic fermentation reactor for anaerobic fermentation of organic wastewater to obtain a fermentation broth
  • the fermentation liquid separation device separates the remaining portion of the fermentation liquid, and removes the residue to obtain a fermentation liquid containing propionic acid;
  • a nitrogen-phosphorus biological removal reactor for mixing a fermentation broth containing nitrate nitrogen and a fermentation broth containing propionic acid to obtain a mixed solution for denitrification and dephosphorization;
  • the organic wastewater treatment system may further comprise: a distributor that adds a part of the precipitate to the nitrogen-phosphorus biological removal reactor and mixes it with the mixed liquid phase before the denitrification and dephosphorization treatment, and the remaining part of the precipitate It is added to the anaerobic fermentation reactor and mixed with the organic wastewater before the anaerobic fermentation.
  • a portion of the precipitate may comprise from 0.5 to 50% by weight of the total precipitate.
  • the pH of the anaerobic fermentation reactor during anaerobic fermentation may be 9 ⁇ 0.5, preferably 9, and the anaerobic fermentation time is from 1 hour to 24 days, preferably 12 days.
  • the organic wastewater needs to be inoculated with anaerobic fermentation microorganisms before the anaerobic fermentation, which comes from the waste sludge produced by the protein processing plant when discharging the protein-containing wastewater.
  • the inoculum of the waste sludge is 5 ⁇ 1% of the volume of the organic wastewater.
  • the pH of the anaerobic fermentation reactor during anaerobic fermentation may be 8 ⁇ 0.5, preferably 8, and the anaerobic fermentation time is 0.5 hours to 16 days, preferably 8 days. .
  • the organic wastewater needs to be inoculated with anaerobic fermentation microorganisms before the anaerobic fermentation, which is derived from the waste sludge produced by the carbohydrate processing plant when discharging the carbohydrate-containing wastewater.
  • the inoculum of the waste sludge is 3.8 ⁇ 1% of the volume of the organic wastewater.
  • the fermentation broth discharged from the anaerobic fermentation reactor contains 70% by weight or more of propionic acid and contains 30% by weight or less of acetic acid.
  • the mixing ratio of the nitrate-containing fermentation broth and the propionic acid-containing fermentation broth is such that the ratio of the total nitrogen to the total phosphorus to the biological oxygen demand is 1: (8-15), preferably 1:11.
  • the present invention obtains a fermentation broth containing a large amount of short-chain fatty acids (such as propionic acid) by controlling the conditions of anaerobic fermentation of organic wastewater, and then divides the fermentation broth into two parts, a part of which is subjected to nitration reaction to bring ammonia nitrogen. It is converted into nitrate nitrogen which is easily used by subsequent nitrogen and phosphorus removal microorganisms, and the other part is mixed with the fermentation liquid obtained by the nitrification reaction. When the obtained mixture is subjected to nitrogen and phosphorus removal treatment, the nitrogen and phosphorus removal system is used. It already contains enough carbon source (short-chain fatty acid).
  • short-chain fatty acids such as propionic acid
  • the present invention can optimize the balance of carbon, nitrogen and phosphorus without additional carbon source, nitrogen source and phosphorus source, and is beneficial to nitrogen and phosphorus removal microorganisms. Simultaneous and efficient removal of carbon, nitrogen and phosphorus.
  • the present invention controls the organic wastewater to be converted into short-chain fatty acids by controlling the conditions of anaerobic fermentation of organic wastewater, instead of being converted into methane, which not only can fully utilize the carbon source, but also reduce greenhouse gas emissions.
  • the present invention combines the obtained partial precipitate (sludge) with organic wastewater and then puts it in an anaerobic fermentation reactor for anaerobic fermentation, which not only promotes the production of short-chain fatty acids, but also realizes the sludge. Resource utilization reduces the amount of sludge generated.
  • Figure 1 is a first schematic view of an organic wastewater treatment system of the present invention.
  • Figure 2 is a second schematic view of the organic wastewater treatment system of the present invention.
  • Anaerobic fermentation reactor 1 aeration tank 2, fermentation liquid separation device 3, nitrogen and phosphorus biological removal reactor 4, first conditioning tank 5, fermentation liquid separation device 6, fermentation liquid storage tank 7, second conditioning tank 8, Sedimentation tank 9 and distributor 10.
  • the invention provides a method for treating organic wastewater and an organic wastewater treatment system.
  • the invention provides a method for treating organic wastewater, which comprises the following steps:
  • volume V 1 ' (2) nitrating a part of the fermentation broth (volume V 1 ') to obtain a fermentation broth containing nitrate nitrogen; separating the remaining part of the fermentation broth (volume V 2 '), removing the residue, and obtaining a liquid as a fermentation liquid containing propionic acid;
  • the organic wastewater may be protein-containing wastewater
  • the protein-containing wastewater is preferably dairy wastewater or food processing wastewater.
  • Dairy waste water is waste water discharged from condensed milk, cheese, butter, dairy refreshing drinks, ice cream and dairy snacks in the production process, mainly from washing water of containers and equipment, which contains dairy raw materials.
  • the pH of the anaerobic fermentation system may be 9 ⁇ 0.5, preferably 9; the time of anaerobic fermentation may be 1 hour to 24 days, preferably 12 days.
  • the average temperature during anaerobic fermentation was 28 °C.
  • VSS/TSS average value of VSS/TSS
  • the organic wastewater may be a carbohydrate-containing wastewater, and the carbohydrate-containing wastewater may preferably be beer wastewater.
  • Beer wastewater refers to the wastewater discharged during the beer production process, which includes wastewater generated by raw material cleaning and wastewater generated during beer brewing.
  • the pH of the anaerobic fermentation system may be 8 ⁇ 0.5, preferably 8, and the anaerobic fermentation may be from 0.5 hours to 16 days, preferably 8 days.
  • the temperature of the anaerobic fermentation was 23 °C. Before anaerobic fermentation, it is necessary to inoculate the waste sludge produced by the alcohol production plant when discharging alcohol wastewater (yellow-black, containing anaerobic fermentation microorganisms, the average value of VSS/TSS is 0.86), and the inoculum is 3.8 of the volume of the starting organic wastewater. %.
  • the organic wastewater in step (1) may have a BOD of 2240-3100 mg/L, a total nitrogen of 90-120 mg/L, an ammonia nitrogen of 85-106 mg/L, and a total phosphate of 20-28.3 mg/L.
  • the fermentation broth obtained in the step (1) contains 70% by weight or more of propionic acid.
  • the fermentation broth obtained in the step (1) is divided into two parts (volumes V 1 ' and V 2 ', respectively).
  • a part of it (volume V 1 ') is subjected to a nitration reaction to convert ammonia nitrogen into nitrate nitrogen, and carbon is converted into carbon dioxide to obtain a fermentation broth containing nitrate nitrogen; the remaining portion (volume V 2 ') Separation is carried out to remove the residue, and the liquid is retained to obtain a fermentation liquid containing propionic acid.
  • the waste sludge generated by the garbage treatment plant in the treatment of the landfill leachate (yellow-black, containing nitrifying microorganisms, and the average value of VSS/TSS is 0.71) is required, and the inoculum amount is desired.
  • the fermentation broth (volume V 1 ') volume of the nitration reaction was 3%; the temperature of the nitration reaction was 24 °C.
  • the mixing ratio of the nitrate-containing fermentation broth and the propionic acid-containing fermentation broth is such that the ratio of the total nitrogen concentration and the total phosphorus concentration of the mixed solution to the biological oxygen demand (BOD) is 1 : (8-15), preferably 1:11.
  • BOD biological oxygen demand
  • the ratio to be 1: (8-15) on the one hand, it can satisfy the amount of carbon source required for microbial growth and metabolism during nitrogen and phosphorus removal, and on the other hand, it can ensure that the treated wastewater does not cause a large amount of carbon source to cause excessive Secondary pollution.
  • the total nitrogen concentration was measured by potassium persulfate oxidation method, the total phosphorus concentration was measured by ammonium molybdate spectrophotometry, and the biological oxygen demand was measured by microbial sensor method.
  • the mixing ratio of the nitrate-containing fermentation broth and the propionic acid-containing fermentation broth is: a nitrate-containing fermentation broth
  • the volume ratio of the mixed liquid may be 6.25 to 60.25%, and the volume ratio of the fermentation liquid containing propionic acid to the mixed liquid may be 39.75 - 93.75%.
  • the conditions for the nitrogen and phosphorus removal treatment of the mixed solution are: the pH value of the nitrogen and phosphorus removal system may be 7.5 ⁇ 0.5, preferably 7.5; the municipal sewage treatment plant needs to be inoculated before the nitrogen and phosphorus removal treatment.
  • the waste sludge produced is light yellow and contains nitrogen and phosphorus removal microorganisms.
  • the average value of VSS/TSS is 0.65; the inoculum is 8% of the volume of the mixture; the reaction temperature is 22 °C.
  • the mixture is subjected to denitrification and dephosphorization treatment, and precipitation is continued to obtain a supernatant and a precipitate.
  • the supernatant is the purified water and can be directly discharged or used.
  • the precipitate is sludge.
  • the sludge can be divided into two parts, a part of the sludge (accounting for 0.5-50% by weight of the total sludge) is mixed with the mixed liquid phase before the denitrification and dephosphorization treatment, and then denitrification and dephosphorization treatment; the remaining part
  • the sludge is mixed with the organic wastewater before the anaerobic fermentation, followed by anaerobic fermentation.
  • the present invention achieves the balance of carbon, nitrogen and phosphorus in the process of nitrogen and phosphorus removal by controlling the mixing ratio of the two fermentation liquids, and the efficient simultaneous removal of carbon, nitrogen and phosphorus can be realized without additional carbon source supplementation.
  • the present invention provides an organic wastewater treatment system for realizing the above-described method for treating organic wastewater, comprising: an anaerobic fermentation reactor 1, an aeration tank 2, a fermentation liquid separation device 3, and a nitrogen-phosphorus biological system.
  • an anaerobic fermentation reactor 1 for realizing the above-described method for treating organic wastewater, comprising: an anaerobic fermentation reactor 1, an aeration tank 2, a fermentation liquid separation device 3, and a nitrogen-phosphorus biological system.
  • the reactor 4 and the sedimentation tank 9 are removed.
  • the anaerobic fermentation reactor 1 is used for anaerobic fermentation of organic wastewater to obtain a fermentation liquid containing 70% by weight or more of propionic acid.
  • the organic wastewater may be protein-containing wastewater
  • the protein-containing wastewater refers to waste water having a higher protein content in the wastewater than other non-protein organic matter, preferably dairy wastewater and food processing wastewater.
  • Dairy waste water is waste water discharged from condensed milk, cheese, butter, dairy refreshing drinks, ice cream and dairy snacks in the production process, mainly from washing water of containers and equipment, which contains dairy raw materials.
  • Food processing wastewater refers to wastewater produced during the processing of foods (such as cakes, breads, etc.).
  • the pH of the anaerobic fermentation system may be 9 ⁇ 0.5, preferably 9, and the anaerobic fermentation may be carried out for 1 hour to 24 days, preferably 12 days.
  • the organic wastewater may be a carbohydrate-containing wastewater
  • the carbohydrate-containing wastewater refers to a content of carbohydrates in the wastewater higher than that of other non-carbohydrates, and may preferably be beer wastewater.
  • Beer wastewater refers to the wastewater discharged during the beer production process, which includes wastewater generated by raw material cleaning and wastewater generated during beer brewing.
  • the pH of the anaerobic fermentation system may be 8 ⁇ 0.5, preferably 8, and the anaerobic fermentation may be carried out for 0.5 hours to 16 days, preferably 8 days.
  • the aeration tank 2 is used for performing a nitrification reaction on a part of the fermentation liquid (volume V 1 '), converting the ammonia nitrogen into nitrate nitrogen, and converting carbon (indicated by COD) into carbon dioxide, thereby obtaining nitrate-containing nitrogen. Fermentation broth.
  • the fermentation broth entering the aeration tank 2 contains short-chain fatty acids (such as propionic acid, etc.), ammonia nitrogen and phosphate, and the liquid discharged from the aeration tank 2 contains short-chain fatty acids (such as propionic acid, etc.), nitrate nitrogen or nitrite. Nitrogen, phosphate, etc.
  • the fermentation broth separation device 3 includes a fermentation broth separation device 6 and a fermentation broth storage tank 7.
  • the fermentation liquid separation device 6 is for separating the remaining portion (volume V 2 ') of the fermentation liquid, removing the residue, and retaining only the liquid to obtain a fermentation liquid containing propionic acid.
  • the fermentation broth storage tank 7 is used to store the propionic acid-containing fermentation broth.
  • the nitrogen and phosphorus biological removal reactor 4 is used for mixing a fermentation broth containing nitrate nitrogen and a fermentation broth containing propionic acid to obtain a mixed solution for denitrification and dephosphorization.
  • the mixing ratio of the nitrate-containing fermentation broth and the propionic acid-containing fermentation broth should be such that the ratio of the total nitrogen to total phosphorus concentration of the mixture to its biological oxygen demand (BOD) is 1: (8-15). It is preferably 1:11.
  • BOD biological oxygen demand
  • the conditions for the nitrogen and phosphorus removal treatment of the mixed solution are as follows: the pH of the nitrogen and phosphorus removal system may be 7.5 ⁇ 0.5, preferably 7.5.
  • the nitrogen and phosphorus-removing microorganisms in the nitrogen-phosphorus biological removal reactor 4 can be converted into intracellular carbon sources under anaerobic fermentation conditions.
  • the nitrogen and phosphorus removal microorganisms have sufficient intracellular carbon source, so under the conditions of hypoxia or aerobic fermentation
  • the intracellular carbon source is decomposed and the energy and reducing power generated by the decomposition of the intracellular carbon source are utilized for phosphorus absorption and denitrification reaction, thereby simultaneously removing the carbon source, the nitrogen source and the phosphorus source in the mixed solution. Since the nitrogen and phosphorus removal microorganism of the present invention has sufficient carbon source available for dephosphorization and denitrification, simultaneous removal of the nitrogen source and the phosphorus source can be achieved without adding an additional carbon source.
  • the sedimentation tank 9 actually functions as a secondary settling tank for precipitating the effluent of the nitrogen-phosphorus bioremover to obtain a supernatant and a precipitate.
  • the supernatant is the purified water and can be directly discharged or used.
  • the precipitate is sludge.
  • the sludge can be divided into two parts, a part of the sludge (accounting for 0.5-50% by weight of the total sludge) is mixed with the mixed liquid phase before the denitrification and dephosphorization treatment, and the remaining part of the sludge is before the anaerobic fermentation.
  • the organic wastewater is mixed.
  • the above organic wastewater treatment system processes the organic wastewater including the following steps:
  • Anaerobic fermentation reactor 1 anaerobic fermentation of organic wastewater to obtain a fermentation broth
  • the aeration tank 2 performs a nitrification reaction on a part of the fermentation liquid (volume V 1 ') to obtain a fermentation liquid containing nitrate nitrogen; the remainder of the fermentation liquid separation device 6 on the fermentation liquid (volume V 2 ) ') separating, removing the residue, obtaining a liquid as a fermentation liquid containing propionic acid, and temporarily storing the propionic acid-containing fermentation liquid in the fermentation liquid storage tank 7;
  • the sedimentation tank 9 precipitates the effluent of the nitrogen-phosphorus biological removal reactor 4 to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the organic wastewater treatment system may further include: a first conditioning tank 5, a second conditioning tank 8, and a distributor 10.
  • the first conditioning tank 5 is used to uniformly adjust the amount of water and water quality of the organic wastewater, and then the homogeneous organic wastewater enters the anaerobic fermentation reactor 1. Since the flow rate or nature of the organic wastewater often fluctuates, it is necessary to provide the first conditioning tank 5 in order to regulate the flow or properties of the organic wastewater to stabilize it, and to prevent the drastic changes in the flow or properties of the organic wastewater to subsequent treatments. The process has a large impact.
  • the second conditioning tank 8 is used to uniformly adjust the water quantity and water quality of the mixed liquid, and then the homogeneous mixed liquid enters the nitrogen phosphorus biological removal reactor 4.
  • the distributor 10 is used for adding a part of the precipitate to the nitrogen-phosphorus biological removal reactor 4 and mixing it with the mixed liquid phase before the denitrification and dephosphorization treatment, and then performing the denitrification and dephosphorization treatment;
  • the remainder of the precipitate is added to the anaerobic fermentation reactor 1 and mixed with the organic wastewater before the anaerobic fermentation, and then subjected to an anaerobic fermentation process.
  • the above organic wastewater treatment system processes the organic wastewater including the following steps:
  • the first regulating tank 5 adjusts the water quantity and the water quality of the organic wastewater uniformly;
  • the aeration tank 2 performs a nitrification reaction on a part of the fermentation liquid (volume V 1 ') to obtain a fermentation liquid containing nitrate nitrogen; and the remainder of the fermentation liquid separation device 6 on the fermentation liquid (volume is V 2 ) ') separating, removing the residue, obtaining a liquid as a fermentation liquid containing propionic acid, and temporarily storing the propionic acid-containing fermentation liquid in the fermentation liquid storage tank 7;
  • the second adjusting tank 8 adjusts the water quantity and the water quality of the mixed liquid uniformly
  • the sedimentation tank 9 precipitates the effluent of the nitrogen-phosphorus biological removal reactor 4 to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the dispenser 10 adds a part of the precipitate to the nitrogen-phosphorus biological removal reactor 4 and mixes it with the mixed liquid phase before the denitrification and dephosphorization treatment, and then performs the above-described nitrogen and phosphorus removal treatment, The remainder of the precipitate is added to the anaerobic fermentation reactor 1 and mixed with the organic wastewater before the anaerobic fermentation, and then the above anaerobic fermentation process is carried out.
  • the embodiment provides a method for treating organic wastewater, which comprises the following steps:
  • the organic wastewater (dairy wastewater) enters the first conditioning tank 5, and the first conditioning tank 5 uniformly adjusts the water quantity and water quality of the organic wastewater;
  • the BOD of the dairy wastewater is 2240 mg/L, and the total nitrogen is 111.6 mg/ L, ammonia nitrogen is 105mg / L, total
  • the phosphate is 28.3 mg / L;
  • the anaerobic fermentation reactor 1 performs anaerobic fermentation on the effluent of the first conditioning tank 5 (homogeneous organic wastewater) to obtain a fermentation broth; the pH of the anaerobic fermentation system may be 8.5, and the fermentation time (hydraulicity) The residence time, HRT) was 1 hour; the obtained fermentation broth had a propionic acid content of 74% and an acetic acid content of 25%.
  • the aeration tank 2 performs a nitrification reaction on a part of the fermentation liquid (volume V 1 ') to obtain a fermentation liquid containing nitrate nitrogen; and the remainder of the fermentation liquid separation device 6 on the fermentation liquid (volume is V 2 ) ') separating, removing the residue, obtaining a liquid as a fermentation liquid containing propionic acid, and temporarily storing the propionic acid-containing fermentation liquid in the fermentation liquid storage tank 7;
  • the second adjusting tank 8 adjusts the water quantity and the water quality of the mixed liquid uniformly
  • the sedimentation tank 9 precipitates the effluent of the nitrogen-phosphorus biological removal reactor 4 (SBR reactor) to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the pH of the nitrogen and phosphorus biological removal reactor 4 is 7.0;
  • the dispenser 10 adds a part of the precipitate (0.5% by mass of the precipitate) to the nitrogen-phosphorus biological removal reactor 4 and mixes it with the mixed liquid phase before the denitrification and dephosphorization treatment, and then proceeds
  • the above-mentioned nitrogen and phosphorus removal treatment simultaneously adds the remainder of the precipitate to the anaerobic fermentation reactor 1 and mixes it with the organic wastewater before the anaerobic fermentation, and then carries out the above anaerobic fermentation process.
  • the BOD removal rate of the purified water obtained in this example was 98.8%, the total nitrogen (TN) removal rate was 83.6%, and the phosphate removal rate was 92.2%.
  • the embodiment provides a method for treating organic wastewater, which comprises the following steps:
  • the organic wastewater (dairy wastewater) enters the first conditioning tank 5, and the first conditioning tank 5 uniformly adjusts the water quantity and water quality of the organic wastewater;
  • the BOD of the dairy wastewater is 2240 mg/L, and the total nitrogen is 111.6 mg/ L, ammonia nitrogen is 105 mg / L, total phosphate is 28.3 mg / L;
  • the anaerobic fermentation reactor 1 performs anaerobic fermentation on the effluent of the first conditioning tank 5 (homogeneous organic wastewater) to obtain a fermentation broth; the pH of the anaerobic fermentation system may be 9.5, the fermentation time (hydraulic force) The residence time, HRT) was 24 days; the obtained fermentation broth had a propionic acid content of 78% and an acetic acid content of 22%.
  • the aeration tank 2 performs a nitrification reaction on a part of the fermentation liquid (volume V 1 ') to obtain a fermentation liquid containing nitrate nitrogen; and the remainder of the fermentation liquid separation device 6 on the fermentation liquid (volume is V 2 ) ') separating, removing the residue, obtaining a liquid as a fermentation liquid containing propionic acid, and temporarily storing the propionic acid-containing fermentation liquid in the fermentation liquid storage tank 7;
  • the second adjusting tank 8 adjusts the water quantity and the water quality of the mixed liquid uniformly
  • the sedimentation tank 9 precipitates the effluent of the nitrogen-phosphorus biological removal reactor 4 (SBR reactor) to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the pH of the nitrogen and phosphorus biological removal reactor 4 is 8.0;
  • the dispenser 10 adds a part of the precipitate (50% of the mass of the precipitate) to the nitrogen-phosphorus biological removal reactor 4 and mixes it with the mixed liquid phase before the denitrification and dephosphorization treatment, and then proceeds
  • the above-mentioned nitrogen and phosphorus removal treatment simultaneously adds the remainder of the precipitate to the anaerobic fermentation reactor 1 and mixes it with the organic wastewater before the anaerobic fermentation, and then carries out the above anaerobic fermentation process.
  • the BOD removal rate of the purified water obtained in the present example was 99.8%, the total nitrogen (TN) removal rate was 86.6%, and the phosphate removal rate was 98.2%.
  • the embodiment provides a method for treating organic wastewater, which comprises the following steps:
  • the organic wastewater (dairy wastewater) enters the first conditioning tank 5, and the first conditioning tank 5 uniformly adjusts the water quantity and water quality of the organic wastewater;
  • the BOD of the dairy wastewater is 2240 mg/L, and the total nitrogen is 111.6 mg/ L, ammonia nitrogen is 105 mg / L, total phosphate is 28.3 mg / L;
  • the anaerobic fermentation reactor 1 performs anaerobic fermentation on the effluent of the first conditioning tank 5 (homogeneous organic wastewater) to obtain a fermentation broth; the pH of the anaerobic fermentation system may be 9, and the fermentation time (hydrodynamic force) The residence time, HRT) is 12 days; the obtained fermentation broth has a propionic acid content of 81% and an acetic acid content of 19%;
  • the aeration tank 2 performs a nitrification reaction on a part of the fermentation liquid (volume V 1 ') to obtain a fermentation liquid containing nitrate nitrogen; and the remainder of the fermentation liquid separation device 6 on the fermentation liquid (volume is V 2 ) ') separating, removing the residue, obtaining a liquid as a fermentation liquid containing propionic acid, and temporarily storing the propionic acid-containing fermentation liquid in the fermentation liquid storage tank 7;
  • the second adjusting tank 8 adjusts the water quantity and the water quality of the mixed liquid uniformly
  • the sedimentation tank 9 precipitates the effluent of the nitrogen-phosphorus biological removal reactor 4 (SBR reactor) to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the pH of the nitrogen and phosphorus biological removal reactor 4 is 7.5;
  • the dispenser 10 adds a part of the precipitate (10% of the mass of the precipitate) to the nitrogen-phosphorus biological removal reactor 4 and mixes it with the mixed liquid phase before the denitrification and dephosphorization treatment, and then proceeds The above-mentioned nitrogen and phosphorus removal treatment, while adding the remainder of the precipitate to the anaerobic fermentation reactor 1 and mixing it with the organic wastewater before the anaerobic fermentation, and then The above anaerobic fermentation process is carried out.
  • the BOD removal rate of the purified water obtained in the present example was 99.9%, the total nitrogen (TN) removal rate was 91.8%, and the phosphate removal rate was 99.1% with respect to the organic wastewater.
  • the anaerobic fermentation reactor 1 performs anaerobic fermentation on the effluent of the first conditioning tank 5 (homogeneous organic wastewater) to obtain a fermentation broth;
  • the pH of the anaerobic fermentation system may be 9, and the fermentation time (hydrodynamic force)
  • the residence time, HRT) is 12 days;
  • the obtained fermentation broth has a propionic acid content of 80% and an acetic acid content of 20%;
  • the second adjusting tank 8 adjusts the water quantity and the water quality of the mixed liquid uniformly
  • the sedimentation tank 9 precipitates the effluent of the nitrogen-phosphorus biological removal reactor 4 (A2O reactor) to obtain a supernatant and a precipitate, and the supernatant is discharged as purified water.
  • the pH of the nitrogen and phosphorus biological removal reactor 4 is 7.5;
  • the BOD removal rate of the purified water obtained in the present example was 99.9%, the total nitrogen (TN) removal rate was 94.8%, and the phosphate removal rate was 99.6% with respect to the organic wastewater.
  • the embodiment provides a method for treating organic wastewater, which comprises the following steps:
  • the organic wastewater enters the first conditioning tank 5, and the first regulating tank 5 adjusts the water quantity and the water quality of the organic wastewater uniformly;
  • the BOD of the food processing wastewater is 2900 mg/L, and the total nitrogen is 120 mg/ L, ammonia nitrogen is 106 mg / L, total phosphate is 20 mg / L;
  • the anaerobic fermentation reactor 1 performs anaerobic fermentation on the effluent of the first conditioning tank 5 (homogeneous organic wastewater) to obtain a fermentation broth;
  • the pH of the anaerobic fermentation system may be 8, and the fermentation time (hydrodynamic force)
  • the residence time, HRT) is 8 days;
  • the obtained fermentation broth has a propionic acid content of 84% and an acetic acid content of 16%;
  • the aeration tank 2 performs a nitrification reaction on a part of the fermentation liquid (volume V 1 ') to obtain a fermentation liquid containing nitrate nitrogen; and the remainder of the fermentation liquid separation device 6 on the fermentation liquid (volume is V 2 ) ') separating, removing the residue, obtaining a liquid as a fermentation liquid containing propionic acid, and temporarily storing the propionic acid-containing fermentation liquid in the fermentation liquid storage tank 7;
  • the second adjusting tank 8 adjusts the water quantity and the water quality of the mixed liquid uniformly
  • the BOD removal rate of the purified water obtained in the present example was 99.9%, the total nitrogen (TN) removal rate was 97.8%, and the phosphate removal rate was 99.8% with respect to the organic wastewater.

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Abstract

一种有机废水的处理方法，其包括：对有机废水进行厌氧发酵，得到发酵液；将一部分发酵液进行硝化反应，得到含硝态氮的发酵液；将剩余的发酵液进行分离，去除残渣后得到含丙酸的发酵液；将两种发酵液混合后进行脱氮除磷处理和沉淀，得到的上清液即为净化水。还公开了一种有机废水处理系统，其包括：厌氧发酵反应器（1）、曝气池（2）、发酵液分离设备（3）、氮磷生物去除反应器（4）和沉淀池（9）。

Description

有机废水的处理方法以及有机废水处理系统 技术领域
本发明属于废水处理技术领域，涉及一种有机废水的处理方法以及有机废水处理系统。
背景技术
有机废水中通常含有碳、氮、磷等污染物，碳污染物一般以COD表示，氮污染物多指硝态氮，磷污染物一般指溶解性磷酸盐，必须将这些污染物除去并且达到排放标准后才能排放。传统的厌氧消化技术主要是将有机物转化为甲烷，并且在对氮和磷进行去除时还需要外加碳源。
发明内容
本发明针对现有技术的不足，主要目的在于提供一种有机废水的处理方法。
本发明的另一个目的在于提供一种能够实现上述的有机废水的处理方法的有机废水处理系统。
为达到上述目的，本发明的解决方案是：
<有机废水的处理方法>
一种有机废水的处理方法，其包括如下步骤：
(1)、对有机废水进行厌氧发酵，得到发酵液；
(2)、将发酵液中的一部分进行硝化反应，得到含硝态氮的发酵液；将发酵液的剩余部分进行分离，去除残渣以得到含丙酸的发酵液；
(3)、将含硝态氮的发酵液和含丙酸的发酵液混合，得到混合液；
(4)、对混合液进行脱氮除磷处理后进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。
其中，在步骤(1)中，有机废水可以为含蛋白质的废水，厌氧发酵的pH值可以为9±0.5，优选为9，厌氧发酵的时间可以为1小时至24天，优选为12天。有机废水在进行厌氧发酵前需要接种厌氧发酵微生物，其来自于蛋白质加工厂在排放含蛋白质的废水时产生的废弃污泥。废弃污泥的接种量为有机废水体积的5±1％。
在步骤(1)中，有机废水可以为含碳水化合物的废水，厌氧发酵的pH值为8±0.5，优 选为8，厌氧发酵的时间可以为0.5小时至16天，优选为8天。有机废水在进行厌氧发酵前需要接种厌氧发酵微生物，其来自于碳水化合物加工厂在排放含碳水化合物的废水时产生的废弃污泥。废弃污泥的接种量为有机废水体积的3.8±1％。
步骤(1)中的发酵液可以含有70wt％以上的丙酸并且含有30wt％以下的乙酸。
在步骤(2)中，含硝态氮的发酵液和含丙酸的发酵液的混合比例使混合液的总氮和总磷之和与生物需氧量的比例为1:(8‐15)，优选为1:11。
在步骤(4)中，脱氮除磷处理的pH值为7.5±0.5，优选为7.5。
步骤(4)中的混合液在进行脱氮除磷处理前与沉淀物中的一部分相混合，步骤(1)中的有机废水在进行厌氧发酵前与沉淀物的剩余部分相混合。沉淀物中的一部分可以占沉淀物总量的0.5‐50wt％。
<有机废水处理系统>
一种实现上述的有机废水的处理方法的有机废水处理系统，其包括：
厌氧发酵反应器，对有机废水进行厌氧发酵以得到发酵液；
曝气池，对发酵液中的一部分进行硝化反应，得到含硝态氮的发酵液；
发酵液分离设备，对发酵液的剩余部分进行分离，去除残渣后得到含丙酸的发酵液；
氮磷生物去除反应器，对由含硝态氮的发酵液和含丙酸的发酵液混合而得到混合液进行脱氮除磷处理；
沉淀池，对氮磷生物去除器的排出物进行沉淀，得到上清液和沉淀物。
其中，有机废水处理系统还可以包括：分配器，其将沉淀物的一部分加入氮磷生物去除反应器中并使其与进行脱氮除磷处理前的混合液相混合，将沉淀物的剩余部分加入厌氧发酵反应器中并使其与进行厌氧发酵前的有机废水相混合。沉淀物中的一部分可以占沉淀物总量的0.5‐50wt％。
当有机废水为含蛋白质的废水时，厌氧发酵反应器在厌氧发酵时的pH值可以为9±0.5，优选为9，厌氧发酵的时间为1小时至24天，优选为12天。有机废水在进行厌氧发酵前需要接种厌氧发酵微生物，其来自于蛋白质加工厂在排放含蛋白质的废水时产生的废弃污泥。废弃污泥的接种量为有机废水体积的5±1％。
当有机废水为含碳水化合物的废水时，厌氧发酵反应器在厌氧发酵时的pH值可以为8±0.5，优选为8，厌氧发酵的时间为0.5小时至16天，优选为8天。有机废水在进行厌氧发酵前需要接种厌氧发酵微生物，其来自于碳水化合物加工厂在排放含碳水化合物的废水时产生的废弃污泥。废弃污泥的接种量为有机废水体积的3.8±1％。
厌氧发酵反应器所排出的发酵液含有70wt％以上的丙酸并且含有30wt％以下的乙酸。
含硝态氮的发酵液和含丙酸的发酵液的混合比例使混合液的总氮和总磷之和与生物需氧量的比例为1:(8‐15)，优选为1:11。
氮磷生物去除反应器在脱氮除磷处理时的pH值为7.5±0.5，优选为7.5。
由于采用上述方案，本发明的有益效果是：
第一、本发明通过控制有机废水厌氧发酵的条件得到了含有大量短链脂肪酸(如丙酸)的发酵液，然后将该发酵液分为两部分，其中一部分进行硝化反应以便将氨态氮转化为容易被后继的脱氮除磷微生物利用的硝态氮，另一部分则与硝化反应所得到的发酵液混合，在对所得到的混合液进行脱氮除磷处理时，脱氮除磷体系已经含有了足够的碳源(短链脂肪酸)，因此，本发明无需额外补充碳源、氮源和磷源即可实现对碳、氮和磷的含量平衡的优化，有利于脱氮除磷微生物对碳、氮和磷的同时并且高效地去除。
第二、本发明通过控制有机废水厌氧发酵的条件使有机废水定向转化为短链脂肪酸，而不是转化为甲烷，不仅能充分利用碳源，而且还能减少温室气体的排放。
第三、本发明将所得的部分沉淀物(污泥)与有机废水混合后置于厌氧发酵反应器中进行厌氧发酵，不仅能够促进短链脂肪酸的产生，而且还能够实现对污泥的资源化利用，减少了污泥的产生量。
附图说明
图1为本发明的有机废水处理系统的第一幅示意图。
图2为本发明的有机废水处理系统的第二幅示意图。
附图标记
厌氧发酵反应器1、曝气池2、发酵液分离设备3、氮磷生物去除反应器4、第一调节池5、发酵液分离装置6、发酵液储存池7、第二调节池8、沉淀池9和分配器10。
具体实施方式
本发明提供了一种有机废水的处理方法和有机废水处理系统。
<有机废水的处理方法>
本发明提供了一种有机废水的处理方法，其包括如下步骤：
(1)、对有机废水进行厌氧发酵，得到发酵液；
(2)、将发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；将发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液；
(3)、将含硝态氮的发酵液和含丙酸的发酵液混合，得到混合液；
(4)、对混合液进行脱氮除磷处理后进行沉淀，得到上清液和沉淀物，上清液作为净化 水排放。
其中，在步骤(1)中，有机废水可以为含蛋白质的废水，该含蛋白质的废水优选为乳品废水、食品加工废水。乳品废水是炼乳、干酪、奶油、乳制清凉饮料、冰激凌以及乳制品点心在生产过程中排出的废水，主要来自容器及设备的清洗水，其中含有乳品原料。
当有机废水为含蛋白质的废水时，厌氧发酵体系的pH值可以为9±0.5，优选为9；厌氧发酵的时间可以为1小时至24天，优选为12天。厌氧发酵时的平均温度为28℃。厌氧发酵之前需要接种乳品加工厂在排放处乳品废水时产生的废弃污泥(呈灰黑色，含有厌氧发酵微生物，VSS/TSS的平均值为0.78)，接种量为起始有机废水体积的5％。
在步骤(1)中，有机废水可以为含碳水化合物的废水，该含碳水化合物的废水可以优选为啤酒废水。啤酒废水是指啤酒生产过程中排出的废水，其包括原料清洗所产生的废水和啤酒酿造过程中产生的废水。
当有机废水为含碳水化合物的废水时，厌氧发酵体系的pH值可以为8±0.5，优选为8；厌氧发酵的时间可以为0.5小时至16天，优选为8天。厌氧发酵的温度为23℃。厌氧发酵之前需接种酒精生产厂在排放酒精废水在时产生的废弃污泥(呈黄黑色，含有厌氧发酵微生物，VSS/TSS平均值为0.86)，接种量为起始有机废水体积的3.8％。
步骤(1)中的有机废水的BOD可以为2240‐3100mg/L、总氮可以为90‐120mg/L、氨氮可以为85‐106mg/L、总磷酸盐可以为20‐28.3mg/L。
步骤(1)所得的发酵液含有70wt％以上的丙酸。
在步骤(2)中，将步骤(1)所得的发酵液分为两部分(体积分别为V1'和V2')。将其中一部分(体积为V1')进行硝化反应，使氨态氮转化为硝态氮，使碳转化为二氧化碳，从而得到含硝态氮的发酵液；将剩余部分(体积为V2')进行分离，去除残渣，保留液体即得到含丙酸的发酵液。
在步骤(2)中，进行硝化反应时，需要接种垃圾处理厂在处理垃圾渗滤液时产生的废弃污泥(呈黄黑色，含有硝化微生物，VSS/TSS平均值为0.71)，接种量为欲进行硝化反应的发酵液(体积为V1')体积的3％；硝化反应的温度为24℃。
在步骤(3)中，含硝态氮的发酵液和含丙酸的发酵液的混合比例应使混合液的总氮和总磷的浓度之和与其生物需氧量(BOD)的比例为1:(8‐15)，优选为1:11。通过控制该比例为1:(8‐15)，一方面能够满足脱氮除磷时微生物生长和代谢需要的碳源量，另一方面可以确保处理后的废水不会发生大量碳源过量从而引起二次污染。总氮浓度的测定采用过硫酸钾氧化法，总磷浓度的测定采用钼酸铵分光光度法，生物需氧量的测定采用微生物传感器法。
在步骤(3)中，含硝态氮的发酵液和含丙酸的发酵液的混合比例为：含硝态氮的发酵液 占混合液的体积比可以为6.25‐60.25％，含丙酸的发酵液占混合液的体积比可以为39.75‐93.75％。
在步骤(4)中，对混合液脱氮除磷处理的条件为：脱氮除磷体系的pH值可以为7.5±0.5，优选为7.5；在脱氮除磷处理前需要接种城市污水处理厂产生的废弃污泥，呈淡黄色，含有脱氮除磷微生物，VSS/TSS平均值为0.65；接种量为混合液体积的8％；反应温度为22℃。
在步骤(4)中，对混合液进行脱氮除磷处理后继续沉淀，得到上清液和沉淀物。上清液即为净化后的水，可以直接排放或使用。沉淀物为污泥。可以将污泥分为两部分，一部分污泥(占污泥总量的0.5‐50wt％)与进行脱氮除磷处理前的混合液相混合，随后再进行脱氮除磷处理；剩余部分的污泥与在进行厌氧发酵前的有机废水相混合，随后再进行厌氧发酵。
总之，本发明通过控制两种发酵液的混合比例来实现脱氮除磷处理过程中的碳、氮和磷的平衡，无需额外补充碳源即可实现对碳、氮和磷的高效同步去除。
<有机废水处理系统>
如图1所示，本发明提供了一种实现上述的有机废水的处理方法的有机废水处理系统，其包括：厌氧发酵反应器1、曝气池2、发酵液分离设备3、氮磷生物去除反应器4和沉淀池9。
其中，厌氧发酵反应器1用于对有机废水进行厌氧发酵以得到发酵液，该发酵液含有70wt％以上的丙酸。
有机废水可以为含蛋白质的废水，该含蛋白质的废水指的是废水中蛋白质含量高于其它非蛋白质类有机物的废水，优选为乳品废水、食品加工废水。乳品废水是炼乳、干酪、奶油、乳制清凉饮料、冰激凌以及乳制品点心在生产过程中排出的废水，主要来自容器及设备的清洗水，其中含有乳品原料。食品加工废水指的是食品(如蛋糕、面包等)在加工过程中产生的废水。在对含蛋白的废水进行厌氧发酵时，厌氧发酵体系的pH值可以为9±0.5，优选为9，厌氧发酵的时间可以为1小时至24天，优选为12天。
有机废水可以为含碳水化合物的废水，该含碳水化合物的废水指的是废水中碳水化合物的含量高于其它非碳水化合物类物质的含量，可以优选为啤酒废水。啤酒废水是指啤酒生产过程中排出的废水，其包括原料清洗所产生的废水和啤酒酿造过程中产生的废水。在对含碳水化合物的废水进行厌氧发酵时，厌氧发酵体系的pH值可以为8±0.5，优选为8，厌氧发酵的时间可以为0.5小时至16天，优选为8天。
曝气池2用于对发酵液中的一部分(体积为V1')进行硝化反应，使氨态氮转化为硝态氮，同时碳(以COD表示)转化为二氧化碳，从而得到含硝态氮的发酵液。进入曝气池2的发酵液含有短链脂肪酸(如丙酸等)、氨氮和磷酸盐等，曝气池2排出的液体含有短链脂肪酸(如丙酸等)、硝态氮或亚硝态氮、磷酸盐等。
发酵液分离设备3包括发酵液分离装置6和发酵液储存池7。发酵液分离装置6用于对发酵液的剩余部分(体积为V2')进行分离，去除残渣，仅保留液体以得到含丙酸的发酵液。发酵液储存池7用于储存该含丙酸的发酵液。
氮磷生物去除反应器4用于对由含硝态氮的发酵液和含丙酸的发酵液混合而得到混合液进行脱氮除磷处理。含硝态氮的发酵液和含丙酸的发酵液的混合比例应使混合液的总氮和总磷的浓度之和与其生物需氧量(BOD)的比例为1:(8‐15)，优选为1:11。对混合液脱氮除磷处理的条件为：脱氮除磷体系的pH值可以为7.5±0.5，优选为7.5。
氮磷生物去除反应器4同时去除混合液中的碳、氮和磷的原理如下：
因为混合液中含有大量的短链脂肪酸(如丙酸、乙酸等)，所以氮磷生物去除反应器4中存活的脱氮除磷微生物在厌氧发酵条件下可以将其转化为胞内碳源，相当于降低了混合液中的短链脂肪酸的含量，起到除碳的效果；然后，脱氮除磷微生物因为获得了足够的胞内碳源，所以在缺氧或好氧的发酵条件下分解该胞内碳源并利用胞内碳源分解所产生的能量和还原力进行磷的吸收和脱氮反应，从而实现对混合液中碳源、氮源和磷源的同时去除。因为本发明的脱氮除磷微生物在除磷脱氮时有足够的碳源可以利用，所以无需添加额外的碳源也能实现对氮源和磷源的同时去除。
沉淀池9实际上起到二沉池(secondary settling tank)的作用，其用于对氮磷生物去除器的排出物进行沉淀，得到上清液和沉淀物。上清液即为净化后的水，可以直接排放或使用。沉淀物为污泥。可以将污泥分为两部分，一部分污泥(占污泥总量的0.5‐50wt％)与进行脱氮除磷处理前的混合液相混合，剩余部分的污泥与在进行厌氧发酵前的有机废水相混合。
上述的有机废水处理系统对有机废水的处理过程包括如下步骤：
(1)、厌氧发酵反应器1对有机废水进行厌氧发酵，得到发酵液；
(2)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(3)、将含硝态氮的发酵液(体积为V1)和含丙酸的发酵液(体积为V2)混合，得到混合液；
(4)、氮磷生物去除反应器4对混合液进行脱氮除磷处理；
(5)、沉淀池9对氮磷生物去除反应器4的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。
如图2所示，根据实际情况，有机废水处理系统还可以增设：第一调节池5、第二调节池8、分配器10。
第一调节池5用于将有机废水的水量和水质调节均匀，之后匀质的有机废水进入厌氧发酵反应器1中。因为有机废水的流量或性质常常发生波动，所以需要设置第一调节池5，以便对有机废水的流量或性质进行调节，使其稳定化，防止有机废水的流量或性质的剧变对后继的各个处理过程造成较大的影响。
第二调节池8用于将混合液的水量和水质调节均匀，之后匀质的混合液进入氮磷生物去除反应器4中。
分配器10用于将沉淀物的一部分加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行脱氮除磷处理；分配器10还用于将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后再进行厌氧发酵过程。
上述的有机废水处理系统对有机废水的处理过程包括如下步骤：
(1)、第一调节池5将有机废水的水量和水质调节均匀；
(2)、厌氧发酵反应器1对第一调节池5排出的匀质的有机废水进行厌氧发酵，得到发酵液；
(3)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(4)、将含硝态氮的发酵液(体积为V1)和含丙酸的发酵液(体积为V2)混合，得到混合液；
(5)、第二调节池8将混合液的水量和水质调节均匀；
(6)、氮磷生物去除反应器4对匀质的混合液进行脱氮除磷处理；
(7)、沉淀池9对氮磷生物去除反应器4的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。
(8)、分配器10将沉淀物的一部分加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行上述的脱氮除磷处理，同时将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后再进行上述的厌氧发酵过程。
以下结合实施例对本发明作进一步的说明。
实施例一
本实施例提供了一种有机废水的处理方法，其包括如下步骤：
(1)、有机废水(乳品废水)进入第一调节池5中，该第一调节池5将有机废水的水量和水质调节均匀；该乳品废水的BOD为2240mg/L、总氮为111.6mg/L、氨氮为105mg/L、总 磷酸盐为28.3mg/L；
(2)、厌氧发酵反应器1对第一调节池5的出水(匀质的有机废水)进行厌氧发酵，得到发酵液；厌氧发酵体系的pH值可以为8.5，发酵的时间(水力停留时间，HRT)为1小时；所得到的发酵液的丙酸含量为74％，乙酸含量为25％。
(3)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(4)、将含硝态氮的发酵液(体积为V1)和含丙酸的发酵液(体积为V2)以1:1的体积比进行混合，得到混合液；
(5)、第二调节池8将混合液的水量和水质调节均匀；
(6)、氮磷生物去除反应器4对匀质的混合液进行脱氮除磷处理；
(7)、沉淀池9对氮磷生物去除反应器4(SBR反应器)的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。氮磷生物去除反应器4的pH值为7.0；
(8)、分配器10将沉淀物的一部分(占沉淀物质量的0.5％)加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行上述的脱氮除磷处理，同时将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后再进行上述的厌氧发酵过程。
经过检测得知，相对于有机废水而言，本实施例所得的净化水的BOD去除率为98.8％，总氮(TN)去除率为83.6％，磷酸盐的去除率为92.2％。
实施例二
本实施例提供了一种有机废水的处理方法，其包括如下步骤：
(1)、有机废水(乳品废水)进入第一调节池5中，该第一调节池5将有机废水的水量和水质调节均匀；该乳品废水的BOD为2240mg/L、总氮为111.6mg/L、氨氮为105mg/L、总磷酸盐为28.3mg/L；
(2)、厌氧发酵反应器1对第一调节池5的出水(匀质的有机废水)进行厌氧发酵，得到发酵液；厌氧发酵体系的pH值可以为9.5，发酵的时间(水力停留时间，HRT)为24天；所得到的发酵液的丙酸含量为78％，乙酸含量为22％。
(3)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(4)、将含硝态氮的发酵液和含丙酸的发酵液进行混合得到混合液；含硝态氮的发酵液 的体积占混合液体积的6.25％，含丙酸的发酵液的体积占混合液体积的93.75％；
(5)、第二调节池8将混合液的水量和水质调节均匀；
(6)、氮磷生物去除反应器4对匀质的混合液进行脱氮除磷处理；
(7)、沉淀池9对氮磷生物去除反应器4(SBR反应器)的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。氮磷生物去除反应器4的pH值为8.0；
(8)、分配器10将沉淀物的一部分(占沉淀物质量的50％)加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行上述的脱氮除磷处理，同时将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后再进行上述的厌氧发酵过程。
经过检测得知，相对于有机废水而言，本实施例所得的净化水的BOD去除率为99.8％，总氮(TN)去除率为86.6％，磷酸盐的去除率为98.2％。
实施例三
本实施例提供了一种有机废水的处理方法，其包括如下步骤：
(1)、有机废水(乳品废水)进入第一调节池5中，该第一调节池5将有机废水的水量和水质调节均匀；该乳品废水的BOD为2240mg/L、总氮为111.6mg/L、氨氮为105mg/L、总磷酸盐为28.3mg/L；
(2)、厌氧发酵反应器1对第一调节池5的出水(匀质的有机废水)进行厌氧发酵，得到发酵液；厌氧发酵体系的pH值可以为9，发酵的时间(水力停留时间，HRT)为12天；所得到的发酵液的丙酸含量为81％，乙酸含量为19％；
(3)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(4)、将含硝态氮的发酵液和含丙酸的发酵液进行混合得到混合液；含硝态氮的发酵液的体积占混合液体积的31.25％，含丙酸的发酵液的体积占混合液体积的68.75％；
(5)、第二调节池8将混合液的水量和水质调节均匀；
(6)、氮磷生物去除反应器4对匀质的混合液进行脱氮除磷处理；
(7)、沉淀池9对氮磷生物去除反应器4(SBR反应器)的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。氮磷生物去除反应器4的pH值为7.5；
(8)、分配器10将沉淀物的一部分(占沉淀物质量的10％)加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行上述的脱氮除磷处理，同时将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后 再进行上述的厌氧发酵过程。
经过检测得知，相对于有机废水而言，本实施例所得的净化水的BOD去除率为99.9％，总氮(TN)去除率为91.8％，磷酸盐的去除率为99.1％。
实施例四
本实施例提供了一种有机废水的处理方法，其包括如下步骤：
(1)、有机废水(食品加工废水)进入第一调节池5中，该第一调节池5将有机废水的水量和水质调节均匀；该食品加工废水的BOD为3100mg/L、总氮为90mg/L、氨氮为85mg/L、总磷酸盐为22mg/L；
(2)、厌氧发酵反应器1对第一调节池5的出水(匀质的有机废水)进行厌氧发酵，得到发酵液；厌氧发酵体系的pH值可以为9，发酵的时间(水力停留时间，HRT)为12天；所得到的发酵液的丙酸含量为80％，乙酸含量为20％；
(3)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(4)、将含硝态氮的发酵液和含丙酸的发酵液进行混合得到混合液；含硝态氮的发酵液的体积占混合液体积的60.25％，含丙酸的发酵液的体积占混合液体积的39.75％；
(5)、第二调节池8将混合液的水量和水质调节均匀；
(6)、氮磷生物去除反应器4对匀质的混合液进行脱氮除磷处理；
(7)、沉淀池9对氮磷生物去除反应器4(A2O反应器)的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。氮磷生物去除反应器4的pH值为7.5；
(8)、分配器10将沉淀物的一部分(占沉淀物质量的10％)加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行上述的脱氮除磷处理，同时将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后再进行上述的厌氧发酵过程。
经过检测得知，相对于有机废水而言，本实施例所得的净化水的BOD去除率为99.9％，总氮(TN)去除率为94.8％，磷酸盐的去除率为99.6％。
实施例五
本实施例提供了一种有机废水的处理方法，其包括如下步骤：
(1)、有机废水(啤酒废水)进入第一调节池5中，该第一调节池5将有机废水的水量和水质调节均匀；该食品加工废水的BOD为2900mg/L、总氮为120mg/L、氨氮为106mg/L、总磷酸盐为20mg/L；
(2)、厌氧发酵反应器1对第一调节池5的出水(匀质的有机废水)进行厌氧发酵，得到发酵液；厌氧发酵体系的pH值可以为8，发酵的时间(水力停留时间，HRT)为8天；所得到的发酵液的丙酸含量为84％，乙酸含量为16％；
(3)、曝气池2对发酵液中的一部分(体积为V1')进行硝化反应，得到含硝态氮的发酵液；发酵液分离装置6对发酵液的剩余部分(体积为V2')进行分离，去除残渣，获取液体以作为含丙酸的发酵液，发酵液储存池7暂时存储该含丙酸的发酵液；
(4)、将含硝态氮的发酵液和含丙酸的发酵液进行混合得到混合液；含硝态氮的发酵液的体积占混合液体积的46.9％，含丙酸的发酵液的体积占混合液体积的53.1％；
(5)、第二调节池8将混合液的水量和水质调节均匀；
(6)、氮磷生物去除反应器4对匀质的混合液进行脱氮除磷处理；
(7)、沉淀池9对氮磷生物去除反应器4(A2O反应器)的排出物进行沉淀，得到上清液和沉淀物，上清液作为净化水排放。氮磷生物去除反应器4的pH值为7.5；
(8)、分配器10将沉淀物的一部分(占沉淀物质量的10％)加入氮磷生物去除反应器4中并使其与进行脱氮除磷处理前的混合液相混合，然后再进行上述的脱氮除磷处理，同时将沉淀物的剩余部分加入厌氧发酵反应器1中并使其与进行厌氧发酵前的有机废水相混合，然后再进行上述的厌氧发酵过程。
经过检测得知，相对于有机废水而言，本实施例所得的净化水的BOD去除率为99.9％，总氮(TN)去除率为97.8％，磷酸盐的去除率为99.8％。
上述的对实施例的描述是为便于该技术领域的普通技术人员能理解和使用本发明。熟悉本领域技术的人员显然可以容易地对这些实施例做出各种修改，并把在此说明的一般原理应用到其他实施例中而不必经过创造性的劳动。因此，本发明不限于上述实施例，本领域技术人员根据本发明的揭示，不脱离本发明范畴所做出的改进和修改都应该在本发明的保护范围之内。

Claims (9)

  1. 一种有机废水的处理方法，其特征在于：包括如下步骤：
    (1)、对有机废水进行厌氧发酵，得到发酵液；
    (2)、将所述发酵液中的一部分进行硝化反应，得到含硝态氮的发酵液；将所述发酵液的剩余部分进行分离，去除残渣以得到含丙酸的发酵液；
    (3)、将所述含硝态氮的发酵液和所述含丙酸的发酵液混合，得到混合液；
    (4)、对所述混合液进行脱氮除磷处理后进行沉淀，得到上清液和沉淀物，所述上清液作为净化水排放。
  2. 根据权利要求1所述的处理方法，其特征在于：在步骤(1)中，所述有机废水为含蛋白质的废水，所述厌氧发酵的pH值为9±0.5，所述厌氧发酵的时间为1小时至24天；和/或，
    在步骤(1)中，所述有机废水为含碳水化合物的废水，所述厌氧发酵的pH值为8±0.5，所述厌氧发酵的时间为0.5小时至16天；
    优选地，在步骤(1)中，所述有机废水为含蛋白质的废水，所述厌氧发酵的pH值为9，所述厌氧发酵的时间为12天；和/或，
    在步骤(1)中，所述有机废水为含碳水化合物的废水，所述厌氧发酵的pH值为8，所述厌氧发酵的时间为8天。
  3. 根据权利要求1所述的处理方法，其特征在于：步骤(1)中的发酵液含有70wt％以上的丙酸；和/或，
    在步骤(2)中，所述含硝态氮的发酵液和所述含丙酸的发酵液的混合比例使所述混合液的总氮和总磷之和与生物需氧量的比例为1:(8‐15)；和/或，
    在步骤(4)中，脱氮除磷处理的pH值为7.5±0.5；
    优选地，在步骤(2)中，所述含硝态氮的发酵液和所述含丙酸的发酵液的混合比例使所述混合液的总氮和总磷之和与生物需氧量的比例为1:11；和/或，
    在步骤(4)中，脱氮除磷处理的pH值为7.5。
  4. 根据权利要求1所述的处理方法，其特征在于：步骤(4)中的混合液在进行所述脱氮除磷处理前与所述沉淀物中的一部分相混合，步骤(1)中的有机废水在进行厌氧发酵前与所述沉淀物的剩余部分相混合；
    优选地，所述沉淀物中的一部分占所述沉淀物的0.5‐50wt％。
  5. 一种实现如权利要求1所述的有机废水的处理方法的有机废水处理系统，其特征在于： 包括：
    厌氧发酵反应器，对有机废水进行厌氧发酵以得到发酵液；
    曝气池，对所述发酵液中的一部分进行硝化反应，得到含硝态氮的发酵液；
    发酵液分离设备，对所述发酵液的剩余部分进行分离，去除残渣后得到含丙酸的发酵液；
    氮磷生物去除反应器，对由所述含硝态氮的发酵液和所述含丙酸的发酵液混合而得到混合液进行脱氮除磷处理；
    沉淀池，对所述氮磷生物去除器的排出物进行沉淀，得到上清液和沉淀物。
  6. 根据权利要求5所述的有机废水处理系统，其特征在于：包括：分配器，将所述沉淀物的一部分加入所述氮磷生物去除反应器中并使其与进行所述脱氮除磷处理前的混合液相混合，将所述沉淀物的剩余部分加入所述厌氧发酵反应器中并使其与进行厌氧发酵前的有机废水相混合。
  7. 根据权利要求6所述的有机废水处理系统，其特征在于：所述沉淀物中的一部分占所述沉淀物的0.5‐50wt％。
  8. 根据权利要求5所述的有机废水处理系统，其特征在于：当所述有机废水为含蛋白质的废水时，所述厌氧发酵反应器在厌氧发酵时的pH值为9±0.5，厌氧发酵的时间为1小时至24天；和/或，
    当所述有机废水为含碳水化合物的废水时，所述厌氧发酵反应器在厌氧发酵时的pH值为8±0.5，厌氧发酵的时间为0.5小时至16天；
    优选地，当所述有机废水为含蛋白质的废水时，所述厌氧发酵反应器在厌氧发酵时的pH值为9，厌氧发酵的时间为12天；和/或，
    当所述有机废水为含碳水化合物的废水时，所述厌氧发酵反应器在厌氧发酵时的pH值为8，厌氧发酵的时间为8天。
  9. 根据权利要求5所述的有机废水处理系统，其特征在于：所述发酵液含有70wt％以上的丙酸；和/或，
    所述含硝态氮的发酵液和所述含丙酸的发酵液的混合比例使所述混合液的总氮和总磷之和与生物需氧量的比例为1:(8‐15)；和/或，
    所述氮磷生物去除反应器在脱氮除磷处理时的pH值为7.5±0.5；
    优选地，所述含硝态氮的发酵液和所述含丙酸的发酵液的混合比例使所述混合液的总氮和总磷之和与生物需氧量的比例为1:11；和/或，
    所述氮磷生物去除反应器在脱氮除磷处理时的pH值为7.5。
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