WO2017161640A1 - 一种有机废水的处理回用方法和设备 - Google Patents

一种有机废水的处理回用方法和设备 Download PDF

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WO2017161640A1
WO2017161640A1 PCT/CN2016/080860 CN2016080860W WO2017161640A1 WO 2017161640 A1 WO2017161640 A1 WO 2017161640A1 CN 2016080860 W CN2016080860 W CN 2016080860W WO 2017161640 A1 WO2017161640 A1 WO 2017161640A1
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effluent
reaction
water
anaerobic ammonium
pump
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PCT/CN2016/080860
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English (en)
French (fr)
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霍守亮
张靖天
席北斗
张莉
马春子
何卓识
党秋玲
余红
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中国环境科学研究院
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Priority to US16/081,378 priority Critical patent/US10501355B2/en
Publication of WO2017161640A1 publication Critical patent/WO2017161640A1/zh

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    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
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    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
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    • C02F3/02—Aerobic processes
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    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
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    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the invention belongs to the field of industrial wastewater treatment, and in particular relates to a method for treating and recycling high-salt, high-ammonia nitrogen and high-concentration refractory organic wastewater.
  • the invention also relates to an apparatus for implementing the above method.
  • high-salt, high-ammonia nitrogen, high-concentration refractory organic wastewater mainly comes from synthetic pharmaceuticals, pesticide production, papermaking black liquor, tannery wastewater, monosodium glutamate production, petroleum refining, coal chemical and other industries.
  • refractory organic substances mainly include: polycyclic aromatic hydrocarbons, heterocyclic compounds, chlorinated aromatic compounds, organic cyanides, organic synthetic polymer compounds, and the like. The degradation mechanism of these compounds is to change their molecular structure through oxidation, reduction, co-metabolism and other mechanisms, and gradually transform into small molecules.
  • wet catalytic oxidation, supercritical oxidation, Fenton treatment, ozone oxidation and other techniques can be used to treat refractory organic matter, but in the case of high ammonia nitrogen concentration, it is difficult to achieve nitrogen removal by conventional anaerobic or aerobic processes. Claim.
  • due to the high concentration of organic matter when multi-effect evaporation or reverse osmosis treatment is used, it is easy to cause clogging of the evaporator or fouling of the membrane, resulting in difficulty in cleaning and an increase in processing cost.
  • Fenton technology is a commonly used advanced oxidation technology, which is often used to treat high concentration refractory organic wastewater, such as dye wastewater, phenol-containing wastewater, acrylonitrile wastewater, papermaking black liquor, landfill leachate, etc. But whether it is standard Fenton reagent or modified Fenton reagent, it is required to be at pH Only between 3-5 can play a normal role.
  • the non-homogeneous Fenton technology can produce more HO ⁇ by loading the iron catalyst onto the substrate even under the neutral pH condition, thus avoiding the alkalinity adjustment of the pH before the subsequent biological treatment, resulting in too high salinity.
  • the problem After the COD is lowered, the denitrification treatment needs to supplement the carbon source, resulting in an increase in cost.
  • the anaerobic ammonium oxidation technology can denitrify with nitrate or nitrite as an electron acceptor, which can effectively solve this problem.
  • the object of the present invention is to provide a method for treating and recycling high-salt, high-ammonia nitrogen and high-concentration refractory organic wastewater.
  • the present invention combines a heterogeneous Fenton method, an anaerobic ammonium oxidation process and a membrane treatment method to treat high-salt, high-ammonia nitrogen, high-concentration refractory organic wastewater.
  • the method for treating and recycling high-salt, high-ammonia nitrogen, high-concentration refractory organic wastewater is as follows:
  • step 2 The effluent after the pretreatment in step 1 is subjected to heterogeneous Fenton reaction, and the nano-Fe 3 O 4 supported by Hangjin soil is used as a catalyst. After the reaction is completed, the catalyst is separated from the reaction liquid, and the reaction liquid is subjected to denitrification and COD reaction;
  • step 3 The effluent of step 2 is subjected to anaerobic ammonium oxidation reaction, so that ammonia nitrogen reacts with nitrite nitrogen to denitrify; 4) the effluent of step 3 is further separated by aerobic microorganism decomposition and ultrafiltration membrane to further remove COD and ammonia nitrogen;
  • step 4 The effluent of step 4 is filtered to remove large particle size particles
  • step 5 The effluent from step 5 enters the RO system, the effluent of the RO system is used as circulating cooling water, and the concentrated water of the RO system is softened;
  • step 6 The concentrated water after the softening in step 6 enters the NF system, and the treated effluent is evaporated to recover NaCl, and the produced concentrated water is returned to the step 1.
  • the treatment recycling method wherein the organic wastewater of step 1 has a salinity of 3%-10%, an ammonia nitrogen concentration of 1000-2500 mg/L, a COD concentration of 2000-5000 mg/L, and a flocculating agent is polyacrylamide.
  • the treatment is reused, wherein the pH of the heterogeneous Fenton reaction in step 2 is between 6.5 and 7.5; the nano-Fe 3 O 4 particles in the catalyst are uniformly distributed in the monodisperse form on the surface and the pores of the Hangjin soil.
  • the catalyst is concentrated at the bottom of the heterogeneous Fenton device by means of an external magnetic field to separate the catalyst from the reaction liquid.
  • the treatment recycling method wherein the softener used in the softening of the concentrated water in the step 5 is Na 2 CO 3 .
  • step 6 The process recycling method, wherein the effluent in step 6 is processed by a multi-effect evaporator to produce industrial NaCl.
  • the device provided by the present invention for implementing the above processing reuse method :
  • Adjusting the sedimentation tank connecting the dosing tank, adjusting the sedimentation tank to be equipped with a stirrer, adjusting the sedimentation tank with the inlet of the raw water and the sediment discharge outlet, and adjusting the sedimentation tank to be connected to the storage tank through the pump and the flow meter;
  • the water storage tank is connected by a pump, a flow meter and a heterogeneous Fenton device.
  • the heterogeneous Fenton device is connected with a dosing tank.
  • the heterogeneous Fenton device is equipped with a stirrer.
  • the bottom of the heterogeneous Fenton device is equipped with an electromagnetic field.
  • the homogeneous Fenton device is connected to the anaerobic ammonium oxidation device by a pump;
  • the anaerobic ammonia oxidation unit is connected to the submerged MBR system through a pump.
  • the outlet of the submerged MBR system is connected to the security filter through the pump.
  • the outlet of the security filter is connected to the RO system.
  • the RO water is treated as the circulating cooling water after treatment.
  • the concentrated water outlet of the system is connected to the integrated softening and coagulation sedimentation system.
  • the integrated coagulation and sedimentation system is connected to the medicine tank through the flow meter and the pump.
  • the outlet of the integrated softening and coagulation sedimentation system is connected to the NF system, and the effluent after the NF system treatment. Connect the multi-effect evaporator, the concentrated water outlet of the NF system is returned to the adjustment sedimentation tank by the pump and flow meter.
  • the device wherein the anaerobic ammonia oxidation device is a container with a fully enclosed structure, the side wall is provided with a plurality of sampling ports, the top portion is provided with an exhaust port, the upper portion is provided with a water outlet and a water outlet for circulating cooling water, and the lower portion is provided There is a water inlet of circulating cooling water, a water inlet is arranged at the bottom, an aeration head is arranged above the water inlet, and the stirring paddle is arranged above the aeration head;
  • the anaerobic ammonium oxidation device is filled with anaerobic ammonium oxide granular sludge, the outer layer of the granular sludge is an aerobic layer, and the inner layer is an anaerobic layer, which can realize the whole process of autotrophic denitrification in the anaerobic ammonium oxidation device;
  • the anaerobic ammonium oxidation device is provided with a graphite counter electrode, a carbon felt working electrode and a reference electrode, and the graphite counter electrode, the carbon felt working electrode and the reference electrode are connected to the potentiostat;
  • the pH on-line controller provided in the anaerobic ammonium oxidation unit is used to monitor the change of the pH value in the device in real time, and adjust the pH value in the anaerobic ammonium oxidation device by adding HCl and NaHCO 3 .
  • the aeration head is denitrified by contact with the anaerobic ammonium oxide granular sludge through the perforated baffle provided above.
  • a sponge filler is disposed between the granular sludge and the water outlet.
  • the device wherein the pump is a centrifugal pump, and the agitating slurry is a mechanical agitating slurry.
  • the invention can realize the treatment and recycling of high-salt, high-ammonia nitrogen and high-concentration refractory organic wastewater, and has the characteristics of wide application range, high pollutant degradation efficiency and easy salt recovery and utilization.
  • Figure 1 is a schematic flow chart of the present invention.
  • Figure 2 is a schematic illustration of the apparatus of the present invention.
  • Figure 3 is a schematic view of an anaerobic ammonium oxidation apparatus in the present invention.
  • Heterogeneous Fenton The pretreated water after pH adjustment is pumped into the heterogeneous Fenton device.
  • the internal reaction system consists of a catalyst composed of H 2 O 2 and the catalyst consists of nano-Fe 3 O 4 supported by Hangjin soil.
  • the nano-Fe 3 O 4 particles are uniformly distributed in the monodisperse form on the surface and the pores of the Hangjin soil, and the particle contact area can be enlarged while avoiding particle aggregation, thereby improving the reaction efficiency.
  • a dosing tank is attached to the top of the apparatus for replenishing the consumed H 2 O 2 into the reaction system.
  • a mechanical stirrer is arranged inside the device for uniformly mixing the wastewater with H 2 O 2 and the catalyst.
  • An external electromagnetic field is provided at the bottom, and a magnetic field is formed after the reaction is completed, and the catalyst is adsorbed to the bottom of the device by magnetic action. After that, the device starts to drain, and the effluent enters the anaerobic ammonia oxidation device. After the drainage is completed, the adsorbed catalyst is discharged from the sludge discharge port.
  • the reaction mechanism of the device is: nano-Fe 3 O 4 supported on Hangjin soil reacts with H 2 O 2 to form HO ⁇ , and the generated HO ⁇ is oxidized with refractory organic matter in wastewater to convert it into easily degradable small molecule. Organics and remove most of the COD.
  • the reaction conditions are as follows: the pH value is between 6.5 and 7.5, the influent COD concentration is between 2000 and 5000 mg/L, and the molar ratio of the amount of H 2 O 2 to the amount of the catalyst is between 1:1 and 1:1.5, and the temperature is At 25-35 ° C, the reaction time is 2-4 hours, and the effluent COD drops to between 350-900 mg/L.
  • Anaerobic ammonium oxidation After the wastewater is treated by heterogeneous Fenton catalytic oxidation, a large number of refractory toxic organic substances are removed, which will not cause toxicity to anammox bacteria. The influent COD content is lower than that of ammonia nitrogen. Under anoxic conditions, anaerobic ammonium oxidizing bacteria react NO 2 - -N and NH 4 + -N to form N 2 and denitrify. The anammox bacteria in the device are domesticated at 3%-10% salinity and are able to tolerate higher salinity.
  • the anaerobic ammonia oxidation device is a fully enclosed structure, and the bottom of the device is filled with anaerobic ammonium oxide granular sludge; the top of the device is provided with a polyethylene sponge as a filler; the middle of the device is equipped with a three-electrode system in which the carbon felt is a working electrode and the graphite sheet is The counter electrode, the saturated calomel electrode is a reference electrode; the device is equipped with a stirring paddle and a pH online controller to ensure that the wastewater and the granular sludge are thoroughly mixed, and the pH value of the device is monitored in real time; a circulating water bath is arranged outside the device. System to ensure the temperature required for the reaction.
  • the reaction conditions are: pH between 6.5-7.5, residence time between 5-15h, temperature between 30-35 °C, working voltage -0.1--0.02V, influent NH 4 + -N concentration at 800 Between 1500 mg/L, the aeration amount is 0.8-1.5 L/min, the stirring speed of the stirring paddle is about 12 rpm, and the denitrification rate is as high as 90% or more.
  • the effluent from the heterogeneous Fenton unit is pumped from the bottom of the anaerobic ammonia oxidation unit. After the reaction is completed, it is discharged from the top outlet, and the generated N 2 is discharged from the top exhaust port.
  • the effluent is discharged from the top into the MBR system, and the sludge is intermittently discharged.
  • the amount of sludge exceeds 90% of the bottom volume, sludge is required, and each sludge discharge accounts for between 1% and 5% of the total sludge. .
  • MBR Membrane Bio-Reactor, Membrane Bioreactor
  • Security filter The function of the security filter is to intercept particles larger than 5 ⁇ m from the MBR effluent to prevent the particles from being scratched by the high pressure pump and then scratching the RO membrane element (Reverse Osmosis membrane).
  • RO The security filter effluent enters the RO membrane module to remove most of the soluble salts and small molecules of soluble organic matter. Under sufficient pressure, the effluent produced by the influent water through the reverse osmosis membrane can be used as circulating cooling water in the process of production.
  • the equipment includes a concentric turbulent mixer, a new turbulent flocculation device, and a variable channel sloping plate sedimentation device.
  • softening and flocculation precipitation treatment are carried out by adding Na 2 CO 3 and polyacrylamide.
  • Nanofiltration After the RO concentrated water enters the NF system, it removes all kinds of substances with divalent and multivalent ions and molecular weight greater than 200Da.
  • the effluent mainly contains NaCl.
  • Multi-effect evaporation The main component of NF effluent is NaCl, which enters the multi-effect evaporation system to produce industrial NaCl.
  • the NF concentrated water mainly contains soluble silicon, Na 2 SO 4 and dissolved organic matter, and directly returns to the pretreatment process.
  • the high salt, high ammonia nitrogen, high concentration refractory organic wastewater referred to in the present invention has a salinity of 3%-10%, an ammonia nitrogen concentration of 1000-2500 mg/L, and a COD concentration of 2000-5000 mg/L.
  • the high-salt, high-ammonia-nitrogen, high-concentration refractory organic wastewater treatment device shown in FIG. 2 includes: a sedimentation tank 1, a storage tank 2, a heterogeneous Fenton device 3, an anaerobic ammonia oxidation device 4, and an immersed MBR system. 5, security filter 6, RO system 7, integrated softening coagulation sedimentation system 8, NF system 9, multi-effect evaporator 10, electromagnetic field 11, drug box 12-14, centrifugal pump 15-23, mechanical agitator 24- 25, flow meter 26-30.
  • the adjustment sedimentation tank 1 and the dosing tank 12 are connected by a pipeline, a centrifugal pump 15 and a flow meter 26, and the adjustment sedimentation tank 1 has a mechanical agitator 24 built therein, and the sedimentation tank 1 is adjusted to pass through the pipeline and the centrifugal pump 16 and the storage tank 2 Connection;
  • the storage tank 2 and the heterogeneous Fenton device 3 are connected by a pipeline, a flow meter 27 and a centrifugal pump 17; between the heterogeneous Fenton device 3 and the dosing tank 13 through a pipeline, a centrifugal pump 18, a flow meter 28 connected, the heterogeneous Fenton device 3 has a mechanical agitator 25 built therein, the heterogeneous Fenton device 3 and the anaerobic ammonium oxidation device 4 are connected by a pipeline, a centrifugal pump 19, and the electromagnetic field 11 is placed at the bottom of the heterogeneous Fenton device 3;
  • the anaerobic ammonium oxidation device 4 is a cylindrical reactor mainly composed of a circulating water bath inlet I, a circulating water bath outlet II, a water inlet a, a sludge outlet b, a sampling port cf, a water outlet g, and a row.
  • Air port h, sampling port i, aeration head j, perforated baffle k, stirring paddle l, graphite electrode m, carbon felt electrode n, potentiostat o, reference electrode (saturated calomel electrode) p, sponge filler r, pH online controller s constitutes.
  • the invention comprises the following steps in the deep treatment of high-salt, high-ammonia nitrogen and high-concentration refractory organic wastewater by using the above equipment:
  • Pretreatment raw water is input into the sedimentation tank 1, and polyacrylamide is added to the solution tank 12 through the centrifugal pump 15, and the dosage is controlled by the flow meter 26, and the reaction time is 4 hours, and a mechanical stirrer is arranged inside the device. 24, the reaction speed can be controlled, the sediment and water are separated in the equipment, the sediment is discharged by the sludge discharging pipe, and the effluent is introduced into the water storage tank 2 through the centrifugal pump 16.
  • Heterogeneous Fenton device the pretreated effluent is pumped into the heterogeneous Fenton device 3, the top of the heterogeneous Fenton device 3 is connected to the dosing tank 13, and the H 2 O is added to the device by the centrifugal pump 18. 2 solution, the dosage is controlled by the flow meter 28.
  • the heterogeneous Fenton device 3 has a heterogeneous Fenton system consisting of nano-ferric oxide and H 2 O 2 supported by Hangjin soil, and the wastewater is catalytically oxidized in the system.
  • the reaction, in which the macromolecular refractory organic matter is converted into small molecules, is removed, and a mechanical stirrer 25 is disposed in the heterogeneous Fenton device 3 to ensure uniform reaction.
  • the bottom of the heterogeneous Fenton device 3 is provided with an electromagnetic field 11 which is energized to form a magnetic field after the reaction is completed, and magnetically acts to adsorb the nano-Fe 3 O 4 supporting catalyst to the bottom. Thereafter, the heterogeneous Fenton device 3 starts to drain, and the effluent enters the anaerobic ammonia oxidation device 4 through the centrifugal pump 19, and the adsorbed catalyst is discharged from the sludge discharge port after the completion of the drainage.
  • the reaction conditions are as follows: the pH value is between 6.5 and 7.5, the influent COD concentration is between 2000 and 5000 mg/L, and the molar ratio of the amount of H 2 O 2 to the amount of the catalyst is between 1:1 and 1:1.5, and the temperature is At 25-35 ° C, the reaction time is 2-4 hours, and the effluent COD content is reduced to 350-900 mg / L.
  • the wastewater is treated by heterogeneous Fenton catalytic oxidation, the organic matter is greatly reduced, and most of the refractory highly toxic substances such as aromatic compounds, heterocyclic compounds, and organic chlorides are removed or decomposed into low molecular weight organic substances.
  • Anaerobic ammonium oxidation device The effluent of the heterogeneous Fenton device 3 is introduced into the anaerobic ammonium oxidation device 4 by the centrifugal pump 19, and the denitrification reaction is carried out under the action of the anaerobic ammonium oxidizing bacteria after acclimation with high salinity.
  • the reaction conditions are: pH between 6.5-7.5, residence time between 5-15h, temperature between 30-35 °C, working voltage -0.1--0.02V, influent NH 4 + -N concentration at 800 Between 1500 mg/L, the aeration amount is 0.8-1.5 L/min, the stirring speed of the stirring paddle is about 12 rpm, and the denitrification rate is as high as 90% or more.
  • the sludge is intermittently discharged. When the amount of sludge exceeds 90% of the bottom volume, sludge is discharged. Each sludge discharge accounts for between 1% and 5% of the total sludge.
  • the anaerobic ammonium oxidation device 4 has a cylindrical full-closed structure, and the bottom is filled with anaerobic ammonium oxide granular sludge after domestication and cultivation, and the outer layer of the granular sludge is an anaerobic layer in the inner layer of the aerobic layer.
  • the whole process of autotrophic denitrification can be realized in the anaerobic ammonium oxidation unit 4.
  • the effluent of the heterogeneous Fenton device 3 enters the anaerobic ammonium oxidation unit 4 from the water inlet a, and contacts the anaerobic ammonium oxide granular sludge through the perforated baffle k to cause a denitrification reaction.
  • the aeration head j at the bottom of the anaerobic ammonium oxidation device 4 converts the ammonia nitrogen portion of the wastewater into nitrous oxide by controlling the aeration amount; the agitating paddle 1 inside the anaerobic ammonium oxidation device 4 is used to oxidize the wastewater with anaerobic ammonium oxide particles.
  • the mud is uniformly mixed; the three-electrode system consisting of the graphite counter electrode m, the carbon felt working electrode n, the reference electrode p, and the potentiostat o in the anaerobic ammonium oxidation device 4 can effectively increase the activity of the anammox bacteria and reduce the nitric acid.
  • the salt nitrogen is nitrite nitrogen to improve the denitrification efficiency; the pH online controller of the anaerobic ammonium oxidation unit 4 is used to monitor the pH value change in the anaerobic ammonium oxidation unit 4 in real time, and is adjusted by adding HCl and NaHCO 3 .
  • the wastewater reacted with the anaerobic ammonium oxidized granular sludge is filtered by the sponge filler r and discharged from the water outlet g, and the N 2 generated by the reaction is discharged from the exhaust port h.
  • the denitrification inside the anaerobic ammonium oxidation unit 4 is monitored by sampling at the sampling ports cf, i.
  • the sludge is discharged from the sludge discharge port b at the bottom of the anaerobic ammonia oxidation unit 4.
  • the anaerobic ammonium oxidation unit 4 is provided with a circulating water bath inlet I and an outlet II, and the reaction temperature inside the anaerobic ammonia oxidation unit 4 is ensured by connecting a circulating water bath system.
  • the composition of the artificial wastewater is as follows:
  • the composition of the trace elements is: CuSO 4 ⁇ 5H 2 O 0.25mg/L, ZnSO 4 ⁇ 7H 2 O 0.43mg/L, CoCl 2 ⁇ 6H 2 O 0.24mg/ L, MnCl 2 ⁇ 4H 2 O 0.99 mg / L, NaMoO 4 ⁇ 2H 2 O 0.22 mg / L, NiCl 2 ⁇ 6H 2 O 0.19 mg / L, NaSeO 4 0.11 mg / L, H 3 BO 3 0.014 mg / L ;
  • the carbon felt is used as the working electrode, the graphite sheet is the counter electrode, and the saturated calomel electrode is the reference electrode.
  • the applied electric field can effectively increase the activity of the anammox bacteria, thereby shortening the startup time.
  • the electrons generated by the applied electric field can also reduce the NO 3 - - N, a by-product of the anaerobic ammonium oxidation reaction, thereby contributing to the improvement of the nitrogen removal efficiency of the system;
  • anaerobic ammonium oxide granular sludge After cultivation and domestication, the outer layer of anaerobic ammonium oxide granular sludge is accompanied by facultative bacteria, which can consume dissolved oxygen in the reactor and create anaerobic conditions for anaerobic ammonium oxidation reaction in the granular sludge;
  • polyethylene sponge filler can attach part of the granular sludge on the one hand to improve the nitrogen removal efficiency of the reactor; on the other hand, it can effectively prevent sludge outflow.
  • the influent water is replaced by high-salt, high-ammonia nitrogen, high-concentration refractory organic wastewater.
  • MBR The device is an immersed MBR system. After the effluent of the anaerobic ammonium oxidation device 4 enters the MBR system 5 through the centrifugal pump 20, the organic matter is further removed and denitrified by the biodegradation and retention of the high concentration activated sludge.
  • RO The MBR effluent enters the security filter 6 through the centrifugal pump 21 to intercept particles having a particle diameter of more than 5 ⁇ m.
  • the security filter effluent enters the RO system 7, and is filtered by the high pressure pump along the surface of the membrane. almost all ions are trapped by the RO membrane.
  • the effluent is ion-free water, which can be used as circulating cooling water in the process of production. The water flows into the subsequent process to continue processing.
  • NF RO concentrated water first enters the integrated softening, coagulation and sedimentation system 8, and the treatment tank 14 is fed with Na 2 CO 3 and polyacrylamide through the centrifugal pump 22, and the dosage is increased by the flow meter 29 control.
  • the wastewater is mixed with softener and flocculant in the system, the sedimentation design stays for 2h, the effluent enters the NF system 9, and the divalent SiO 3 2- and SO 4 2- are trapped to form NF concentrated water, and the generated NF concentrated water is centrifuged.
  • the pump 23 returns to the adjustment sedimentation tank 1, and the flow rate is controlled by the flow meter 30.
  • the NF effluent mainly contains NaCl, and enters the multi-effect evaporator 10 to evaporate and recover NaCl.
  • the wastewater is from wastewater discharged from coal gasification syngas condensate.
  • the water quality of the wastewater is as follows: pH 7.5-8.2, COD 3000-4800 mg/L, NH 4 + -N 1600-2300 mg/L, salinity 6%. -8%, phenol content is 420-810 mg / L.
  • the wastewater is pumped into the regulating sedimentation tank. After filling, 0.5% polyacrylamide solution is added, and the ratio of 2kg polyacrylamide/m 3 wastewater is added to remove suspended solids and colloidal substances. After the sedimentation, the effluent enters the heterogeneous phase. Fenton device.
  • the catalyst is nano-Fe 3 O 4 supported by Hangjin soil.
  • the preparation method comprises the steps of mixing FeCl 3 ⁇ 6H 2 O, FeCl 2 ⁇ 4H 2 O and hydrochloric acid solution at a molar ratio of 2:1:1, and slowly adding hydrochloric acid to the deoxygenation.
  • an acidic solution is prepared, and then FeCl 3 ⁇ 6H 2 O, FeCl 2 ⁇ 4H 2 O is dissolved in the solution, and after completely dissolved, the volume is made up to 100 ml with deoxygenated water.
  • the effluent from the pretreatment process enters the heterogeneous Fenton unit, and the H 2 O 2 solution is added and continuously stirred.
  • the molar ratio of the amount of H 2 O 2 to the amount of the catalyst is 1:1, the temperature is 25 ° C, and the reaction time is 2 hours.
  • COD The removal rate is between 83% and 85%, the effluent COD content is reduced to 450-810 mg/L, the phenol removal rate is 85%-93%, and the effluent phenol content is reduced to 30-80 mg/L.
  • the effluent enters the anaerobic ammonium oxidation unit.
  • the wastewater enters from the bottom of the anaerobic ammonia oxidation unit and is thoroughly mixed with the anaerobic ammonium oxidation sludge.
  • the reaction conditions are as follows: pH between 6.5 and 7.5, residence time between 5 and 15 hours, and temperature between 30 and 35 °C. Between, the working voltage is -0.1--0.02V, the influent NH 4 + -N concentration is between 800-1500mg/L, the aeration rate is 0.8-1.5L/min, and the stirring speed of the stirring paddle is about 12 rpm. . After the reaction, the effluent NH 4 + -N was lowered to 150-220 mg/L, and the COD was lowered to 220-400 mg/L. The effluent enters the MBR system.
  • the wastewater enters the MBR system, and the organic matter is further removed and denitrified by the biodegradation and retention of the high-concentration activated sludge.
  • the effluent COD is less than 50 mg/L, and the NH 4 + -N is less than 5 mg/L.
  • the wastewater first enters the security filter to remove particles larger than 5 ⁇ m, and the effluent enters the RO system.
  • the produced water contains almost no ions and can be reused as circulating cooling water.
  • the salt content of concentrated water is between 10% and 25%, and the content of Ca and Mg ions is between 480-560 mg/L and 55-70 mg/L, respectively.
  • the concentrated water directly enters the softening treatment process.
  • the wastewater enters the integrated softening and coagulation sedimentation equipment, and Na 2 CO 3 and polyacrylamide are added.
  • the dosage is 3kg sodium carbonate/m 3 wastewater and 2kg polyacrylamide/m 3 wastewater respectively.
  • the removal rate of Ca and Mg ions in the post-waste water is above 85%.
  • the wastewater enters the NF system and intercepts a large amount of divalent ions.
  • the NaCl content in the effluent accounts for 90% of the total ion.
  • the effluent enters the evaporation device, and the concentrated water returns to the pretreatment process.
  • the NaCl in the NF effluent was recovered by evaporation, and the purity of NaCl was above 85%.

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Abstract

一种有机废水的处理回用方法：1)有机废水进行预处理；2)步骤1预处理后的出水进行非均相Fenton反应，杭锦土负载的纳米Fe 3O 4为催化剂，反应结束后将催化剂与反应液分离，反应液进行COD去除反应；3)步骤2的出水进行厌氧氨氧化反应，使氨氮和亚硝酸盐氮反应而脱氮；4)步骤3的出水经好氧微生物分解和超滤膜分离后，去除COD和氨氮；5)步骤4的出水进行过滤去除大粒径颗粒；6)步骤5的出水进入RO系统，RO系统的出水用作循环冷却水，RO系统的浓水进行软化处理；7)步骤6软化后的浓水进入NF系统处理，处理后的出水进行蒸发回收NaCl，产生的浓水返回步骤1。一种实现有机废水处理回用方法的设备，包括调节沉淀池（1）、贮水池（2）、非均相Fenton装置（3）、厌氧氨氧化装置（4）、浸没式MBR系统（5）、保安过滤器（6）、RO系统（7）、一体化软化混凝沉淀系统（8）、NF系统（9）和多效蒸发器（10）等。

Description

一种有机废水的处理回用方法和设备 技术领域
本发明属于工业废水处理领域，具体地涉及一种高盐、高氨氮、高浓度难降解有机废水的处理回用方法。
本发明还涉及一种用于实现上述方法的设备。
背景技术
随着社会经济的快速发展，人民生活水平的提高，水环境污染问题日益引起了社会的广泛关注。几十年来，技术的进步和经验的累积，使得常规生活污水得到有效地处理，但对于工业废水中难降解有机污染物，由于其成分复杂、分子结构稳定，采用常规的生化处理技术很难达标。特别是高盐、高氨氮、高浓度难降解有机废水的处理，仍需要不断地探索和研究。此外，随着排放标准的升高和用水成本的增加，处理后废水的分质回用显得越来越重要。
从来源上看，高盐、高氨氮、高浓度难降解有机废水主要来自合成制药、农药生产、造纸黑液、制革废水、味精生产、石油炼制、煤化工等行业。从结构和特性来看，难降解有机物主要包括：多环芳烃类、杂环化合物、氯化芳香族化合物、有机氰化物、有机合成高分子化合物等。这些化合物的降解机理是通过氧化、还原、共代谢等机制改变其分子结构，并逐渐转化为小分子。因而，可采用湿式催化氧化、超临界氧化、Fenton处理、臭氧氧化等技术来处理难降解有机物，但在氨氮浓度较高的情况下，后续采用传统的厌氧或好氧工艺很难达到脱氮要求。此外，由于有机物浓度较高，采用多效蒸发或反渗透处理时，容易造成蒸发器堵塞或膜结垢，造成清洗困难，处理成本增加。
Fenton技术是一种常用的高级氧化技术，经常被用于处理高浓度难降解有机废水，如染料废水、含酚废水、丙烯腈废水、造纸黑液、垃圾渗滤液等。但无论是标准Fenton试剂还是改性Fenton试剂，都要求在pH为 3-5之间才能发挥正常的作用。而非均相Fenton技术通过将铁催化剂负载到基质上，即使在pH为中性条件下，仍能产生较多的HO·，从而避免了后续生物处理前加碱调节pH值导致盐度过高的问题。在COD降下来后，脱氮处理还需补充碳源，导致成本升高。厌氧氨氧化技术能够以硝酸盐或亚硝酸盐为电子受体进行脱氮，可以有效解决该问题。
发明内容
本发明的目的在于提供一种高盐、高氨氮、高浓度难降解有机废水的处理回用方法。
本发明的又一目的是提供一种用于实现上述方法的设备。
为实现上述目的，本发明将非均相Fenton法、厌氧氨氧化工艺与膜处理法相结合，以处理高盐、高氨氮、高浓度难降解有机废水。
进一步地，本发明提供的高盐、高氨氮、高浓度难降解有机废水的处理回用方法，其流程如下：
1)有机废水进行预处理，加入絮凝剂去除水中悬浮物和胶体物质；
2)步骤1预处理后的出水进行非均相Fenton反应，杭锦土负载的纳米Fe3O4为催化剂，反应结束后将催化剂与反应液分离，反应液进行脱氮和COD反应；
3)步骤2的出水进行厌氧氨氧化反应，使得氨氮和亚硝酸盐氮反应而脱氮；4)步骤3的出水经好氧微生物分解和超滤膜分离后，进一步去除COD和氨氮；
5)步骤4的出水进行过滤去除大粒径颗粒；
6)步骤5的出水进入RO系统，RO系统的出水用作循环冷却水，RO系统的浓水进行软化处理；
7)步骤6软化后的浓水进入NF系统处理，处理后的出水进行蒸发回收NaCl，产生的浓水返回步骤1。
所述的处理回用方法，其中，步骤1的有机废水的盐度为3％-10％，氨氮浓度为1000-2500mg/L，COD浓度为2000-5000mg/L，絮凝剂为聚丙烯酰胺。
所述的处理回用，其中，步骤2中非均相Fenton反应的pH值在6.5-7.5 之间；催化剂中的纳米Fe3O4颗粒以单分散形式均匀地分布在杭锦土的表面和孔道内；反应结束后采用外加磁场的方式使催化剂在非均相Fenton装置底部聚集，实现催化剂与反应液的分离。
所述的处理回用方法，其中，步骤5中浓水软化所采用的软化剂为Na2CO3。
所述的处理回用方法，其中，步骤6中的出水经多效蒸发器处理后生产工业NaCl。
本发明提供的用于实现上述处理回用方法的设备：
调节沉淀池，连接有加药箱，调节沉淀池内设有搅拌器，调节沉淀池设有原水的进水口和沉淀排污口，调节沉淀池通过泵、流量计连接至贮水池；
贮水池通过泵、流量计和非均相Fenton装置相连接，非均相Fenton装置连接有加药箱，非均相Fenton装置内设有搅拌器，非均相Fenton装置的底部置有电磁场，非均相Fenton装置通过泵连接厌氧氨氧化装置；
厌氧氨氧化装置通过泵连接浸没式MBR系统，浸没式MBR系统的出水口通过泵连接保安过滤器，保安过滤器的出水口连接RO系统，RO系统处理后达标的出水作为循环冷却水，RO系统的浓水出口连接一体化软化混凝沉淀系统，一体化混凝沉淀系统通过流量计和泵连接加药箱，一体化软化混凝沉淀系统的出水口连接NF系统，NF系统处理后的出水连接多效蒸发器，NF系统的浓水出口通过泵、流量计返回至调节沉淀池。
所述的设备，其中，厌氧氨氧化装置为全密闭结构的容器，侧壁设有若干个采样口，顶部设有排气口，上部设有出水口和循环冷却水的出水口，下部设有循环冷却水的进水口，底部设有进水口，进水口的上方设有曝气头，搅拌桨设在曝气头的上方；
厌氧氨氧化装置内填充有厌氧氨氧化颗粒污泥，颗粒污泥外层为好氧层，内层为厌氧层，能在厌氧氨氧化装置内实现全程自养脱氮过程；
厌氧氨氧化装置内设有石墨对电极、碳毡工作电极和参比电极，石墨对电极、碳毡工作电极和参比电极均连接恒电位仪；
厌氧氨氧化装置内设置的pH在线控制器用以实时监控装置内pH值的变化，并通过添加HCl和NaHCO3调节厌氧氨氧化装置内的pH值。
所述的设备，其中，曝气头通过上方设置的带孔挡板与厌氧氨氧化颗粒污泥接触发生脱氮反应。
所述的设备，其中，颗粒污泥与出水口之间设有海绵填料。
所述的设备，其中，泵为离心泵，搅拌浆为机械搅拌浆。
本发明能够实现对高盐、高氨氮、高浓度难降解有机废水的处理及回收利用，具有适用范围广、污染物降解效率高、易于盐分回收利用的特点。
附图说明
图1是本发明的流程示意图。
图2是本发明的装置示意图。
图3是本发明中的厌氧氨氧化装置示意图。
具体实施方式
请参阅图1。本发明公开的
Figure PCTCN2016080860-appb-000001
Figure PCTCN2016080860-appb-000002
的组合工艺，主要工序包括：
1)预处理：原水进入调节沉淀池后，投加聚丙烯酰胺，反应时间4h，沉淀物与水在池内分离，出水进入贮水池。沉淀过程中产生的污泥送至污泥处理站处理。
2)非均相Fenton：经pH值回调后的预处理水被泵入非均相Fenton装置，装置内部的反应体系由催化剂与H2O2构成，催化剂由杭锦土负载的纳米Fe3O4构成，纳米Fe3O4颗粒以单分散形式均匀地分布在杭锦土的表面和孔道内，在避免颗粒聚集的同时还能够扩大其与废水接触的面积，提高反应效率。装置顶部连有加药箱用于向反应体系内补充消耗的H2O2。装置内部设有机械搅拌器，用于将废水与H2O2、催化剂均匀混合。底部设有外加电磁场，在反应结束后通电形成磁场，利用磁性作用将催化剂吸附在装置底部。之后，装置开始排水，出水进入厌氧氨氧化装置，排水结束后，被吸附的催化剂由排泥口排出。该装置的反应机理是：负载在杭锦土上的纳米Fe3O4与H2O2反应生成HO·，生成的HO·与废水中难降解有机物发生氧化反应，使其转化为易降解的小分子有机物并去除大部分COD。 反应条件为：pH值在6.5-7.5之间，进水COD浓度在2000-5000mg/L之间，H2O2用量与催化剂用量的摩尔比为1:1-1:1.5之间，温度为25-35℃，反应时间为2-4小时，出水COD降至350-900mg/L之间。
3)厌氧氨氧化：废水经非均相Fenton催化氧化处理后，大量难降解有毒有机物被去除，不会对厌氧氨氧化菌产生毒性。进水中COD含量低于氨氮，在缺氧的条件下，厌氧氨氧化菌使得NO2 --N和NH4 +-N反应生成N2而脱氮。装置内的厌氧氨氧化菌在3％-10％的盐度下驯化，能够耐受较高的盐度。厌氧氨氧化装置为全密闭结构，装置底部充满厌氧氨氧化颗粒污泥；装置顶部附有聚乙烯海绵作为填料；装置中部装有三电极体系，该体系中碳毡为工作电极，石墨片为对电极，饱和甘汞电极为参比电极；装置内部装有搅拌桨和pH在线控制器，分别用以保证废水与颗粒污泥充分混合，并实时监控装置pH值变化；装置外部设有循环水浴系统，用以保证反应所需要的温度。反应条件为：pH值在6.5-7.5之间，停留时间在5-15h之间，温度在30-35℃之间，工作电压-0.1--0.02V，进水NH4 +-N浓度在800-1500mg/L之间，曝气量为0.8-1.5L/min，搅拌桨的搅拌速率约为12转/分，脱氮率高达90％以上。非均相Fenton装置出水由厌氧氨氧化装置底部泵入，反应结束后由顶部出水口排出，产生的N2由顶部排气口排出。反应结束后出水由顶部排出进入MBR系统，污泥间歇排出，当污泥量超出底部容积的90％时，需要排泥，每次排泥量占污泥总量的1％-5％之间。
4)MBR(Membrane Bio-Reactor,膜生物反应器)：废水进入MBR后，通过高浓度活性污泥的生物降解、截留作用，对小分子有机化合物进一步生化降解，同时也截留部分悬浮物。采用浸没式MBR装备处理厌氧氨氧化装置出水，装置内设中空纤维超滤膜，采用连续或间歇曝气方式对运行条件进行优化。
5)保安过滤器：保安过滤器的作用是截留MBR出水带来的大于5μm的颗粒，以防止颗粒经高压泵加速后划伤RO膜元件(Reverse Osmosis membrane)。
6)RO：保安过滤器出水进入RO膜组件，去除绝大部分可溶性盐分、小分子可溶性有机物等。在足够的压力下，进水通过反渗透膜产生的出水可用作工艺生产过程中循环冷却水。
7)软化处理：由于浓缩作用，RO浓水的COD和硬度偏高，为防止堵塞膜片，RO浓水需在一体化软化、混凝沉淀系统中进行软化处理。该设备包括同心湍流混合器、新型湍流絮凝装置和变流道斜板沉淀装置。在设备内，通过投加Na2CO3、聚丙烯酰胺进行软化、絮凝沉淀处理。
8)纳滤：RO浓水进入NF系统后，去除二价和多价离子、分子量大于200Da的各类物质，出水中主要含有NaCl。
9)多效蒸发：NF出水主要成分为NaCl，进入多效蒸发系统生产工业NaCl，NF浓水主要含有可溶性硅、Na2SO4和溶解性有机物，直接返回预处理工艺处理。
本发明所指的高盐、高氨氮、高浓度难降解有机废水盐度在3％-10％之间，氨氮浓度在1000-2500mg/L之间，COD浓度在2000-5000mg/L之间。
以下结合附图和具体实施例对本发明的设备作进一步说明。
如图2所示的高盐、高氨氮、高浓度难降解有机废水处理装置，包括：调节沉淀池1、贮水池2、非均相Fenton装置3、厌氧氨氧化装置4、浸没式MBR系统5、保安过滤器6、RO系统7、一体化软化混凝沉淀系统8、NF系统9、多效蒸发器10，电磁场11，药剂箱12-14、离心泵15-23、机械搅拌器24-25、流量计26-30。调节沉淀池1和加药箱12之间通过管路、离心泵15和流量计26连接，调节沉淀池1内置有机械搅拌器24，调节沉淀池1通过管路和离心泵16与贮水池2连接；贮水池2和非均相Fenton装置3之间通过管路、流量计27和离心泵17连接；非均相Fenton装置3和加药箱13之间通过管路、离心泵18、流量计28连接，非均相Fenton装置3内置有机械搅拌器25，非均相Fenton装置3和厌氧氨氧化装置4通过管路、离心泵19连接，非均相Fenton装置3底部置有电磁场11；厌氧氨氧化装置4和浸没式MBR系统5通过管路、离心泵20连接；浸没式MBR系统5和保安过滤器6通过管路、离心泵21连接；保安过滤器6和RO系统7通过管路连接；RO系统7和一体化软化混凝沉淀系统8通过管路连接；一体化混凝沉淀系统8和加药箱14之间通过管路、流量计29、离心泵22连接，一体化软化混凝沉淀系统8和NF系统9之间通过管路连接；NF系统9和多效蒸发器10通过管路连接，NF系统9和调节沉淀池1 通过管路、离心泵23和流量计30连接。
如图3所示，厌氧氨氧化装置4为圆柱形反应器，主要由循环水浴进水口Ⅰ、循环水浴出水口Ⅱ、进水口a、排泥口b、采样口c-f、出水口g、排气口h、采样口i、曝气头j、带孔挡板k、搅拌桨l、石墨电极m、碳毡电极n、恒电位仪o、参比电极(饱和甘汞电极)p、海绵填料r、pH在线控制器s构成。
本发明在使用上述设备进行高盐、高氨氮、高浓度难降解有机废水深度处理时，包括如下步骤：
1)预处理：将原水输入调节沉淀池1，由加药箱12通过离心泵15向其中投加聚丙烯酰胺，投加量由流量计26控制，反应时间4h，装置内部设有机械搅拌器24，可控制反应速度，沉淀物与水在设备内分离，沉淀物由排泥管道排出，出水通过离心泵16作用进入贮水池2。
2)非均相Fenton装置：经预处理后的出水被泵入非均相Fenton装置3，非均相Fenton装置3顶部与加药箱13连接，通过离心泵18向装置内投加H2O2溶液，投加量由流量计28控制，非均相Fenton装置3内部有由杭锦土负载的纳米四氧化三铁和H2O2构成的非均相Fenton体系，废水在该体系内发生催化氧化反应，其中大分子难降解有机物被转化为小分子而去除，非均相Fenton装置3内设有机械搅拌器25，保证反应均匀。非均相Fenton装置3底部设有电磁场11，在反应结束后通电形成磁场，利用磁性作用将负载纳米Fe3O4的杭锦土催化剂吸附在底部。之后，非均相Fenton装置3开始排水，出水通过离心泵19进入厌氧氨氧化装置4，待排水结束后被吸附的催化剂由排泥口排出。反应条件为：pH值在6.5-7.5之间，进水COD浓度在2000-5000mg/L之间，H2O2用量与催化剂用量的摩尔比为1:1-1:1.5之间，温度为25-35℃，反应时间为2-4小时，出水COD含量降至350-900mg/L之间。废水经非均相Fenton催化氧化处理后，有机物种类大大减少，芳香族化合物、杂环化合物、有机氯化物等难降解高毒性物质被大部分去除或分解为低分子量的有机物。
3)厌氧氨氧化装置：非均相Fenton装置3出水经离心泵19作用进入厌氧氨氧化装置4后，在经高盐度驯化后的厌氧氨氧化菌作用下实施脱氮反应。反应条件为：pH值在6.5-7.5之间，停留时间在5-15h之间，温度 在30-35℃之间，工作电压-0.1--0.02V，进水NH4 +-N浓度在800-1500mg/L之间，曝气量为0.8-1.5L/min，搅拌桨的搅拌速率约为12转/分，脱氮率高达90％以上。污泥间歇排出，当污泥量超出底部容积的90％时，开始排泥，每次排泥量占污泥总量的1％-5％之间。
如图3所示，厌氧氨氧化装置4为圆柱形全密闭结构，底部充满经驯化培养后的厌氧氨氧化颗粒污泥，颗粒污泥外层为好氧层内层为厌氧层，能够在厌氧氨氧化装置4内实现全程自养脱氮过程。非均相Fenton装置3出水由进水口a进入厌氧氨氧化装置4，透过带孔挡板k与厌氧氨氧化颗粒污泥接触，发生脱氮反应。厌氧氨氧化装置4底部的曝气头j通过控制曝气量使得废水中氨氮部分转化成亚硝氮；厌氧氨氧化装置4内部的搅拌桨l用于将废水与厌氧氨氧化颗粒污泥混合均匀；厌氧氨氧化装置4内部的石墨对电极m、碳毡工作电极n、参比电极p、恒电位仪o构成的三电极体系可有效提高厌氧氨氧化菌的活性并还原硝酸盐氮为亚硝酸盐氮以提高脱氮效率；厌氧氨氧化装置4内部的pH在线控制器s用以实时监控厌氧氨氧化装置4内pH值的变化，并通过添加HCl和NaHCO3调节厌氧氨氧化装置4内pH值。与厌氧氨氧化颗粒污泥作用的废水经海绵填料r过滤后由出水口g排出，反应产生的N2由排气口h排出。通过在采样口c-f、i采样测定，监测厌氧氨氧化装置4内部的脱氮情况。污泥由厌氧氨氧化装置4底部的排泥口b排出。厌氧氨氧化装置4外部设有循环水浴进口Ⅰ和出口Ⅱ，通过连接循环水浴系统保证厌氧氨氧化装置4内部的反应温度。
厌氧氨氧化颗粒污泥的培养驯化过程：
①向反应器中接种厌氧氨氧化污泥；
②向人工废水中充入氮气，使废水中的DO浓度为0mg/L，调节pH为7-8；人工废水成分如下：
NH4 +-N 100mg/L，NO2--N 100mg/L，KHCO3 1.5-2.0g/L，NaCl 10g/L，KH2PO4 54mg/L，FeSO4·7H2O 9mg/L，EDTA 5mg/L，微量元素1mL/L；所述微量元素的成分为：CuSO4·5H2O 0.25mg/L，ZnSO4·7H2O 0.43mg/L，CoCl2·6H2O 0.24mg/L，MnCl2·4H2O 0.99mg/L，NaMoO4·2H2O 0.22mg/L，NiCl2·6H2O 0.19mg/L，NaSeO4 0.11mg/L，H3BO3 0.014mg/L；
③采用碳毡为工作电极，石墨片为对电极，饱和甘汞电极为参比电极。外加电场可有效提高厌氧氨氧化菌活性，进而缩短启动时间。此外，外加电场产生的电子还可以还原厌氧氨氧化反应的副产物NO3--N，从而有助于提高系统的脱氮效率；
④提高人工废水总氮浓度并降低水力停留时间，逐渐提高进水负荷；
⑤待反应稳定后，逐步提高人工废水中DO浓度，以培养反应器内可以消耗氧气的细菌；
⑥经过培养驯化，厌氧氨氧化颗粒污泥外层附有兼氧菌，可消耗反应器内的溶解氧，为颗粒污泥内部厌氧氨氧化反应营造厌氧条件；
⑦向反应器中接种亚硝化菌，并适当降低人工废水中的亚硝酸盐氮浓度，同时向反应器进行曝气，控制曝气量使得人工废水中的氨氮部分转化成为亚硝氮；
⑧在线监测反应器内pH值，通过添加HCl和NaHCO3控制反应器内pH值为7.5-8.0之间；
⑨经过驯化培养，部分亚硝化菌成功附着在厌氧氨氧化颗粒污泥外表面，形成了外层好氧内层厌氧的颗粒污泥，实现了全程自养脱氮反应器高效启动过程；
⑩聚乙烯海绵填料的添加，一方面可以附着部分颗粒污泥，以提高反应器脱氮效率；另一方面，也可有效防止污泥外流。
反应器成功启动后，进水换为高盐、高氨氮、高浓度难降解有机废水。
4)MBR：该装置为浸没式MBR系统，厌氧氨氧化装置4出水经离心泵20作用进入MBR系统5后，通过高浓度活性污泥的生物降解、截留作用，进一步去除有机物并脱氮。
5)RO：MBR出水经离心泵21作用进入保安过滤器6，截留粒径大于5μm的颗粒。保安过滤器出水进入RO系统7，在高压泵作用下沿膜表面错流过滤，几乎所有的离子均被RO膜截留，出水为无离子水，可用作工艺生产过程中循环冷却水，RO浓水流入后续工序继续处理。
6)NF：RO浓水先进入一体化软化、混凝沉淀系统8，由加药箱14通过离心泵22向系统中投加Na2CO3、聚丙烯酰胺进行处理，投加量由流量计29控制。废水与软化剂、絮凝剂在系统内湍流混合，沉淀设计停留 2h，出水进入NF系统9，二价的SiO3 2-和SO4 2-被截留生成NF浓水，生成的NF浓水通过离心泵23返回调节沉淀池1，流量由流量计30控制，NF出水中主要含有NaCl，进入多效蒸发器10蒸发回收NaCl。
实施例：
下面以某煤化工企业含盐废水为例来说明本发明：
该废水来自煤气化合成气冷凝液排放废水，该废水的水质如下：pH值为7.5-8.2，COD为3000-4800mg/L，NH4 +-N为1600-2300mg/L，盐度为6％-8％，苯酚含量为420-810mg/L。
本实施例是采用本发明的的设备完成。
1、预处理工序
将废水用泵打入调节沉淀池，注满后投加0.5％的聚丙烯酰胺溶液，投加比例为2kg聚丙烯酰胺/m3废水，去除悬浮物和胶体物质，沉淀后出水进入非均相Fenton装置。
2、非均相Fenton装置
催化剂为杭锦土负载的纳米Fe3O4，其制备方法为将FeCl3·6H2O、FeCl2·4H2O、盐酸溶液以摩尔比2:1:1混合，先将盐酸缓缓加入除氧水中，制成酸性溶液，再以此溶液溶解FeCl3·6H2O、FeCl2·4H2O，待完全溶解后用除氧水定容至100ml。称取5g杭锦土在不断搅拌下加入150ml浓氨水，使溶液中的杭锦土完全呈现悬浮态，向其中逐滴加入上述制备好的Fe2+/Fe3+溶液，滴加的同时通N2除氧。此时出现黑色悬浮液，滴加完毕后，继续搅拌老化20min，静置于外磁场下固液分离，反复用除氧水洗涤3次后，60℃下真空干燥12h，隔气储存。
预处理工序的出水进入非均相Fenton装置，加入H2O2溶液并不断搅拌，H2O2用量与催化剂用量的摩尔比为1:1，温度为25℃，反应时间为2小时，COD去除率为83％-85％之间，出水COD含量降至450-810mg/L之间，苯酚去除率为85％-93％，出水苯酚含量降至30-80mg/L。出水进入厌氧氨氧化装置。
3、厌氧氨氧化装置
废水从厌氧氨氧化装置底部进入，与厌氧氨氧化污泥充分混合，控制反应条件为：pH值在6.5-7.5之间，停留时间在5-15h之间，温度在30-35℃ 之间，工作电压-0.1--0.02V，进水NH4 +-N浓度在800-1500mg/L之间，曝气量为0.8-1.5L/min，搅拌桨的搅拌速率约为12转/分。反应结束后，出水NH4 +-N降至150-220mg/L，COD降至220-400mg/L。出水进入MBR系统。
4、MBR
废水进入MBR系统，经高浓度活性污泥的生物降解、截留作用，进一步去除有机物并脱氮，出水COD小于50mg/L，NH4 +-N小于5mg/L。
5、保安过滤器
废水先进入保安过滤器去除粒径大于5μm颗粒，出水进入RO系统。
6、RO系统
废水进入RO系统后，经脱盐处理，脱盐率在99％以上，产水几乎不含离子，可回用作循环冷却水。浓水含盐量在10％-25％之间，Ca、Mg离子含量分别在480-560mg/L和55-70mg/L之间，浓水直接进入软化处理工序。
7、软化处理
废水先进入一体化软化、混凝沉淀设备，投加Na2CO3和聚丙烯酰胺，投加比例分别为3kg碳酸钠/m3废水和2kg聚丙烯酰胺/m3废水，经混凝软化处理后废水中Ca、Mg离子去除率在85％以上。
8、NF系统
废水进入NF系统，截留了大量二价离子，出水中NaCl含量占全部离子总量的90％，出水进入蒸发装置，浓水返回预处理工序。
9、蒸发装置
采用蒸发的方式回收NF出水中NaCl，NaCl纯度在85％以上。

Claims (10)

  1. 一种有机废水的处理回用方法，其流程如下：
    1)有机废水进行预处理，加入絮凝剂去除水中悬浮物和胶体物质；
    2)步骤1预处理后的出水进行非均相Fenton反应，杭锦土负载的纳米Fe3O4为催化剂，反应结束后将催化剂与反应液分离，反应液进行COD去除反应；
    3)步骤2的出水进行厌氧氨氧化反应，使得氨氮和亚硝酸盐氮反应而脱氮；
    4)步骤3的出水经好氧微生物分解和超滤膜分离后，进一步去除COD和氨氮；
    5)步骤4的出水进行过滤去除大粒径颗粒；
    6)步骤5的出水进入RO系统，RO系统的出水用作循环冷却水，RO系统的浓水进行软化处理；
    7)步骤6软化后的浓水进入NF系统处理，处理后的出水进行蒸发回收NaCl，产生的浓水返回步骤1。
  2. 根据权利要求1所述的处理回用方法，其中，步骤1的有机废水的盐度为3％-10％，氨氮浓度为1000-2500mg/L，COD浓度为2000-5000mg/L，絮凝剂为聚丙烯酰胺。
  3. 根据权利要求1所述的处理回用方法，其中，步骤2中非均相Fenton反应的pH值在6.5-7.5之间；催化剂中的纳米Fe3O4颗粒以单分散形式均匀地分布在杭锦土的表面和孔道内；反应结束后采用外加磁场的方式使催化剂在非均相Fenton装置底部聚集，实现催化剂与反应液的分离。
  4. 根据权利要求1所述的处理回用方法，其中步骤3中亚硝酸盐氮来自氨氮的亚硝化反应和三电极体系对硝酸盐氮的还原。
  5. 根据权利要求1所述的处理回用方法，其中，步骤6中浓水软化所采用的软化剂为Na2CO3。
  6. 根据权利要求1所述的处理回用方法，其中，步骤7中的出水经多效蒸发器处理后生产工业NaCl。
  7. 一种用于实现权利要求1所述处理回用方法的设备：
    调节沉淀池，连接有加药箱，调节沉淀池内设有搅拌器，调节沉淀池设有原水的进水口和沉淀排污口，调节沉淀池通过泵、流量计连接至贮水池；
    贮水池通过泵、流量计和非均相Fenton装置相连接，非均相Fenton装置连接有加药箱，非均相Fenton装置内设有搅拌器，非均相Fenton装置的底部置有电磁场，非均相Fenton装置通过泵连接厌氧氨氧化装置；
    厌氧氨氧化装置通过泵连接浸没式MBR系统，浸没式MBR系统的出水口通过泵连接保安过滤器，保安过滤器的出水口连接RO系统，RO系统处理后达标的出水作为循环冷却水，RO系统的浓水出口连接一体化软化混凝沉淀系统，一体化混凝沉淀系统通过流量计和泵连接加药箱，一体化软化混凝沉淀系统的出水口连接NF系统，NF系统处理后的出水连接多效蒸发器，NF系统的浓水出口通过泵、流量计返回至调节沉淀池。
  8. 根据权利要求7所述的设备，其中，厌氧氨氧化装置为全密闭结构的容器，侧壁设有若干个采样口，顶部设有排气口，上部设有出水口和循环冷却水的出水口，下部设有循环冷却水的进水口，底部设有进水口，进水口的上方设有曝气头，搅拌桨设在曝气头的上方；
    厌氧氨氧化装置内填充有厌氧氨氧化颗粒污泥，颗粒污泥外层为好氧层，内层为厌氧层，能在厌氧氨氧化装置内实现全程自养脱氮过程；
    厌氧氨氧化装置内设有石墨对电极、碳毡工作电极和参比电极，石墨对电极、碳毡工作电极和参比电极均连接恒电位仪；
    厌氧氨氧化装置内设置的pH在线控制器用以实时监控装置内pH值的变化，并通过添加HCl和NaHCO3调节厌氧氨氧化装置内的pH值。
  9. 根据权利要求8所述的设备，其中，曝气头通过上方设置的带孔挡板与厌氧氨氧化颗粒污泥接触发生脱氮反应；颗粒污泥与出水口之间设有海绵填料。
  10. 根据权利要求7所述的设备，其中，泵为离心泵，搅拌浆为机械搅拌浆。
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