CN110790378B - Method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling - Google Patents
Method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling Download PDFInfo
- Publication number
- CN110790378B CN110790378B CN201911193092.9A CN201911193092A CN110790378B CN 110790378 B CN110790378 B CN 110790378B CN 201911193092 A CN201911193092 A CN 201911193092A CN 110790378 B CN110790378 B CN 110790378B
- Authority
- CN
- China
- Prior art keywords
- anaerobic
- aerobic
- water
- effluent
- area
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 38
- 230000008878 coupling Effects 0.000 title claims abstract description 24
- 238000010168 coupling process Methods 0.000 title claims abstract description 24
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 24
- 239000002351 wastewater Substances 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 99
- 238000006243 chemical reaction Methods 0.000 claims abstract description 89
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 239000002002 slurry Substances 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 238000010992 reflux Methods 0.000 claims abstract description 23
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 12
- 239000010802 sludge Substances 0.000 claims abstract description 10
- 239000010815 organic waste Substances 0.000 claims abstract description 9
- 238000000855 fermentation Methods 0.000 claims abstract description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 8
- 230000001360 synchronised effect Effects 0.000 claims abstract description 8
- 238000005273 aeration Methods 0.000 claims description 31
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 21
- 239000001301 oxygen Substances 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims description 15
- 239000007787 solid Substances 0.000 claims description 14
- 238000009826 distribution Methods 0.000 claims description 12
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 8
- 238000005352 clarification Methods 0.000 claims description 4
- 239000003344 environmental pollutant Substances 0.000 claims description 4
- 231100000719 pollutant Toxicity 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 238000007865 diluting Methods 0.000 claims description 3
- 239000002910 solid waste Substances 0.000 claims description 3
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 20
- 230000001276 controlling effect Effects 0.000 description 9
- 210000003608 fece Anatomy 0.000 description 6
- 239000010871 livestock manure Substances 0.000 description 6
- 239000010865 sewage Substances 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 239000010813 municipal solid waste Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 102000019197 Superoxide Dismutase Human genes 0.000 description 1
- 108010012715 Superoxide dismutase Proteins 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003851 biochemical process Effects 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 231100000518 lethal Toxicity 0.000 description 1
- 230000001665 lethal effect Effects 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 235000003170 nutritional factors Nutrition 0.000 description 1
- 239000003895 organic fertilizer Substances 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- -1 superoxide anion free radical Chemical class 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
-
- 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
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
A method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling comprises the following steps: after the organic waste is crushed and screened, putting the filtered slurry into an anaerobic reaction unit, and performing anaerobic fermentation to obtain biogas and biogas slurry; introducing the anaerobic effluent into a solid-liquid separation unit for solid-liquid separation, and returning the separated biogas residues into the anaerobic reaction unit through a sludge reflux pump; the separated biogas slurry enters an aerobic reaction unit, and is subjected to a synchronous nitrification and denitrification process to remove nitrogen; and part of the effluent of the aerobic reaction unit flows back to the anaerobic reaction unit, is fully diluted and mixed with the organic waste raw slurry for anaerobic reaction, and the other part of the effluent enters the next treatment process or is discharged after reaching the standard. The anaerobic effluent enters a solid-liquid separation unit to separate suspended matters, the effluent enters an aerobic unit to control the DO value in the water body of the aerobic unit to finish denitrification, then the reflux ratio of the aerobic effluent is controlled to return to the anaerobic unit again, and the anaerobic biogas is subjected to cyclic reaction, so that the anaerobic biogas gas production rate is improved, and meanwhile, the quality of the aerobic effluent is higher.
Description
Technical Field
The invention relates to a method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling, belonging to the technical field of sewage treatment.
Background
Anaerobic reactors are generally preferentially adopted for the treatment and resource utilization of wastewater, but because reactants often contain a large amount of nitrogen-containing substances, a large amount of protein is converted and decomposed and a large amount of free ammonia nitrogen is released in the anaerobic fermentation process, so that the accumulation of ammonia nitrogen is caused, and the concentration of the ammonia nitrogen is often up to more than 2000 mg/L. According to research, an important nutritional factor influencing the growth of methanogens is ammonia nitrogen, and the ammonia nitrogen concentration is favorable for the anaerobic reaction when the ammonia nitrogen concentration is 50-200 mg/L; but when the ammonia nitrogen concentration reaches more than 2000mg/L, the gas production efficiency of methanogens can be obviously inhibited; when the ammonia nitrogen concentration reaches 5500mg/L, the methane output is reduced by 50 percent. In fact, the effect of producing biogas is not ideal due to the influence of high-concentration ammonia nitrogen in domestic kitchen (garbage) leachate treatment plants which are operated well at present.
In addition, according to the existing treatment examples of a large amount of kitchen (garbage) leachate, livestock and poultry manure and the like, the treatment of biogas slurry (containing biogas residues) after anaerobic treatment is also a great problem. In existing implementations, removal of high concentrations of nitrogen is often achieved by two stages of biochemistry. However, as effluent discharge standards become more and more strict, TN (total nitrogen content in water) is more and more limited, and in order to meet the discharge standards, a lengthy advanced treatment process section must be added, which is accompanied by the problems of high investment cost and operation cost.
Above two problems, on one hand hope to improve efficiency and output of anaerobically producing the natural pond gas, on the other hand, hope that the natural pond liquid that produces can environmental protection be handled and is dealt with, the result is to solve the problem of high concentration ammonia nitrogen, and this pollutant general solution is aerobic biochemical, also has therefore the researcher to propose the anaerobism aerobic coupling thinking of anaerobism supernatant circulation aerobic treatment, but has some technical problems:
DO (dissolved oxygen in water) problem: the oxygen demand of the aerobic process is generally larger, for example, the dissolved oxygen in the aerobic section of the A/O process is controlled to be more than 2.0mg/L, while in the anaerobic reaction, especially in the methanogenesis stage, the methanogen is lack of superoxide dismutase and O2Is very sensitive. If the effluent of the traditional aerobic biochemical process is directly circulated to the anaerobic unit, a large amount of O2Will react with some active groups in the methanogen cells, leading to the disintegration of important enzyme systems; while O is2The generated superoxide anion free radical can also cause cell lethal damage, and finally, the anaerobic reaction fails;
the problem of nitrate nitrogen: generally, the anaerobic environment is a water body environment with no nitrate nitrogen or a very small amount of nitrate nitrogen, but most of aerobic processes can only complete the conversion process from ammonia nitrogen to nitrate nitrogen, but cannot complete the conversion from nitrate nitrogen to nitrogen. That is, once the aerobic effluent returns to the anaerobic unit, a large amount of nitrate nitrogen is carried to directly destroy the anaerobic environment, so that heterotrophic bacteria in the reactor become dominant bacteria, the anaerobic reaction process is seriously influenced, and even the anaerobic reaction fails.
In addition, for sewage with high suspended matter content (solid content is more than 3%), after the anaerobic reaction, the fine particles and suspended matter in the mixed liquor are anaerobic products, and after the anaerobic products directly enter the aerobic biochemical tank, the mixed liquor can be mixed with other reactants and aerobic and facultative productsOxygen species compete for O2And the oxygen supply in the biochemical pond is insufficient, the aerobic environment is damaged, and the aerobic reaction efficiency is influenced, so that the content of suspended substances in the aerobic inlet water needs to be reduced.
Disclosure of Invention
The invention provides a method for treating high solid content organic wastewater by anaerobic-aerobic deep coupling, which overcomes the defects of the prior art, anaerobic effluent enters a solid-liquid separation unit to separate suspended matters, the effluent enters an aerobic unit to control DO value in the water body of the aerobic unit to complete denitrification, then the aerobic effluent returns to the anaerobic unit again by controlling reflux ratio, and the anaerobic biogas gas production rate is improved by circulating reaction, and meanwhile, the quality of the aerobic effluent is higher.
The technical scheme adopted by the invention for solving the technical problems is as follows:
the method for treating the organic wastewater with high solid content by anaerobic-aerobic deep coupling comprises the coupling use of an anaerobic treatment unit and an aerobic treatment unit, and the anaerobic-aerobic deep coupling treatment method comprises the following steps:
a. after organic waste is crushed and screened, collecting solid waste for additional treatment, putting the filtered slurry into an anaerobic reaction unit, fully mixing the slurry with anaerobic sludge which is added into the anaerobic reaction unit in advance, and performing anaerobic fermentation to obtain biogas and biogas slurry;
b. introducing effluent biogas slurry of anaerobic fermentation into a solid-liquid separation unit for solid-liquid separation, and returning separated biogas residues into the anaerobic reaction unit through a sludge reflux pump;
c. the separated biogas slurry enters an aerobic reaction unit, and is subjected to a synchronous nitrification and denitrification process to remove nitrogen;
d. and (3) refluxing part of the effluent of the aerobic reaction unit to the anaerobic reaction unit, fully diluting and mixing the effluent with the organic waste raw slurry, carrying out anaerobic reaction, and allowing the other part of the effluent to enter the next treatment process or be discharged after reaching the standard.
In the method for treating the organic wastewater with high solid content by anaerobic-aerobic deep coupling, the aerobic reaction unit is an integrated reactor, and the aerobic reaction process comprises the following steps:
s1, enabling the biogas slurry separated by the solid-liquid separation unit to enter a water inlet premixing area at the bottom of the aerobic reactor main body (3-1) through a water inlet point, wherein the water inlet point is arranged at the front end of the water inlet premixing area, controlling the dissolved oxygen concentration in the biogas slurry in the water inlet premixing area through a microporous aeration system at the bottom of the water inlet premixing area, enabling the biogas slurry to flow into a main aeration area, and controlling the dissolved oxygen concentration in the main aeration area through intermittent aeration in the main aeration area to carry out synchronous nitrification and denitrification reaction to degrade pollutants;
s2, pushing the degraded circulating water in the main aeration area to flow through a gas stripping area at the tail end, wherein the gas stripping area is arranged on the same side of the water inlet point, a water distribution facility is arranged behind the gas stripping area, the gas-stripped and pushed slurry-water mixed liquid is shunted through the water distribution facility, and a part of the gas-stripped and pushed slurry-water mixed liquid flows back to the water inlet premixing area to be mixed with new inlet water for circular reaction;
s3, enabling the other part of the muddy water mixed liquid shunted by the water distribution facility to upwards enter a backflow channel, enabling a part of mixed water in the backflow channel to ascend and pass through a clarification zone, enabling the discharged water to enter a water outlet channel after solid-liquid separation, discharging the discharged water, enabling the other part of mixed water to flow back to a main aeration zone, mixing the mixed water with the inlet water entering the main aeration zone through the water inlet premixing zone again, and carrying out circular reaction.
In the method for treating the organic wastewater with high solid content by anaerobic-aerobic deep coupling, in the step, the dissolved oxygen concentration in the water inlet premixing zone and the main aeration zone of the aerobic reaction unit is lower than 0.3 mg/L. The concentration of the dissolved oxygen can ensure that the nitrification and denitrification processes are synchronously carried out in the aerobic reaction, and the concentration of the dissolved oxygen in the aerobic effluent is lower than 0.2mg/L, thereby ensuring the gas production efficiency of the anaerobic reaction.
In the step d, the dissolved oxygen content in the effluent of the aerobic reaction unit is controlled to be less than or equal to 0.2mg/L, the nitrate nitrogen content is controlled to be less than or equal to 15mg/L, and the SS is controlled to be less than or equal to 50mg/L by the aeration device.
In the step d, the reflux ratio of aerobic effluent is controlled to be more than or equal to 100 percent.
In the method for treating the organic wastewater with the high solid content by anaerobic-aerobic deep coupling, in the step, the water distribution facility controls the reflux ratio of the mixed liquid which flows back to the water inlet premixing area to be less than or equal to 50%. Ensuring that the oxygen carried in the return water only occupies a small part of the oxygen provided by the microporous aeration facility in the water inlet premixing area.
In the method for treating the organic wastewater with the high solid content by anaerobic-aerobic deep coupling, the anaerobic reaction unit is a fully mixed reactor or a two-phase anaerobic reactor, the two-phase anaerobic reactor comprises an acid production reactor and a formaldehyde production reactor, and effluent of the aerobic reaction unit flows back to the formaldehyde production reactor.
According to the method for treating the organic wastewater with the high solid content by anaerobic-aerobic deep coupling, the solid-liquid separation unit is a centrifugal separator or an air floatation separation device. After solid-liquid separation is carried out on anaerobic effluent, suspended matters in the effluent are separated, and the separated effluent enters aerobic reaction, so that the influence of suspended particles on the aerobic reaction is avoided.
The invention has the beneficial effects that: the denitrification rate of the aerobic reaction unit is close to 100 percent, namely the ammonia nitrogen concentration of the effluent is close to zero, the ammonia nitrogen concentration in the anaerobic reactor can be controlled below 1000mg/L (ideally 200 mg/L) by controlling the reflux ratio of the aerobic effluent, the anaerobic reaction inhibition degree is lower under the ammonia nitrogen concentration, and the methane output is greatly improved.
Circularly coupling the anaerobic reaction unit and the aerobic reaction unit, and performing environment-friendly treatment on the biogas slurry: after the anaerobic reaction unit degrades a large amount of BOD, the aerobic reaction unit removes the residual BOD and ammonia nitrogen, and the effluent can reach the first-level A standard and even has better water quality.
And thirdly, by controlling the dissolved oxygen in the aerobic reaction stage to be less than or equal to 0.3mg/L and synchronously carrying out the nitrification and denitrification processes, the DO of the effluent of the aerobic reaction unit is extremely low and is always controlled to be less than 0.2mg/L (generally speaking, the DO in the anaerobic environment is less than 0.2 mg/L), and the backflow mixed liquid is ensured not to damage the anaerobic environment.
Fourthly, because the aerobic nitrification, the aerobic BOD oxidation and the anoxic denitrification are carried out in parallel in the aerobic reaction unit, the high-concentration ammonia nitrogen is finally converted into N2The content of nitrate nitrogen in the aerobic effluent reflux is extremely low and is basically kept below 15mg/L, and the anaerobic reaction is avoidedShould have little effect.
The circulation reflux ratio of the aerobic mixed liquor can be automatically controlled and adjusted by an electric adjusting valve on a reflux pipeline, so that the COD value of the slurry in the anaerobic reactor is flexibly adjusted, the impact load resistance of an anaerobic reaction unit is improved, and the anaerobic reactor is particularly suitable for treating organic wastes with high concentration and high water fluctuation change.
The anaerobic effluent has strong biodegradability, higher COD and high ammonia nitrogen, and is particularly suitable for subsequent aerobic denitrification: firstly, a carbon source is not required to be added, so that the aeration cost and the medicament cost are saved; secondly, most of organic nitrogen is converted into ammonia nitrogen in the anaerobic stage, so that the nitrification and denitrification processes are accelerated, and the aerobic biochemical efficiency is improved.
And seventhly, in the high solid content anaerobic process, the anaerobic effluent biogas slurry contains a large amount of fine particles and suspended substances, the SS removal rate is high through the solid-liquid separation unit, and the aerobic biochemical influent SS is ensured to be less than or equal to 200 mg/L.
Drawings
The invention is further described below with reference to the accompanying drawings.
FIG. 1 is a schematic diagram of the overall structure of an anaerobic reactor of the present invention;
FIG. 2 is a schematic diagram of the overall apparatus structure of an anaerobic reactor which is a two-phase anaerobic reactor;
FIG. 3 is a schematic structural diagram of an aerobic integrated reactor.
In the figure: 1. an anaerobic reaction unit; 1-1, an acid production reactor; 1-2, a formaldehyde production reactor; 2. a solid-liquid separation unit; 3. an aerobic reaction unit; 3-1, an aerobic reactor main body; 3-2, a water inlet premixing area; 3-3, water inlet points; 3-4, a main aeration zone; 3-5, a gas stripping zone; 3-6, water distribution facilities; 3-7, a backflow channel; 3-8, a clarification zone; 3-9, a water outlet channel; 4. a sludge reflux pump.
Detailed Description
The invention utilizes the coupling of an anaerobic reaction unit and an aerobic reaction unit, a solid-liquid separation unit is arranged between the anaerobic reaction unit and the aerobic reaction unit, after the suspended matters in the effluent water after the anaerobic reaction are separated, the separated effluent water enters the aerobic reaction unit, the nitrification and denitrification reactions are synchronously carried out by controlling the concentration of dissolved oxygen in the aerobic reaction unit to be lower than 0.3mg/L, nitrate nitrogen in the water is converted into nitrogen to finish denitrification, then the aerobic effluent water enters the anaerobic reaction unit again to be mixed with sewage raw water, the reflux ratio (the reflux ratio is the ratio of the reflux water quantity to the treated water quantity) is controlled, an electric regulating valve is arranged on a reflux pipeline, the valve is connected with an internet control system, the valve can be automatically opened/closed or the flow of the valve is increased/decreased according to the signal feedback, so that the concentration of ammonia nitrogen in the anaerobic reaction unit is controlled to be lower than 1000mg/L, the inhibition degree of the anaerobic reaction is reduced, and the biogas yield is improved.
The anaerobic-aerobic deep coupling treatment method comprises the following steps:
a. after organic waste is crushed and screened, collecting solid waste for additional treatment, putting the filtered slurry into an anaerobic reaction unit 1, wherein the anaerobic reaction unit 1 is a fully mixed reactor or a two-phase anaerobic reactor, and fully mixing the slurry with anaerobic sludge which is added into the anaerobic reaction unit in advance and carrying out anaerobic fermentation to obtain biogas and biogas slurry;
b. introducing effluent biogas slurry of anaerobic fermentation into a solid-liquid separation unit 2 for solid-liquid separation, and returning separated biogas residues into the anaerobic reaction unit 1 through a sludge reflux pump 4;
c. the separated biogas slurry enters an aerobic reaction unit 3, is subjected to a synchronous nitrification and denitrification process, is subjected to nitrogen removal, and is controlled to have dissolved oxygen content less than or equal to 0.2mg/L, nitrate nitrogen content less than or equal to 15mg/L and SS content less than or equal to 50mg/L in aerobic effluent;
d. and (3) refluxing part of the effluent of the aerobic reaction unit 3 to the anaerobic reaction unit, controlling the reflux ratio to be more than or equal to 100%, fully diluting and mixing the effluent with the organic waste raw slurry, carrying out anaerobic reaction again, and allowing the other part of the effluent to enter the next treatment process or be discharged after reaching the standard.
The aerobic reaction process comprises the following steps:
s1, enabling the biogas slurry separated by the solid-liquid separation unit 2 to enter a water inlet premixing area 3-2 at the bottom of the aerobic reactor main body 3-1 through a water inlet point, enabling the water inlet point 3-3 to be arranged at the front end of the water inlet premixing area 3-2, controlling the dissolved oxygen concentration in the biogas slurry in the water inlet premixing area through a microporous aeration system at the bottom of the water inlet premixing area, enabling the biogas slurry to flow into a main aeration area 3-4, controlling the dissolved oxygen concentration in the main aeration area through intermittent aeration in the main aeration area, and performing synchronous nitrification and denitrification to degrade pollutants;
s2, pushing the degraded circulating water in the main aeration area to flow through a gas stripping area 3-5 at the tail end, wherein the gas stripping area is arranged on the same side of the water inlet point, a water distribution facility 3-6 is arranged behind the gas stripping area, the water-sludge mixed liquid subjected to gas stripping and flow pushing is shunted through the water distribution facility 3-6, and a part of the water-sludge mixed liquid flows back to the water inlet premixing area to be mixed with new inlet water for circular reaction;
s3, enabling the other part of the muddy water mixed liquid shunted by the water distribution facility to upwards enter a backflow channel 3-7, enabling one part of mixed water in the backflow channel to ascend through a clarification zone 3-8, enabling the discharged water to enter a water outlet channel 3-9 after solid-liquid separation, discharging the discharged water, enabling the other part of mixed water to flow back to a main aeration zone, mixing the mixed water with the inlet water entering the main aeration zone through the water inlet premixing zone again, and performing circular reaction.
13500 breeding sows in a certain pig farm, fattening 150000 storing the sows, wherein the manure cleaning mode is a water soaking manure mode, the discharge amount of manure sewage Q =2000m and the year/d is according to the raw water indexes: COD is less than or equal to 18000mg/L, TKN is less than or equal to 1300mg/L, TS is less than 4%, effluent COD is less than 150mg/L, ammonia nitrogen is less than 100mg/L, and energy utilization requirements are met. The following process flow is designed according to project requirements: a solid-liquid separation unit, an anaerobic reaction unit and an aerobic reaction unit. The solid-liquid separation unit comprises a grid, a slag separation tank and a solid-liquid separator, the anaerobic treatment unit adopts an IC reactor, and the aerobic treatment unit adopts a synchronous nitrification and denitrification process.
S1: the manure sequentially passes through a grating, a slag separation tank and a solid-liquid separator, floating materials, small particles, suspended matters and the like in the sewage are intercepted and separated, and the manure is stacked after being collected to obtain an organic fertilizer;
s2: the mixed solution obtained from S1 is put into an IC reactor, and most of organic substances are degraded anaerobically;
s3: the biogas obtained in the step S2 is combusted to generate power to be needed by the power of a pig farm;
s4: and (3) treating the effluent obtained in the step (S1) in an aerobic biochemical tank, wherein the effluent reaches the standard and simultaneously reflows according to 100 percent.
Claims (5)
1. A method for treating organic wastewater with high solid content by anaerobic-aerobic deep coupling comprises the coupling use of an anaerobic treatment unit and an aerobic treatment unit, and is characterized in that: the anaerobic-aerobic deep coupling treatment method comprises the following steps:
a. after organic waste is crushed and screened, collecting solid waste for additional treatment, putting the filtered slurry into an anaerobic reaction unit (1), fully mixing the slurry with anaerobic sludge which is added into the anaerobic reaction unit in advance, and performing anaerobic fermentation to obtain biogas and biogas slurry;
b. introducing effluent biogas slurry of anaerobic fermentation into a solid-liquid separation unit (2) for solid-liquid separation, and returning separated biogas residues into the anaerobic reaction unit (1) through a sludge reflux pump (4);
c. the separated biogas slurry enters an aerobic reaction unit (3) and is subjected to a synchronous nitrification and denitrification process to remove nitrogen;
d. refluxing part of the effluent of the aerobic reaction unit (3) to an anaerobic reaction unit, fully diluting and mixing the effluent with the organic waste raw slurry, carrying out anaerobic reaction, and allowing the other part of the effluent to enter the next treatment process or be discharged after reaching the standard;
in the step d, the content of dissolved oxygen in the effluent of the aerobic reaction unit (3) is controlled to be less than or equal to 0.2mg/L, the content of nitrate nitrogen is controlled to be less than or equal to 15mg/L, and SS is controlled to be less than or equal to 50mg/L by an aeration device;
in the step d, controlling the aerobic effluent reflux ratio to be more than or equal to 100 percent;
the aerobic reaction unit (3) is an integrated reactor, and the aerobic reaction process comprises the following steps:
s1, enabling the biogas slurry separated by the solid-liquid separation unit (2) to enter a water inlet premixing area (3-2) at the bottom of the aerobic reactor main body (3-1) through a water inlet point, enabling the water inlet point (3-3) to be arranged at the front end of the water inlet premixing area (3-2), controlling the dissolved oxygen concentration in the biogas slurry in the water inlet premixing area through a microporous aeration system at the bottom of the water inlet premixing area, enabling the biogas slurry to flow into a main aeration area (3-4), controlling the dissolved oxygen concentration in the main aeration area through intermittent aeration in the main aeration area, and performing synchronous nitrification and denitrification to degrade pollutants;
s2, pushing the degraded circulating water in the main aeration area to flow through a gas stripping area (3-5) at the tail end, wherein the gas stripping area is arranged at the same side of the water inlet point, a water distribution facility (3-6) is arranged behind the gas stripping area, the gas-stripped mud-water mixed liquid is divided through the water distribution facility (3-6), and part of the gas-stripped mud-water mixed liquid flows back to the water inlet premixing area to be mixed with new inlet water for circular reaction;
s3, enabling the other part of muddy water mixed liquid shunted by the water distribution facility to upwards enter a backflow channel (3-7), enabling one part of mixed water in the backflow channel to ascend through a clarification area (3-8), enabling outlet water to enter a water outlet channel (3-9) after solid-liquid separation, enabling the outlet water to be discharged outwards, enabling the other part of mixed water to flow back to a main aeration area, enabling the other part of mixed water to be mixed with inlet water entering the main aeration area through a water inlet premixing area again, and carrying out circular reaction.
2. The anaerobic-aerobic deep coupling treatment method for organic wastewater with high solid content as claimed in claim 1, characterized in that: in the step S1, the dissolved oxygen concentration in the water inlet premixing area and the main aeration area of the aerobic reaction unit (3) is lower than 0.3 mg/L.
3. The anaerobic-aerobic deep coupling treatment method for organic wastewater with high solid content as claimed in claim 2, characterized in that: in the step S2, the water distribution facility (3-6) controls the reflux ratio of the mixed liquid refluxed into the water inlet premixing area (3-2) to be less than or equal to 50%.
4. The anaerobic-aerobic deep coupling treatment method for organic wastewater with high solid content as claimed in claim 3, characterized in that: the anaerobic reaction unit (1) is a fully mixed reactor or a two-phase anaerobic reactor, the two-phase anaerobic reactor comprises an acid production reactor (1-1) and a formaldehyde production reactor (1-2), and the effluent of the aerobic reaction unit (3) flows back to the formaldehyde production reactor (1-2).
5. The anaerobic-aerobic deep coupling treatment method for organic wastewater with high solid content as claimed in claim 4, characterized in that: the solid-liquid separation unit (2) is a centrifugal separator or an air floatation separation device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911193092.9A CN110790378B (en) | 2019-11-28 | 2019-11-28 | Method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911193092.9A CN110790378B (en) | 2019-11-28 | 2019-11-28 | Method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110790378A CN110790378A (en) | 2020-02-14 |
| CN110790378B true CN110790378B (en) | 2022-04-19 |
Family
ID=69446808
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911193092.9A Active CN110790378B (en) | 2019-11-28 | 2019-11-28 | Method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110790378B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112011441A (en) * | 2020-09-08 | 2020-12-01 | 重庆市环卫集团有限公司 | Dry anaerobic digestion system for urban organic garbage |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5061368A (en) * | 1989-02-16 | 1991-10-29 | Hitachi Plant Engineering & Construction Co., Ltd. | System for treating waste water by nitrification |
| CN105565493A (en) * | 2015-12-14 | 2016-05-11 | 安徽国祯环保节能科技股份有限公司 | Device and method for advanced denitrification of early landfill leachate through synchronous nitrification/denitrification treatment |
| CN106186313A (en) * | 2015-05-07 | 2016-12-07 | 易百皓源（北京）环保科技有限公司 | For improveing integrated sewage disposal pond and the sewage water treatment method of AO |
| CN107416977A (en) * | 2017-09-14 | 2017-12-01 | 广州沼能环保科技有限责任公司 | A kind of biogas slurry treatment method |
| CN109305725A (en) * | 2018-11-23 | 2019-02-05 | 恩格拜（武汉）生态科技有限公司 | Biochemical sewage treatment process |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004528163A (en) * | 2001-02-23 | 2004-09-16 | ヴイ．エイ．アイ． リミテッド | Method and apparatus for biological treatment of wastewater |
-
2019
- 2019-11-28 CN CN201911193092.9A patent/CN110790378B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5061368A (en) * | 1989-02-16 | 1991-10-29 | Hitachi Plant Engineering & Construction Co., Ltd. | System for treating waste water by nitrification |
| CN106186313A (en) * | 2015-05-07 | 2016-12-07 | 易百皓源（北京）环保科技有限公司 | For improveing integrated sewage disposal pond and the sewage water treatment method of AO |
| CN105565493A (en) * | 2015-12-14 | 2016-05-11 | 安徽国祯环保节能科技股份有限公司 | Device and method for advanced denitrification of early landfill leachate through synchronous nitrification/denitrification treatment |
| CN107416977A (en) * | 2017-09-14 | 2017-12-01 | 广州沼能环保科技有限责任公司 | A kind of biogas slurry treatment method |
| CN109305725A (en) * | 2018-11-23 | 2019-02-05 | 恩格拜（武汉）生态科技有限公司 | Biochemical sewage treatment process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110790378A (en) | 2020-02-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107010788B (en) | Large-scale pig farm cultivation wastewater treatment system and method | |
| CN100371270C (en) | Combined treatment process for manioc producing effluent | |
| CN110790379A (en) | Method for treating high-concentration organic wastewater by anaerobic-aerobic deep coupling | |
| CN107055813B (en) | Anaerobic sewage treatment device and process | |
| CN100534928C (en) | Short-path deep biological denitrogenation method for city garbage percolate | |
| CN203878024U (en) | Wastewater treatment system for culture farm | |
| CN101786730B (en) | Method and equipment for cross backflow two-stage double-expansion granular sludge treatment of coking wastewater | |
| CN103922538B (en) | Livestock and poultry breeding wastewater treatment method | |
| CN101935136B (en) | Zero energy consumption low sludge yield municipal sewage dephosphorization and denitrification treatment method | |
| CN105819567A (en) | Self-circulation anaerobic reactor | |
| CN101805096B (en) | Method for treating rubbish percolates of different times for deep denitrification by using bipolar USAB+A/O+SBR process | |
| CN107840550B (en) | Method for treating garbage leachate | |
| CN114716112A (en) | Rural sewage treatment system and process | |
| CN111908618A (en) | High ammonia-nitrogen concentration effluent disposal system | |
| CN110790378B (en) | Method for treating high-solid-content organic wastewater by anaerobic-aerobic deep coupling | |
| KR100274534B1 (en) | Nitrogen and phosphorus removal methods with using fermented organic wastes | |
| CN111592104A (en) | Short-range efficient biological treatment device and treatment method for kitchen waste digestive juice | |
| CN114634244A (en) | Methane fermentation coupling integrated denitrification system and process for livestock and poultry manure wastewater | |
| CN212712945U (en) | High ammonia-nitrogen concentration effluent disposal system | |
| CN214829778U (en) | Black water and grey water recycling treatment system for rural areas | |
| CN216377647U (en) | High-efficient pulse water distribution anaerobism sludge denitrification reaction unit | |
| CN2931465Y (en) | Apparatus of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique | |
| CN114149155A (en) | Urine extraction wastewater treatment and nitrogen and phosphorus resource recovery method | |
| KR100714825B1 (en) | Method for treating sewage and high organic loading wastewater by anaerobic/oxic process with membrane and biological aerated filter | |
| CN112142254A (en) | High-concentration nitrogen-containing leather sewage treatment method and device based on composite microbial inoculum |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A method of anaerobic aerobic deep coupling treatment for high solid content organic wastewater Granted publication date: 20220419 Pledgee: Guanggu Branch of Wuhan Rural Commercial Bank Co.,Ltd. Pledgor: ENGELBART (WUHAN) ECOLOGICAL TECHNOLOGY Co.,Ltd. Registration number: Y2024980004614 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |