CN111892240A - Method for treating amino acid extraction wastewater by using hydrated lime to replace neutralizer and flocculant - Google Patents
Method for treating amino acid extraction wastewater by using hydrated lime to replace neutralizer and flocculant Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 94
- 238000000034 method Methods 0.000 title claims abstract description 46
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 title claims abstract description 35
- 239000000920 calcium hydroxide Substances 0.000 title claims abstract description 35
- 235000011116 calcium hydroxide Nutrition 0.000 title claims abstract description 35
- 229910001861 calcium hydroxide Inorganic materials 0.000 title claims abstract description 35
- 150000001413 amino acids Chemical class 0.000 title claims abstract description 12
- 238000000605 extraction Methods 0.000 title claims abstract description 12
- 230000003647 oxidation Effects 0.000 claims abstract description 21
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 21
- 230000008569 process Effects 0.000 claims abstract description 21
- 239000008394 flocculating agent Substances 0.000 claims abstract description 14
- 238000005189 flocculation Methods 0.000 claims abstract description 7
- 230000016615 flocculation Effects 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 230000003301 hydrolyzing effect Effects 0.000 claims abstract description 5
- 230000003311 flocculating effect Effects 0.000 claims abstract description 4
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 40
- 239000010802 sludge Substances 0.000 claims description 35
- 238000004062 sedimentation Methods 0.000 claims description 16
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 14
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 13
- 239000006228 supernatant Substances 0.000 claims description 13
- 238000003756 stirring Methods 0.000 claims description 10
- 230000009615 deamination Effects 0.000 claims description 9
- 238000006481 deamination reaction Methods 0.000 claims description 9
- 239000002699 waste material Substances 0.000 claims description 9
- 230000020477 pH reduction Effects 0.000 claims description 8
- 239000000292 calcium oxide Substances 0.000 claims description 7
- 235000012255 calcium oxide Nutrition 0.000 claims description 7
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 7
- 238000000354 decomposition reaction Methods 0.000 claims description 6
- 230000007062 hydrolysis Effects 0.000 claims description 5
- 238000006460 hydrolysis reaction Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 230000003472 neutralizing effect Effects 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 239000013589 supplement Substances 0.000 claims description 3
- 238000010979 pH adjustment Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 7
- 239000010865 sewage Substances 0.000 abstract description 4
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 230000001376 precipitating effect Effects 0.000 abstract description 3
- 230000007547 defect Effects 0.000 abstract description 2
- 239000003153 chemical reaction reagent Substances 0.000 abstract 2
- 238000009776 industrial production Methods 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 21
- 229940024606 amino acid Drugs 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 7
- 235000011121 sodium hydroxide Nutrition 0.000 description 7
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 5
- 229910001424 calcium ion Inorganic materials 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000005273 aeration Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 230000001112 coagulating effect Effects 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- AGPKZVBTJJNPAG-WHFBIAKZSA-N L-isoleucine Chemical compound CC[C@H](C)[C@H](N)C(O)=O AGPKZVBTJJNPAG-WHFBIAKZSA-N 0.000 description 1
- 229930182844 L-isoleucine Natural products 0.000 description 1
- 241000108664 Nitrobacteria Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229960000310 isoleucine Drugs 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229920002401 polyacrylamide Polymers 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
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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
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- 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
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- 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]
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention belongs to the field of amino acid extraction wastewater treatment, and particularly relates to a method for treating amino acid extraction wastewater by using hydrated lime to replace a neutralizer and a flocculating agent. The method comprises the following steps: 1. adjusting pH and deaminating; 2. flocculating and precipitating; 3. anaerobic treatment; 4. hydrolyzing and acidifying; 5. contact oxidation; 6. separating mud and water; 7. the method can achieve the effect of sewage pretreatment, and can treat the wastewater to reach the discharge standard through subsequent biochemical advanced treatment. According to the method, one reagent is used for simultaneously replacing two reagents which have completely different functions and are high in price, so that the wastewater treatment cost is greatly reduced; and effectively makes up the defect of unstable flocculation in the use process of the flocculating agent, and is more convenient and faster to operate. Is in line with green and economic, and is suitable for industrial production.
Description
Technical Field
The invention relates to the field of wastewater treatment, in particular to a method for treating amino acid extraction wastewater by using hydrated lime to replace a neutralizer and a flocculating agent.
Background
A large amount of acidic high ammonium salt wastewater is generated in the production process of L-isoleucine, and the common treatment method comprises the steps of pretreating by physical and chemical methods, then performing subsequent biochemical advanced treatment to reach the effluent discharge standard, and then discharging the effluent to a regional treatment place for further treatment.
The most common pretreatment method at present is to use liquid caustic soda (NaOH solution) to adjust the pH of the wastewater, blow off ammonia, mix with general wastewater, adjust the pH to alkalinity again with liquid caustic soda, and then add special inorganic and organic flocculants according to a certain proportion under sufficient stirring, thereby adsorbing and precipitating most of solid particles and organic matters in the wastewater, thus greatly reducing the organic matters and related biochemical indexes in the wastewater, and reducing the burden of subsequent biochemical deep treatment. However, because the price of both the liquid caustic soda and the flocculant is relatively high, according to statistics, the treatment capacity of 1800 tons per day needs to consume 25 tons of liquid caustic soda and 200KG of composite flocculant, which is 2.6 ten thousand yuan; meanwhile, the flocculating agent is often influenced by stirring and flow velocity in the process of adding the flocculating agent, so that the condition of unstable flocculating effect can occur, and the process stability is poor.
Disclosure of Invention
The invention provides a method for treating amino acid extraction wastewater by using hydrated lime to replace a neutralizer and a flocculating agent, which aims to solve the technical problems, and can reduce flocculation consumption, improve the stability of flocculation effect, stabilize process and reduce wastewater treatment cost.
The technical scheme adopted by the invention is as follows:
a process for treating amino acid extraction wastewater using slaked lime to replace neutralizing agents and flocculants, the process comprising the steps of:
s1, pH adjustment and deamination: the high ammonia nitrogen wastewater enters a high ammonia nitrogen wastewater adjusting tank, slaked lime is added in batches under stirring, the pH value of the wastewater is adjusted to be more than 11, the wastewater enters a deamination tower for blow-off, the blow-off wastewater and the common wastewater obtain mixed wastewater, and the mixed wastewater is precipitated to obtain supernatant;
s2, flocculating and settling: the supernatant obtained in the step S1 enters a flocculation sedimentation tank, and is further precipitated through a physical separation system to obtain supernatant and waste mud;
s3, anaerobic treatment: the supernatant obtained in the step S2 is introduced into an anaerobic reactor (anaerobic expanded granular sludge bed) to be anaerobically decomposed;
s4, hydrolysis acidification: the wastewater after anaerobic treatment in the step S3 enters a hydrolytic acidification tank for aerobic decomposition;
s5, contact oxidation: the wastewater treated in the step S4 enters a biological contact oxidation tank for biochemical treatment, and indexes are controlled;
s6, separating mud from water: the wastewater treated by the contact oxidation in the step S5 is rapidly separated in a secondary sedimentation tank through a physical device, the sludge deposited to the bottom supplements the sludge reduced in the previous process, and the redundant part is deslimed at a desliming post.
S7, emission up to standard: and (4) discharging the wastewater to a regional treatment plant through an online monitoring discharge port for further harmless treatment.
Preferably, in step S1, the indexes of the high ammonia nitrogen wastewater are: ammonia nitrogen 6000-11000 mg/L, COD: 500-1000 mg/L, pH 2-4.
Preferably, in step S1, the COD of the general wastewater is: 4000mg/L, ammonia nitrogen: 150mg/L, pH: 2-4, the indexes of the mixed wastewater are as follows: COD: 2000-4000 mg/L of ammonia nitrogen and 500-1000 mg/L of ammonia nitrogen.
Preferably, in step S1, after the pH of the wastewater is adjusted to be above 11, the temperature of the wastewater is increased to 40-50 ℃, and then the wastewater enters a deamination tower for stripping.
Preferably, in the step S1, the mixed wastewater is subjected to precipitation treatment after being supplemented with slaked lime to control the pH value 7-9. The subsequent process requires that the living range pH of the active bacteria is 7-9.
Preferably, in the step S1, the slaked lime may be replaced by quick lime.
Preferably, the step S2 further comprises separating the waste sludge deposited at the bottom, and pumping the waste sludge to a desliming station for desliming.
Preferably, the COD is reduced by at least 50% by the anaerobic treatment of step S3; through step S4, aerobic decomposition, wastewater index: COD is less than 600mg/L, and ammonia nitrogen is less than or equal to 200 mg/L; after the contact oxidation of step S5, the wastewater index: COD: 150-200mg/L and ammonia nitrogen less than or equal to 10 mg/L.
Preferably, in step S5, the bio-contact oxidation pond is a bio-contact oxidation pond consisting of 5 galleries, and the bio-contact oxidation pond is biochemically processed and gradually pushed to gallery 5 from gallery 1, and aeration regulation is additionally installed in each gallery.
Preferably, after the treatment of step S6, the clear liquid in the secondary sedimentation tank can reach COD less than or equal to 150mg/L and NH3-N≤5mg/L，pH6～9。
Preferably, in the step S4, the weight of the product is 2KG/10m3Sodium carbonate is added into the waste water in a flowing mode.
The invention has the following beneficial effects:
1. the invention finds a single additive, namely hydrated lime, which can simultaneously replace liquid caustic soda and a flocculating agent. Tests show that the cost of alkali for adjusting pH can be reduced by about 80% because the same amount of waste water is treated, the amount of liquid alkali is 1/4 and the price of hydrated lime is 1/2 of liquid alkali. Moreover, in the test process, the addition of the hydrated lime shows that the wastewater is static after the pH is adjusted, so that the obvious sedimentation effect is achieved. Further, the method tries to directly settle without adding a special flocculating agent and then enters the next working procedure, and no obvious adverse effect is found on the subsequent treatment. In view of this, cancel the use of pretreatment process flocculating agent, can save flocculating agent expense nearly 0.3 ten thousand yuan again a day, this has important meaning to reduction in production cost. Meanwhile, due to the good dispersion when the hydrated lime is added, the precipitation effect is less influenced by the stirring strength and the flow velocity, the process stability is greatly improved, the problems existing in the prior art are well solved, and the single-day sewage treatment cost is as follows: using 25 tons of liquid alkali every day200KG of composite flocculant, which is 2.6 ten thousand yuan for Renminbi; at present, 10 tons of hydrated lime is used every day, which is 0.6 ten thousand yuan in RMB. Can save more than 2 ten thousand yuan; the index of the wastewater treated by the adjusted process after being treated by the secondary sedimentation tank is far lower than the discharge standard, so the wastewater can be discharged without advanced treatment in the biological aerated filter. By the invention, the clear liquid in the secondary sedimentation tank can reach COD less than or equal to 150mg/L and NH3N is less than or equal to 5mg/L, pH is 6-9, and is far lower than the third-level emission standard: COD less than or equal to 500mg/L, NH3N is less than or equal to 32mg/L, SS is less than or equal to 280mg/L, and pH is 6-9. In the step S2, the supernatant obtained in the step S1 enters a flocculation sedimentation tank, is further adsorbed and precipitated by a physical separation system to obtain supernatant and waste sludge, and thoroughly removes large particles and a part of organic matters, and then the particles (waste sludge) separated and deposited at the bottom are pumped to a desliming station for desliming.
2. In the step S1, the pH value of the wastewater is adjusted to be more than 11, the temperature of the wastewater is increased to 40-50 ℃, and then the wastewater enters a deamination tower for stripping. As the pH value reaches more than 11 and the temperature is 40-50 ℃, the ammonia molecules are easy to blow out, the air stripping efficiency is ensured, and the higher the air stripping efficiency is, the lower the cost is). In addition, under the condition of not heating in the early stage of the slaked lime experiment, the pH value can not reach the required 11 all the time due to the limited solubility of the slaked lime, and then the slaked lime is improved, heated while stirring, and in a small amount of feeding way,
3. in the test process, by comparing two schemes of quick lime and hydrated lime, the quick lime needs 15% more than the hydrated lime to reach the required pH value, and 6KG hydrated lime or 7KG quick lime is needed for normally treating one ton of wastewater. In addition, the use of quicklime can deposit more solid slag in the regulating tank, and the solid slag is difficult to clean. The effective component of the hydrated lime can reach more than 92 percent, the content of the quicklime is 82 percent, and the price is only 5 percent different, so the hydrated lime has better effect and lower cost when being selected.
4. Step S4 hydrolytic acidification: and the macromolecular organic matters are further acidified and decomposed into biochemical micromolecular nutrient substances which are beneficial to the absorption of the activated sludge, and a part of COD is consumed by the sludge.
5. The addition of hydrated lime is mainly used for replacing liquid caustic soda to adjust the pH value to the required range, so that the cost can be saved. In addition, the applicant also finds that after the pH value is adjusted by using the hydrated lime, more calcium ions enter the subsequent treatment process, the most important process for degrading COD and ammonia nitrogen in sewage treatment is in the contact oxidation pond, and almost 95% of ammonia nitrogen is treated by nitrobacteria and denitrifying bacteria in the activated sludge in the contact oxidation pond. After the hydrated lime is continuously used, more and more calcium ions are enriched in the contact oxidation pond, so that the activity of the sludge is reduced until the sludge is lost, which is shown in that the sludge in the contact oxidation pond is whitened (normally grey brown), the sludge is not fluffy, the sludge is heavy, the effluent index is continuously increased, the treatment capacity is greatly reduced, and the whole sewage treatment system can be seriously crashed. In order to solve the defect, a small amount of sodium carbonate solution is ingeniously added into a hydrolysis tank of the previous process step of entering a contact oxidation tank, and carbonate ions in the sodium carbonate solution are combined with calcium ions to block the calcium ions and prevent the calcium ions from entering the contact oxidation tank. After this measure, the contact oxidation basin capacity can be kept essentially unaffected at the best level after continuous uninterrupted use of slaked lime. The usage amount of the sodium carbonate is 300-400 KG/day, and the equivalent amount is more than 1000 Yuan.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a raw water state diagram of amino acid extraction wastewater;
FIG. 3 is a water quality state diagram of amino acid extraction wastewater added with flocculant (polyacrylamide);
FIG. 4 is a water quality state diagram of amino acid extraction wastewater added with slaked lime in example 1.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and specific embodiments, so that the technical solutions and advantages thereof will be more clearly understood. It is to be understood that the examples and drawings are provided solely for the purposes of illustration and description and are not intended as a definition of the limits of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
A process for treating amino acid extraction wastewater using slaked lime to replace neutralizing agents and flocculants, the process comprising the steps of:
1. high ammonia nitrogen wastewater (ammonia nitrogen 6000-11000 mg/L, COD: 500-1000 mg/L, pH: 2-4) enters a high ammonia wastewater adjusting tank, slaked lime is added in batches under stirring, the pH value of the wastewater is adjusted to be more than 11, meanwhile, steam raises the temperature of the wastewater to be more than 40 ℃, the wastewater enters a deamination tower to be blown off, ammonia nitrogen escapes in the form of ammonia gas and is absorbed for other use, the ammonia nitrogen of the wastewater after being blown off can be reduced to be less than 3000 mg/L, and the wastewater is stirred and mixed with general wastewater (COD: about 4000mg/L, ammonia nitrogen: about 150mg/L, pH: 2-4) in proportion in the comprehensive adjusting tank, so that the index of the wastewater entering the next link is controlled to be COD: 2000-4000 mg/L of ammonia nitrogen and 500-1000 mg/L of ammonia nitrogen, and controlling the PH 7-9 by adding a certain amount of slaked lime and precipitating at the same time.
2. The supernatant containing a small amount of solid matters enters a flocculation sedimentation tank, is further adsorbed and precipitated through a physical separation system to thoroughly remove large particles and partial organic matters, and then the particles (waste mud) separated and deposited at the bottom are pumped to a desliming station for desliming.
3. The supernatant enters an EGSB (anaerobic expanded granular sludge bed), flows into the EGSB from the bottom to be mixed and contacted with sludge, and microorganisms (anaerobic activated sludge) decompose organic matters to reduce COD by about 50 percent.
4. The wastewater after anaerobic treatment enters a facultative tank-a hydrolysis acidification tank, and is further acidified and decomposed into micromolecular nutrients which can be biochemically absorbed by activated sludge, and simultaneously consumes a part of COD, the wastewater index is controlled to be about 500mg/L and 100mg/L of ammonia nitrogen, and then the next procedure is carried out.
5. Entering a biological contact oxidation pond consisting of 5 galleries for biochemical treatment, gradually flowing from the gallery 1 to the gallery 5, adding aeration adjustment to each gallery in the interval, and finely adjusting according to the change of PH, dissolved oxygen, sludge concentration, sludge amount, sludge color, COD, ammonia nitrogen and the like of each gallery according to the detection parameters of each gallery to control the tail end water outlet index COD of the gallery 5 to be about 150mg/L and the ammonia nitrogen to be below 5 mg/L.
6. The biochemically treated wastewater contains a certain amount of sludge, the sludge is quickly separated in a secondary sedimentation tank through a physical device, the sludge deposited to the bottom supplements the sludge reduced in the previous process, and the redundant sludge is deslimed at a desliming post.
7. Through the treatment of all the steps, the clear liquid in the secondary sedimentation tank can reach COD less than or equal to 150mg/L and NH3N is less than or equal to 5mg/L, pH is 6-9, and is far lower than the third-level emission standard: COD less than or equal to 500mg/L, NH3N is less than or equal to 32mg/L, SS is less than or equal to 280mg/L, and pH is 6-9. And (4) discharging the wastewater to a regional treatment plant through an online monitoring discharge port for further harmless treatment.
Example 1
1. Adding slaked lime into a high ammonia-nitrogen wastewater regulating tank by times under stirring, regulating the pH value of high ammonia-nitrogen wastewater (8200 mg/L ammonia nitrogen, COD: 600mg/L and pH: 3) to 12, starting steam to increase the temperature to 42 ℃, entering a deamination tower, blowing off until the ammonia nitrogen is 2500, stopping blowing off, putting the high ammonia-nitrogen wastewater into a comprehensive regulating tank, stirring and mixing with general wastewater (COD: 4100mg/L, ammonia nitrogen: 150mg/L and pH: 2) to form mixed wastewater with the COD of 2800mg/L and the ammonia nitrogen of 500mg/L, wherein the pH is about 8, and stopping stirring and naturally settling.
2. The supernatant with a small amount of precipitate enters a coagulating sedimentation tank, is filtered by a grating and a filter screen, flows into the coagulating sedimentation tank from the bottom of an EGSB (anaerobic expanded granular sludge bed) to be mixed and contacted with sludge, and microorganisms in the activated sludge decompose organic matters, so that the COD (chemical oxygen demand) of the wastewater is reduced to 1500 mg/L.
3. Hydrolysis and acidification: the wastewater after anaerobic treatment enters a hydrolytic acidification tank and is decomposed in an aerobic way; adding sodium carbonate in the aerobic decomposition process according to 2KG/10m3The sodium carbonate is added into the waste water in quantity.
4. The hydrolyzed wastewater enters a biological contact oxidation tank and flows to a gallery 5 from a gallery 1 step by step, aeration adjustment is additionally arranged in each gallery in the interval, parameters such as pH (potential of hydrogen), dissolved oxygen and the like are correspondingly adjusted by observing the color of sludge according to COD (chemical oxygen demand) and ammonia nitrogen data, the COD is about 150mg/L and the ammonia nitrogen is about 5mg/L when the wastewater flows out of the tail end of the gallery, the wastewater reaches the discharge standard after being filtered by a secondary sedimentation tank through a grid and a filter screen to remove solid matters, and the wastewater is discharged to a regional treatment plant for deep harmless treatment.
The above-mentioned embodiments are merely preferred technical solutions of the present invention, but the scope of the present invention is not limited thereto. The embodiments and features of the embodiments in the present application may be arbitrarily combined with each other without conflict. The protection scope of the present invention is defined by the claims, and includes equivalents of technical features of the claims. Any changes or alternative modifications that can be easily conceived by those skilled in the art within the technical scope of the present disclosure are also covered by the protection scope of the present invention.
Claims (10)
1. A method of treating amino acid extraction wastewater using slaked lime to replace a neutralizing agent and a flocculating agent, the method comprising the steps of:
s1, pH adjustment and deamination: the high ammonia nitrogen wastewater enters a high ammonia nitrogen wastewater adjusting tank, slaked lime is added in batches under stirring, the pH value of the wastewater is adjusted to be more than 11, the wastewater enters a deamination tower for blow-off, the blow-off wastewater and the common wastewater are mixed in a comprehensive adjusting tank to obtain mixed wastewater, and the mixed wastewater is precipitated to obtain supernatant;
s2, flocculating and settling: the supernatant obtained in the step S1 enters a flocculation sedimentation tank, and is further precipitated through a physical separation system to obtain supernatant and waste mud;
s3, anaerobic treatment: the supernatant obtained in the step S2 enters an anaerobic reactor for anaerobic decomposition;
s4, hydrolysis acidification: the wastewater after anaerobic treatment in the step S3 enters a hydrolytic acidification tank for aerobic decomposition;
s5, contact oxidation: the wastewater treated in the step S4 enters a biological contact oxidation tank for biochemical treatment, and indexes are controlled;
s6, separating mud from water: the wastewater subjected to the contact oxidation treatment in the step S5 is rapidly separated in a secondary sedimentation tank through a physical device, sludge deposited to the bottom supplements sludge reduced in the previous process, and the redundant part is deslimed at a desliming post;
s7, emission up to standard: and (4) discharging the wastewater to a regional treatment plant through an online monitoring discharge port for further harmless treatment.
2. The method of claim 1, wherein: in the step S1, the indexes of the high ammonia nitrogen wastewater are as follows: ammonia nitrogen 6000-11000 mg/L, COD: 500-1000 mg/L, pH 2-4.
3. The method of claim 1, wherein: in step S1, the general wastewater has the following indexes: COD: 4000mg/L, ammonia nitrogen: 150mg/L, pH: 2-4; the indexes of the mixed wastewater are as follows: COD: 2000-4000 mg/L of ammonia nitrogen and 500-1000 mg/L of ammonia nitrogen.
4. The method of claim 1, wherein: in the step S1, after the pH value of the wastewater is adjusted to be more than 11, the temperature of the wastewater is increased to 40-50 ℃, and then the wastewater enters a deamination tower for stripping.
5. The method of claim 1, wherein: in the step S1, the mixed wastewater is subjected to precipitation treatment after slaked lime is added to control the pH value 7-9.
6. The method of claim 1, wherein: in the step S1, the slaked lime may be replaced by quick lime.
7. The method of claim 1, wherein: the step S2 includes separating the waste sludge deposited at the bottom, and pumping the waste sludge to a desliming station for desliming.
8. The method of claim 1, wherein: through the anaerobic treatment of the step S3, COD is reduced by at least 50 percent; through step S4, aerobic decomposition, wastewater index: COD is less than 600mg/L, and ammonia nitrogen is less than or equal to 200 mg/L; after the contact oxidation of step S5, the wastewater index: COD: 150-200mg/L, ammonia nitrogen is less than or equal to 10 mg/L.
9. The method of claim 1, wherein: through the treatment of the step S6, the clear liquid in the secondary sedimentation tank can reach COD less than or equal to 150mg/L, ammonia nitrogen less than or equal to 5mg/L and pH 6-9.
10. The method of claim 1, wherein: in the step S4, the data is recorded according to 2KG/10m3Sodium carbonate is added into the waste water in a flowing mode.
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