CN114634278A - Ammonia nitrogen removal process for landfill leachate - Google Patents
Ammonia nitrogen removal process for landfill leachate Download PDFInfo
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- CN114634278A CN114634278A CN202210142133.7A CN202210142133A CN114634278A CN 114634278 A CN114634278 A CN 114634278A CN 202210142133 A CN202210142133 A CN 202210142133A CN 114634278 A CN114634278 A CN 114634278A
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- landfill leachate
- sludge
- ammonia nitrogen
- denitrification
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- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 31
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 238000004062 sedimentation Methods 0.000 claims abstract description 46
- 230000001112 coagulating effect Effects 0.000 claims abstract description 41
- 238000005273 aeration Methods 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000000926 separation method Methods 0.000 claims abstract description 23
- 230000033228 biological regulation Effects 0.000 claims abstract description 7
- 239000010802 sludge Substances 0.000 claims description 67
- 239000000203 mixture Substances 0.000 claims description 30
- 230000014759 maintenance of location Effects 0.000 claims description 26
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 24
- 239000006004 Quartz sand Substances 0.000 claims description 18
- 238000005345 coagulation Methods 0.000 claims description 17
- 230000015271 coagulation Effects 0.000 claims description 17
- 239000008394 flocculating agent Substances 0.000 claims description 12
- 239000010813 municipal solid waste Substances 0.000 claims description 12
- 238000001556 precipitation Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 238000003825 pressing Methods 0.000 claims description 10
- 238000001035 drying Methods 0.000 claims description 9
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- 230000001105 regulatory effect Effects 0.000 claims description 6
- 238000010000 carbonizing Methods 0.000 claims description 5
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- 229920000642 polymer Polymers 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 5
- 238000000108 ultra-filtration Methods 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 4
- 238000010979 pH adjustment Methods 0.000 claims description 4
- 229910021435 silicon-carbon complex Inorganic materials 0.000 claims description 4
- 239000011867 silicon-carbon complex material Substances 0.000 claims description 4
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- 239000002957 persistent organic pollutant Substances 0.000 abstract description 2
- 231100000331 toxic Toxicity 0.000 abstract description 2
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 13
- 229910052799 carbon Inorganic materials 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- HMDDXIMCDZRSNE-UHFFFAOYSA-N [C].[Si] Chemical compound [C].[Si] HMDDXIMCDZRSNE-UHFFFAOYSA-N 0.000 description 9
- 239000000945 filler Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000011812 mixed powder Substances 0.000 description 6
- 239000004677 Nylon Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
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- 238000006297 dehydration reaction Methods 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 229920001778 nylon Polymers 0.000 description 5
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 4
- 239000000084 colloidal system Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000001272 nitrous oxide Substances 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000002470 thermal conductor Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000011258 core-shell material Substances 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
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- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F1/5281—Installations for water purification using chemical 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/44—Time
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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
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- 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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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention relates to the technical field of leachate, in particular to an ammonia nitrogen removal process for landfill leachate. According to the invention, through raw water regulation, coagulating sedimentation, ozone aeration, denitrification, aerobism and MBR separation, pathogenic microorganisms and toxic and harmful physicochemical pollutants in the leachate are removed, and hydroxyl free radicals with strong oxidation capacity are initiated to enhance the decomposition of high-stability and difficultly-degraded organic pollutants in water, so that the water quality is purified, and the effect of removing ammonia nitrogen is improved.
Description
Technical Field
The invention relates to the technical field of leachate, in particular to an ammonia nitrogen removal process for landfill leachate.
Background
The landfill leachate is high-concentration organic wastewater which is formed by deducting the saturated water holding capacity of garbage and a soil covering layer from water contained in the garbage in a garbage landfill, rain, snow and water entering the landfill and other water and passing through the garbage layer and the soil covering layer. Also included are accumulated moisture leaking from the waste ready for incineration. Along with the improvement of people's standard of living, the gathering of population leads to domestic waste's production volume to increase year by year, and people also are higher and higher to the requirement of environment, and rubbish is enclosed city the problem that country and government are waited to solve for the build of msw incineration power plant also becomes the trend, and wherein, the filtration liquid that rubbish produced needs, filtration liquid treatment plant handles, because several big characteristics of rubbish leachate: the concentration of COD and ammonia nitrogen of the leachate is high, the content of heavy metal ions and salt is high, the PH is low and is acidic, and the seasonal change of the quantity of the leachate determines that the difficulty of treating the leachate and domestic sewage is high.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention aims to provide an ammonia nitrogen removal process for landfill leachate.
The purpose of the invention is realized by the following technical scheme:
an ammonia nitrogen removal process for landfill leachate comprises the following steps:
(1) raw water regulation: conveying the landfill leachate to a raw water adjusting tank for storage and pH adjustment;
(2) coagulating sedimentation: conveying the landfill leachate from a raw water regulating tank to a coagulative precipitation tank, putting a flocculating agent into the coagulative precipitation tank for coagulative precipitation, and recovering sludge to a sludge collecting tank;
(3) ozone aeration: conveying the garbage percolate in the coagulation sedimentation tank to an ozone aeration tank for aeration treatment;
(4) denitrification: conveying the landfill leachate from the ozone aeration tank to a denitrification tank for denitrification reaction;
(5) aerobic treatment: conveying the landfill leachate from the denitrification tank to an aerobic tank for aerobic reaction;
(6) MBR separation: and conveying the landfill leachate from the aerobic tank to an MBR (membrane bioreactor) for ultrafiltration separation, wherein clear liquid reaches the discharge standard, one part of sludge flows back to the denitrification tank, and the other part of sludge is recycled to the sludge collection tank.
Wherein the hydraulic retention time of the coagulating sedimentation in the step (2) is 22-30 h.
Wherein, in the coagulating sedimentation in the step (2), the added flocculating agent is polyacrylamide and/or polyaluminium chloride.
Wherein the retention time of the ozone aeration in the step (3) is 6-10h, and the volume ratio of the ozone aeration tank to the coagulation sedimentation tank is 1-2: 1.
Wherein the hydraulic retention time of the denitrification in the step (4) is 55-60h, and the volume ratio of the denitrification tank to the coagulation sedimentation tank is 3-4: 1.
Wherein the aerobic hydraulic retention time in the step (5) is 40-45h, and the volume ratio of the aerobic tank to the coagulating sedimentation tank is 3-4: 1.
Wherein the hydraulic retention time of the MBR separation in the step (6) is 10-15h, and the volume ratio of the MBR reactor to the coagulation sedimentation tank is 0.1-0.3: 1.
Wherein, in the MBR separation in the step (6), the sludge reflux ratio which flows back to the denitrification tank is 50-70%.
Wherein, the method also comprises the following step (7) of sludge recovery: adding a proper amount of quartz sand into the sludge collection tank, then carrying out filter pressing and drying to obtain a mud cake, carbonizing and crushing the mud cake to obtain a carbon-silicon complex, and carrying out sludge blending with a high polymer to obtain the heat-conducting composition.
The prior art is generally to the recovery of mud make the mud cake back return the power plant again and burn the electricity generation again, but mud is because have strong hydrophilicity, and the water content is great, generally can reach 90%, directly carries out the filter-pressing and gets rid of the efficiency of moisture and be limited, and the energy consumption cost of follow-up stoving is extremely high. The inventor finds that the reason of difficult dehydration of the filter pressing is the compressibility of the sludge, and the sludge colloid collapses in the filter pressing process, so that the sludge is more and more compact, thereby closing the escape passage of the internal moisture and hindering the dehydration process. According to the invention, a proper amount of quartz sand is mixed into the sludge, and the quartz sand has good rigidity, so that the compressibility of the sludge is low, and the quartz sand can keep a water channel stable in a filter pressing process, thereby improving the dehydration performance of the sludge. However, since the silica sand is nonflammable, the efficacy of the dewatered sludge as a raw material for power generation is greatly reduced, and for this reason, the applicant has developed another recycling method in which the dewatered sludge is carbonized to form a mixture mainly composed of carbon and silica sand, i.e., a carbon-silicon mixture, in which carbon is a good thermal conductor and can be used as a filler for a thermally conductive composition.
Therefore, the invention aims at sludge recovery, and also provides a preparation method of the heat-conducting composition, which comprises the following steps: adding 10-20 parts by weight of carbon-silicon mixture and 25-35 parts by weight of nylon resin powder into 100 parts by weight of methanol, heating and pressurizing in the stirring process, increasing the air pressure to 1-2MPa, heating to 140-150 ℃, then preserving heat for 1-2h, cooling to room temperature, filtering and drying to obtain mixed powder; and (2) mixing the mixed powder, the lubricant and the antioxidant at a high speed according to the weight ratio of 100:1-2:0.1-0.2, and then putting the mixture into a double-screw extruder for extrusion molding to obtain the heat-conducting composition.
Wherein the grain diameter of the silicon-carbon mixture is 100-200 mu m, and the adding amount of the quartz sand in the sludge recovery in the step (7) is 5-10 wt% of the sludge (containing water) in the sludge pool.
The invention utilizes the carbon-silicon mixture to prepare the heat-conducting composition, thereby not only well reducing the dehydration difficulty of the sludge, but also providing another sludge utilization method. And the mixed quartz sand has high temperature resistance and does not generate chemical change at the carbonization temperature of 1000 ℃, so the mixed quartz sand can be used as a separant of a silicon-carbon mixture, can prevent organic matters of sludge from being carbonized to form continuous carbon blocks, and is beneficial to the subsequent crushing process. In addition, the quartz sand is used as a reinforcing filler, the mechanical property of nylon can be improved, although the quartz sand is not a good thermal conductor, organic matters of sludge can tightly coat the quartz sand in the filter pressing process, so a carbon layer can be formed on the surface of the quartz sand after carbonization, most of the silicon-carbon mixture exists in the form of core-shell structure particles taking the quartz sand as core carbon as a shell, the specific surface area of carbon is increased, and the quartz sand basically cannot obstruct continuous heat conduction of the carbon, so that the finally prepared nylon composition has excellent mechanical property and heat conductivity.
The invention has the beneficial effects that: according to the invention, through raw water regulation, coagulating sedimentation, ozone aeration, denitrification, aerobism and MBR separation, pathogenic microorganisms and toxic and harmful physicochemical pollutants in the leachate are removed, and hydroxyl free radicals with strong oxidation capacity are initiated to enhance the decomposition of high-stability and difficultly-degraded organic pollutants in water, so that the water quality is purified, and the effect of removing ammonia nitrogen is improved.
Coagulating sedimentation can reduce or eliminate the electric potential of colloid, destroys the stable state of particles, and enables suspended matters, calcium, magnesium, colloid and flocculating agent of the wastewater to rapidly react through the violent stirring of the stirrer, and the suspended matters, the calcium, the magnesium, the colloid and the flocculating agent are mutually adsorbed and combined to form larger particles which are easy to precipitate.
The strong oxidizing property of ozone aeration can quickly decompose various organic and inorganic pollutants and microorganisms in the sludge water, the deamination and denitrification effects are enhanced, and byproducts are obviously reduced.
The denitrifying bacteria reduce nitrate and release molecular nitrogen (N2) or nitrous oxide (N2O) under the anoxic condition, so that ammonia nitrogen in the wastewater can be effectively removed, and other pollutants in the wastewater can be degraded
The degradation of the organic matters in the sewage by the aerobic bacteria achieves the aim of removing the organic matters.
MBR separation can not only intercept microorganisms in water, but also intercept partial insoluble pollutants of macromolecules, prolong the retention time of the pollutants in a reactor, increase the removal rate of the pollutants difficult to degrade, and simultaneously has good denitrification effect due to long sludge age.
Detailed Description
The present invention will be further described with reference to the following examples for facilitating understanding of those skilled in the art, and the description of the embodiments is not intended to limit the present invention.
Example 1
An ammonia nitrogen removal process for landfill leachate comprises the following steps:
(1) raw water regulation: conveying the landfill leachate to a raw water adjusting tank for storage and pH adjustment;
(2) coagulating sedimentation: conveying the landfill leachate from a raw water regulating tank to a coagulative precipitation tank, putting a flocculating agent into the coagulative precipitation tank for coagulative precipitation, and recovering sludge to a sludge collecting tank;
(3) ozone aeration: conveying the garbage percolate in the coagulation sedimentation tank to an ozone aeration tank for aeration treatment;
(4) denitrification: conveying the landfill leachate from the ozone aeration tank to a denitrification tank for denitrification reaction;
(5) aerobic: conveying the landfill leachate from the denitrification tank to an aerobic tank for aerobic reaction;
(6) MBR separation: and conveying the landfill leachate from the aerobic tank to an MBR (membrane bioreactor) for ultrafiltration separation, wherein clear liquid reaches the discharge standard, one part of sludge flows back to the denitrification tank, and the other part of sludge is recycled to the sludge collection tank.
Wherein the hydraulic retention time of the coagulating sedimentation in the step (2) is 26 h.
And (3) in the coagulating sedimentation in the step (2), the added flocculating agent is polyacrylamide.
Wherein the retention time of the ozone aeration in the step (3) is 8h, and the volume ratio of the ozone aeration tank to the coagulation sedimentation tank is 1.5: 1.
Wherein the hydraulic retention time of the denitrification in the step (4) is 57h, and the volume ratio of the denitrification tank to the coagulation sedimentation tank is 3.5: 1.
Wherein the aerobic hydraulic retention time in the step (5) is 42h, and the volume ratio of the aerobic tank to the coagulating sedimentation tank is 3.5: 1.
And (3) the hydraulic retention time of MBR separation in the step (6) is 12h, and the volume ratio of the MBR to the coagulating sedimentation tank is 0.2: 1.
Wherein, in the MBR separation in the step (6), the sludge reflux ratio which flows back to the denitrification tank is 60 percent.
Example 2
An ammonia nitrogen removal process for landfill leachate comprises the following steps:
(1) raw water regulation: conveying the landfill leachate to a raw water adjusting tank for storage and pH adjustment;
(2) coagulating sedimentation: conveying the landfill leachate from a raw water regulating tank to a coagulative precipitation tank, putting a flocculating agent into the coagulative precipitation tank for coagulative precipitation, and recovering sludge to a sludge collecting tank;
(3) ozone aeration: conveying the garbage percolate in the coagulation sedimentation tank to an ozone aeration tank for aeration treatment;
(4) denitrification: conveying the landfill leachate from the ozone aeration tank to a denitrification tank for denitrification reaction;
(5) aerobic treatment: conveying the landfill leachate from the denitrification tank to an aerobic tank for aerobic reaction;
(6) MBR separation: and conveying the landfill leachate from the aerobic tank to an MBR (membrane bioreactor) for ultrafiltration separation, wherein clear liquid reaches the discharge standard, one part of sludge flows back to the denitrification tank, and the other part of sludge is recycled to the sludge collection tank.
Wherein the hydraulic retention time of the coagulating sedimentation in the step (2) is 22 h.
And (3) in the coagulating sedimentation in the step (2), the added flocculating agent is polyaluminium chloride.
Wherein the retention time of the ozone aeration in the step (3) is 6h, and the volume ratio of the ozone aeration tank to the coagulation sedimentation tank is 1: 1.
Wherein the hydraulic retention time of the denitrification in the step (4) is 55h, and the volume ratio of the denitrification tank to the coagulation sedimentation tank is 3: 1.
Wherein the aerobic hydraulic retention time in the step (5) is 40h, and the volume ratio of the aerobic tank to the coagulating sedimentation tank is 3: 1.
Wherein, the hydraulic retention time of the MBR separation in the step (6) is 10h, and the volume ratio of the MBR reactor to the coagulation sedimentation tank is 0.1: 1.
Wherein, in the MBR separation in the step (6), the sludge reflux ratio which flows back to the denitrification tank is 50%.
Wherein, the method also comprises the following step (7) of sludge recovery: adding a proper amount of quartz sand into the sludge collection tank, then carrying out filter pressing and drying to obtain a mud cake, carbonizing and crushing the mud cake to obtain a carbon-silicon complex, and carrying out sludge blending with a high polymer to obtain the heat-conducting composition.
Example 3
An ammonia nitrogen removal process for landfill leachate comprises the following steps:
(1) raw water regulation: conveying the landfill leachate to a raw water regulating tank for storage and pH regulation;
(2) coagulating sedimentation: conveying the landfill leachate from a raw water regulating tank to a coagulating sedimentation tank, putting a flocculating agent into the coagulating sedimentation tank for coagulating sedimentation, and recovering sludge into a sludge collecting tank;
(3) ozone aeration: conveying the garbage percolate in the coagulation sedimentation tank to an ozone aeration tank for aeration treatment;
(4) denitrification: conveying the landfill leachate from the ozone aeration tank to a denitrification tank for denitrification reaction;
(5) aerobic treatment: conveying the landfill leachate from the denitrification tank to an aerobic tank for aerobic reaction;
(6) MBR separation: and conveying the landfill leachate from the aerobic tank to an MBR (membrane bioreactor) for ultrafiltration separation, wherein clear liquid reaches the discharge standard, one part of sludge flows back to the denitrification tank, and the other part of sludge is recycled to the sludge collection tank.
Wherein the hydraulic retention time of the coagulating sedimentation in the step (2) is 30 h.
And (3) in the coagulating sedimentation in the step (2), the added flocculating agent is polyaluminium chloride.
Wherein the retention time of the ozone aeration in the step (3) is 10h, and the volume ratio of the ozone aeration tank to the coagulation sedimentation tank is 2: 1.
Wherein the hydraulic retention time of the denitrification in the step (4) is 60 hours, and the volume ratio of the denitrification tank to the coagulation sedimentation tank is 4: 1.
Wherein the aerobic hydraulic retention time in the step (5) is 45h, and the volume ratio of the aerobic tank to the coagulating sedimentation tank is 4: 1.
Wherein the hydraulic retention time of the MBR separation in the step (6) is 15h, and the volume ratio of the MBR reactor to the coagulation sedimentation tank is 0.3: 1.
Wherein, in the MBR separation in the step (6), the sludge reflux ratio which flows back to the denitrification tank is 70%.
Example 4
This example is an extension of example 1, namely further comprising step (7) sludge recovery: adding a proper amount of quartz sand into the sludge collection tank, then carrying out filter pressing and drying to obtain a mud cake, carbonizing and crushing the mud cake to obtain a carbon-silicon complex, and carrying out sludge blending with a high polymer to obtain the heat-conducting composition.
The preparation method of the heat-conducting composition comprises the following steps: adding 15 parts by weight of carbon-silicon mixture and 30 parts by weight of nylon resin powder into 100 parts by weight of methanol, heating and pressurizing in the stirring process, increasing the air pressure to 1.5MPa, heating to 145 ℃, then preserving heat for 1.5h, cooling to room temperature, filtering and drying to obtain mixed powder; the mixed powder, the lubricant and the antioxidant are mixed at a high speed according to the weight ratio of 100:1.5:0.15, and then are put into a double-screw extruder for extrusion molding, so that the heat-conducting composition is obtained.
Wherein the grain diameter of the silicon-carbon mixture is 150 mu m, and the adding amount of quartz sand in the sludge recovery in the step (7) is 7.5 wt% of the sludge (containing water) in the sludge tank.
Comparative example 1
This comparative example is an extension of example 1, i.e. further comprising step (7) sludge recovery: and carrying out filter pressing and drying on the sludge in the sludge collection tank to obtain a mud cake, carbonizing and crushing the mud cake to obtain a carbon filler, and carrying out sludge blending with a high polymer to obtain the heat-conducting composition.
The preparation method of the heat-conducting composition comprises the following steps: adding 15 parts by weight of carbon filler and 30 parts by weight of nylon resin powder into 100 parts by weight of methanol, heating and pressurizing in the stirring process, increasing the air pressure to 1.5MPa, heating to 145 ℃, then preserving heat for 1.5h, cooling to room temperature, filtering and drying to obtain mixed powder; and (3) mixing the mixed powder, the lubricant and the antioxidant at a high speed according to the weight ratio of 100:1.5:0.15, and then putting the mixture into a double-screw extruder for extrusion molding to obtain the heat-conducting composition.
Wherein the particle size of the carbon filler is 150 μm.
The thermally conductive compositions of example 1, comparative example 1 and comparative example 2 were subjected to performance tests, and the results were as follows:
from the comparison of the above experiments, no matter the difficulty of dehydration and drying into mud cakes, the tensile strength of the composition is less influenced without adding quartz sand, but the carbon filler is too compact and not easy to disperse, and the composition is more easy to generate stress concentration phenomenon, so that the elongation at break of the composition is obviously reduced; secondly, although the thermal conductivity is not very different, considering that the proportion of carbon of comparative example 1 is 2 times that of example 4, the specific surface area of the carbon filler is actually not as good as that of the silicon-carbon mixture, so the thermal conductivity cannot have a significant advantage.
The above-described embodiments are preferred implementations of the present invention, and the present invention may be implemented in other ways without departing from the spirit of the present invention.
Claims (9)
1. The ammonia nitrogen removal process of the landfill leachate is characterized by comprising the following steps: the method comprises the following steps:
(1) raw water regulation: conveying the landfill leachate to a raw water adjusting tank for storage and pH adjustment;
(2) coagulating sedimentation: conveying the landfill leachate from a raw water regulating tank to a coagulative precipitation tank, putting a flocculating agent into the coagulative precipitation tank for coagulative precipitation, and recovering sludge to a sludge collecting tank;
(3) ozone aeration: conveying the garbage percolate in the coagulation sedimentation tank to an ozone aeration tank for aeration treatment;
(4) denitrification: conveying the landfill leachate from the ozone aeration tank to a denitrification tank for denitrification reaction;
(5) aerobic treatment: conveying the landfill leachate from the denitrification tank to an aerobic tank for aerobic reaction;
(6) MBR separation: and conveying the landfill leachate from the aerobic tank to an MBR (membrane bioreactor) for ultrafiltration separation, wherein clear liquid reaches the discharge standard, one part of sludge flows back to the denitrification tank, and the other part of sludge is recycled to the sludge collection tank.
2. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that: the hydraulic retention time of the coagulating sedimentation in the step (2) is 22-30 h.
3. The ammonia nitrogen removal process for landfill leachate according to claim 1, characterized in that: and (3) in the coagulating sedimentation in the step (2), the added flocculating agent is polyacrylamide and/or polyaluminium chloride.
4. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that: the retention time of the ozone aeration in the step (3) is 6-10h, and the volume ratio of the ozone aeration tank to the coagulation sedimentation tank is 1-2: 1.
5. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that: the hydraulic retention time of the denitrification in the step (4) is 55-60h, and the volume ratio of the denitrification tank to the coagulating sedimentation tank is 3-4: 1.
6. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that: the aerobic hydraulic retention time in the step (5) is 40-45h, and the volume ratio of the aerobic tank to the coagulating sedimentation tank is 3-4: 1.
7. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that: the hydraulic retention time of MBR separation in the step (6) is 10-15h, and the volume ratio of the MBR reactor to the coagulating sedimentation tank is 0.1-0.3: 1.
8. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that: and (5) in the MBR separation in the step (6), the sludge reflux ratio which flows back to the denitrification tank is 50-70%.
9. The ammonia nitrogen removal process of landfill leachate according to claim 1, characterized in that:
also comprises the following steps of (7) sludge recovery: adding a proper amount of quartz sand into the sludge collection tank, then carrying out filter pressing and drying to obtain a mud cake, carbonizing and crushing the mud cake to obtain a carbon-silicon complex, and carrying out sludge blending with a high molecular polymer to obtain the heat-conducting composition.
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