CN106007278A - Sludge treatment method - Google Patents
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- CN106007278A CN106007278A CN201610442808.4A CN201610442808A CN106007278A CN 106007278 A CN106007278 A CN 106007278A CN 201610442808 A CN201610442808 A CN 201610442808A CN 106007278 A CN106007278 A CN 106007278A
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- 239000010802 sludge Substances 0.000 title claims abstract description 185
- 238000000034 method Methods 0.000 title abstract description 35
- 230000029087 digestion Effects 0.000 claims abstract description 85
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000010865 sewage Substances 0.000 claims abstract description 20
- 239000000706 filtrate Substances 0.000 claims abstract description 15
- 239000007787 solid Substances 0.000 claims abstract description 11
- 235000014113 dietary fatty acids Nutrition 0.000 claims abstract description 8
- 239000000194 fatty acid Substances 0.000 claims abstract description 8
- 229930195729 fatty acid Natural products 0.000 claims abstract description 8
- 150000004665 fatty acids Chemical class 0.000 claims abstract description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 36
- 238000005273 aeration Methods 0.000 claims description 21
- 229910052757 nitrogen Inorganic materials 0.000 claims description 18
- 238000010992 reflux Methods 0.000 claims description 17
- 230000018044 dehydration Effects 0.000 claims description 14
- 238000006297 dehydration reaction Methods 0.000 claims description 14
- 238000001914 filtration Methods 0.000 claims description 14
- 239000000395 magnesium oxide Substances 0.000 claims description 14
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 14
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 14
- 238000004065 wastewater treatment Methods 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 7
- 238000003672 processing method Methods 0.000 claims description 7
- 230000033116 oxidation-reduction process Effects 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 abstract description 14
- 238000004062 sedimentation Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000005416 organic matter Substances 0.000 description 5
- 229910019142 PO4 Inorganic materials 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 4
- 239000010452 phosphate Substances 0.000 description 4
- 235000021391 short chain fatty acids Nutrition 0.000 description 4
- 230000000087 stabilizing effect Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 230000006641 stabilisation Effects 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 210000005056 cell body Anatomy 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000001079 digestive effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000012774 insulation material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 238000010564 aerobic fermentation Methods 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000003834 intracellular effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 235000021049 nutrient content Nutrition 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Classifications
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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
- C02F11/00—Treatment of sludge; Devices therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/20—Sludge processing
Landscapes
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Treatment Of Sludge (AREA)
Abstract
The invention discloses a sludge treatment method, and belongs to the technical field of sludge treatment and resource utilization. The method comprises the steps that sewage plant secondary sedimentation tank excess sludge and partial digestion dewatered sludge are mixed, blended to the given solid concentration and fed into a reactor for high-temperature micro-aerobic digestion, a certain volume of digested sludge is discharged at set time intervals, and concentration and dewatering are performed to collect a filtrate. After sludge digestion treatment, the volatile solid removal rate is 26-35%; the filtrate obtained after digestion sludge dewatering contains a high concentration of short-chain volatile fatty acid and can be used as an additional carbon source of a surface source wastewater biochemical treatment system for low-carbon-nitrogen-ratio domestic sewage, the Dian lake and the like.
Description
Technical field
The present invention relates to the processing method of a kind of mud, belong to Treatment of Sludge and application technology as the second resource field.
Background technology
China's municipal sewage treatment ability and treatment effeciency were developed rapidly in Eleventh Five-Year Plan, " 12 " period, brought increasing sharply of sludge yield.2009, China's urban wastewater treatment amount was 28,000,000,000 m3, wet mud (moisture content is assessed with 80%) yield is about 20,050,000 tons.2015, the wet sludge yield of China up to nearly 40,000,000 tons.
Comparing the quick growth of sludge yield, China's specific resistance to filtration Facilities Construction relatively lags behind.At present, wastewater treatment in China factory only about 25% mud obtained the most appropriate process, the unprocessed disposal of mud and the phenomenon arbitrarily stacked happen occasionally, and bring ecological environment around and have a strong impact on.In April, 2015, State Council promulgates " water prevention and cure of pollution action plan ", " mud that sewage treatment facility produces should carry out stabilisation, innoxious and recycling treatment disposal, and region and above municipal sludge harmless treatment disposal rate should reach more than 90% before at the bottom of the year two thousand twenty " is clearly proposed.
Developed country's Treatment of Sludge emphasizes recycling, American-European based on Land_use change, and Japan is utilized as main with building materials after burning.Along with the cry of environmental protection and recycling is the most surging, developed country clearly using Land_use change as the encouragement direction of specific resistance to filtration, and gradually limit the sludge treating methods such as landfill, burning.In terms of technological development direction, after deeply dehydrating sludge, sanitary landfills is the most cambic technology path；Sludge anhydration burning reduction is best, but existence process cost of disposal is higher, the difficult this kind of deficiency of incineration flue gas；After anaerobic sludge digestion/aerobic fermentation, Land_use change is higher due to its resource utilization efficiency, will be the major way of specific resistance to filtration.
Anaerobic sludge digestion recovering energy source material biogas, but anaerobic digestion process is complicated, capital expenditure is higher, operational management is complicated, thus be only suitable in the stabilizing treatment of large-scale wastewater treatment plant mud.Sludge aerobic digestion process has the advantages such as organic matter degradation rate is fast, operation control is flexible, but its energy consumption is of a relatively high with operating cost, thus the more employing in medium and small municipal sewage plant.Existing patent of invention CN200410066202.2 discloses a kind of high temperature aerobic digestion device for sludge, and digestion process temperature of reactor can stably rise to 45～65 DEG C, and mud can get stabilizing treatment at 5～12 d.The method lays particular emphasis on the minimizing of volatile organic constituents in mud and processes, and mud is after aerobic sigestion processes, and carbon containing organic component is eventually converted into CO2、H2The little molecular product such as O.Patent of invention CN200910309367.0 discloses a kind of method for recycling and processing organic sludge as resources, thickened sludge carries out digestion process in the reactor of 48～52 DEG C, mud experiences the first reaction zone high temperature concurrent oxidation and aquoiysis acidifying and the digestion of second reaction zone high-temperature micro-aerobic respectively, and mud cake outward transport is made in the digested sludge of discharge after follow-up processed.The nutrients such as dewatered sludge nitrogen, phosphorus, potassium enrich, can be agricultural as the additive safety of fertilizer or improvement soil, thus realize the purpose of recycling sludge.Patent of invention CN20140067635.3 discloses a kind of organic sludge high-temperature micro-aerobic anaerobic digestion device and method, and organic sludge adds alkali liquor after high-temperature micro-aerobic digests and adjusts pH value to weakly acidic pH, is completed the stabilizing treatment of mud afterwards by anaerobic fermentation.The method utilizes the organic sludge first stage thermophilic digestion restricted supply of process oxygen to produce a certain amount of volatile fatty acid VFA, thus beneficially second stage anaerobic digestion produces methane；But there is the deficiencies such as big, the complex technical process of alkali liquor dosage in the method, it is difficult to is able to popularization and application in the sludge stabilization treatment of middle or small sewage treatment.In existing sludge organism treatment technology, more emphasize the biodegradation of organic component in mud, typically can meet agricultural requirement after digested sludge dehydration, but the carbon containing intermediate product that digestion process metabolism produces effectively is not utilized；It addition, digested sludge dehydration gained filtrate ammonia nitrogen concentration is the highest, thus affect its subsequent treatment and utilization.
Summary of the invention
The sludge reduction that the present invention provides a kind of operating cost economy, operating process relatively simple processes and application technology as the second resource method.High temperature micro-oxygen digestion techniques is used to process sewage plant excess sludge, the heat utilizing Organic oxidation in mud to decompose release maintains self-heating and the condition of high temperature of reactor, high temperature, micro-oxygen consumption environment promote room temperature microorganism rapid decline further and discharge intracellular organic matter, are that short chain volatile fatty acid (SCFAs) enters in sludge-digestion liquid through metabolic conversion.The digested sludge discharged is after processed, and in gained filtrate, carbon source is sufficient, may act as the additional carbon of low-carbon and nitrogen Waste Water Treatment；The nutrient contents such as gained filter cake nitrogen, phosphorus, potassium are higher, meet Land_use change or agricultural demand.This technical method can not only effectively solve the carbon source supplementary question of low-carbon and nitrogen Waste Water Treatment, and has organically combined stabilizing treatment and the recycling of sewage plant sludge.
The method of the invention main operational steps is as follows with technology contents:
(1) delivering to sludge digestion reactor 3 after being concentrated by sewage plant excess sludge, use microporous aeration device 9 to carry out low intensity aeration, add allogenic material magnesium oxide simultaneously, the consumption of magnesium oxide is 0.5 ~ 0.8 kg/ (m3Mud)；Mud is drawn again to spray from sludge digestion reactor 3 top through sludge reflux pump 10 bottom sludge digestion reactor 3 and is sent back to sludge digestion reactor 3；
(2) under the continuous service condition of slaking apparatus, carry out a spoil disposal operation at set intervals, and supplement isopyknic thickened sludge determine (sludge volume is calculated as mud dischargeable capacity ÷ sludge retention time) to digestion reactor, sludge volume by mud dischargeable capacity and mud mean residence time 2～4d；The digested sludge discharged is delivered to sludge concentration tank 4 and is carried out concentration, sends in sludge press filtration device 5 afterwards and carries out sludge dewatering treatment；Dehydration gained filtrate is the sludge internal carbon source containing volatile fatty acid；A gained filtering residue dewatered sludge part is discarded another part and is then passed through in feeding-mixing trough 2 with the excess sludge in biochemical treatment system second pond 8 and carries out mixing and allocating, more again sends sludge digestion reactor 3 back to.
Preferably, in sludge digestion reactor 3 of the present invention, feed sludge solid contents is 3.5～6.5%；For ensureing micro-oxygen digestive environments of reactor, aeration intensity controls at 0.6～1.0 m3Air/(h m3Mud), microporous aeration disc is uniformly arranged on reactor bottom；The oxidation-reduction potential (ORP) of digestion system maintains-350～-100mV.
Preferably, in sludge digestion reactor 3 of the present invention, sludge digestion temperature is 45～60 DEG C；For maintaining the Digestive States of self-heating high-temp, by 180～300 W/ (m3Mud) energy input density determine the watt level of sludge reflux pump 10.
Obtaining filtrate after digested sludge of the present invention dehydration can be directly as the additional carbon of low-carbon and nitrogen Waste Water Treatment, wastewater biological denitrificaion reaction member (7-1 anoxic pond, 7-2 Aerobic Pond) is sent into after being mixed in proportion with the pending water of sewage disposal system regulating reservoir 6 feeding；Comparing the situation not supplementing sludge carbon source, second pond 8 water outlet Nitrogen removal effect improves more than 54%.
The device have the advantages that as follows:
(1) adding allogenic material magnesium oxide in sludge digestion process, effectively reduce ammonia nitrogen and the phosphate of the release of high temperature micro-oxygen digestion process, the filtrate after digested sludge dehydration can directly serve as the additional carbon of low-carbon and nitrogen biochemical treatment of wastewater.
(2) after sludge high temperature micro-oxygen digestion process, digested sludge after dehydration meets agricultural requirement, dehydration gained filtrate may act as carbon source, in mud, organic solid thing component clearance is not less than 26%, it is simultaneously achieved the minimizing of mud, stabilisation and resource, efficiently solve sewage plant sludge to process and dispose and low-carbon and nitrogen wastewater treatment process needs the problem of extra supplementary carbon source, Sewage Plant is long-term, stable operation time economy, environmental benefit obvious.
Accompanying drawing illustrates:
The technological process of Fig. 1 high temperature micro-oxygen digestion release sludge internal carbon source reinforced low-carbon nitrogen wastewater biological denitrificaion
In figure: 1 mud storage tank；2 feeding-mixing troughs；3 sludge digestion reactors；4 sludge concentration tanks；5 sludge press filtration devices；6 sewage disposal system regulating reservoirs；7 wastewater biological denitrificaion devices (7-1 anoxic pond, 7-2 Aerobic Pond)；8 second ponds；9 aerators；10 sludge reflux pumps.
Detailed description of the invention
Below in conjunction with appended Fig. 1, embodiments of the invention are elaborated；The present embodiment is implemented premised on technical solution of the present invention, gives detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
The evaluation method discharging sludge internal carbon source reinforced low-carbon nitrogen biological wastewater treatment effect in following example is as follows: Waste Water Treatment uses A/O technique, and primary operating parameter is: dissolved oxygen in anoxic tank DO 0.3～0.4 mg/L, hydraulic detention time HRT 5 h；Aerobic Pond DO 2.2～3.0 mg/L, pH 7.2～7.6, MLSS 1800～2200 mg/L, HRT 15 h；Second pond supernatant is to anoxic pond reflux ratio 200%, return sludge ratio 120%, sludge age SRT 40 d.Low-carbon and nitrogen waste water quality index is as follows: COD 230～250 mg/L, TN 37～40 mg/L, TP 1.8～2.1 mg/L.By 1/30 addition digested sludge dehydration gained filtrate of A/O system flow of inlet water.
Embodiment 1
Employing dischargeable capacity is 2.0m3Cylindrical sludge digestion reactor 3, circulating sludge is drawn bottom sludge digestion reactor 3, after sludge reflux pump 10 delivers to tower top, spray returns digestion reactor, tower top is uniformly arranged 3 spray equipments, reactor bottom uniformly installs 3 300mm microporous aeration devices 9, outside sludge digestion reactor 3 cell body, air inlet pipeline and sludge reflux pipeline be all coated with insulation material thick for 6cm to maintain the self-heating high-temp state of reactor.
(1) when sludge digestion reactor 3 starts, after being concentrated by sewage plant excess sludge, (initial charge sludge solid content is 3.5%) delivers to sludge digestion reactor 3, microporous aeration device 9 is used to carry out low intensity aeration, adding allogenic material magnesium oxide, the consumption of magnesium oxide is 0.5 kg/ (m simultaneously3Mud)；By energy input density 250 W/ (m3Mud) watt level that determines sludge reflux pump 10 is 500 W, returned sludge is drawn again to spray from sludge digestion reactor 3 top through sludge reflux pump 10 bottom digestion reactor 3 and is sent back in digestion reactor；The aeration intensity of sludge digestion reactor 3 is 0.6m3Air/(h m3Mud), the most each branch line air-flow total amount 1.2m3/ h, the tail gas of generation is delivered to the emission-control equipment of sewage treatment plant and is uniformly processed.
(2), after the first batch of mud in sludge digestion reactor 3 runs 3d continuously, semicontinuous operation is carried out by the requirement of sludge retention time 2.5 d.Every 24 h discharge 0.8 m3Digested sludge, and supplement isopyknic fresh sludge (solid contents 3.4～3.7%), add magnesium oxide 0.4kg simultaneously；After running 10d, the digested sludge of discharge is delivered to sludge concentration tank 4 and is carried out concentration, sends in sludge press filtration device 5 afterwards and carries out sludge dewatering treatment；Dehydration gained filtrate is containing volatile fatty acid, and SCFAs concentration reaches 8450～9380 mg/L；A gained filtering residue dewatered sludge part is discarded another part and is then passed through in feeding-mixing trough 2 with the excess sludge in biochemical treatment system second pond 8 and carries out mixing and allocating, more again sends sludge digestion reactor 3 back to.Run duration, temperature of reactor reaches 45～50 DEG C, and digestion system ORP value is-290～-100mV, and mud volatile organic matter clearance is 30～35%.
Waste water A/O system the effluent index of low-carbon and nitrogen water inlet is as follows: COD 82～90 mg/L, ammonia nitrogen 7～10 mg/L, phosphate 0.3～0.4 mg/L；Waste water A/O system water outlet the ammonia nitrogen concentration not adding sludge-digestion liquid is 18～22 mg/L；Compare the biochemical treatment of wastewater not having supplementary carbon source, add the Waste Water Treatment Nitrogen removal effect after sludge internal carbon source and improve 54～61%.
Embodiment 2
Employing dischargeable capacity is 12m3Cylindrical sludge digestion reactor 3, circulating sludge is drawn bottom sludge digestion reactor 3, after sludge reflux pump 10 delivers to tower top, spray returns sludge digestion reactor 3, tower top is uniformly arranged 7 spray equipments, reactor bottom uniformly installs 5 300 mm microporous aeration devices 9, outside sludge digestion reactor 3 cell body, air inlet pipeline and sludge reflux pipeline be all coated with insulation material thick for 6 cm to maintain the self-heating high-temp state of reactor.
(1) when sludge digestion reactor 3 starts, after being concentrated by sewage plant excess sludge, (initial charge sludge solid content is 6.5%) delivers to sludge digestion reactor 3, microporous aeration device 9 is used to carry out low intensity aeration, adding allogenic material magnesium oxide, the consumption of magnesium oxide is 0.7 kg/ (m simultaneously3Mud)；By energy input density 180 W/ (m3Mud) watt level that determines sludge reflux pump 10 is 2.2kW, returned sludge is drawn again to spray from sludge digestion reactor 3 top through sludge reflux pump 10 bottom digestion reactor 3 and is sent back in digestion reactor；The aeration intensity of sludge digestion reactor 3 is 1.0m3Air/(h m3Mud), i.e. sludge digestion reactor 3 aeration total amount is 12 m3/ h, the tail gas of generation is delivered to the emission-control equipment of sewage treatment plant and is uniformly processed.
(2) after the first batch of mud in sludge digestion reactor 3 runs 3d continuously, carrying out semicontinuous operation by the requirement of sludge retention time 3d, every 24h discharges 4.0m3Digested sludge, and supplementary equal-volume fresh sludge (solid contents 6.4～6.7%), add magnesium oxide 2.8kg simultaneously；After running 10d, the digested sludge of discharge is delivered to sludge concentration tank 4 and is carried out concentration, sends in sludge press filtration device 5 afterwards and carries out sludge dewatering treatment；Dehydration gained filtrate is containing volatile fatty acid, and SCFAs concentration reaches 9130～11600mg/L；A gained filtering residue dewatered sludge part is discarded another part and is then passed through with the excess sludge in biochemical treatment system second pond 8 in feeding-mixing trough (2) and carries out mixing and allocating, more again sends sludge digestion reactor 3 back to.Run duration, temperature of reactor reaches 51～55 DEG C, and digestion system ORP value is-340～-130 mV, and mud volatile organic matter clearance is 26～32%.
After adding digested sludge dehydration gained filtrate supplementary carbon source, low-carbon and nitrogen Waste Water Treatment effluent index is as follows: COD 83～92 mg/L, ammonia nitrogen 7～9 mg/L, phosphate 0.3～0.4 mg/L；Waste water A/O system water outlet the ammonia nitrogen concentration not adding sludge-digestion liquid is 19～23 mg/L；Compare the biochemical treatment of wastewater not having supplementary carbon source, add the Waste Water Treatment Nitrogen removal effect after sludge internal carbon source and improve nearly 60%.
Embodiment 3
Using dischargeable capacity is 2.0 m3Cylindrical sludge digestion reactor 3, circulating sludge is drawn bottom sludge digestion reactor 3, after sludge reflux pump 10 delivers to tower top, spray returns sludge digestion reactor 3, and tower top is uniformly arranged 3 spray equipments, and reactor bottom uniformly installs 3 300 mm microporous aeration devices 9；Sludge digesting unit periphery is installed and is added heat pipe and temperature controller, and controlling sludge digestion reaction temperature is 60 DEG C.
(1) when sludge digestion reactor 3 starts, after being concentrated by sewage plant excess sludge, (initial charge sludge solid content is 5.0%) delivers to sludge digestion reactor 3, microporous aeration device 9 is used to carry out low intensity aeration, adding allogenic material magnesium oxide, the consumption of magnesium oxide is 0.8 kg/ (m simultaneously3Mud)；By energy input density 200 W/ (m3Mud) watt level that determines sludge reflux pump 10 is 400W, returned sludge is drawn again to spray from sludge digestion reactor 3 top through sludge reflux pump 10 bottom digestion reactor 3 and is sent back in digestion reactor；The aeration intensity of sludge digestion reactor 3 is 0.8m3Air/(h m3Mud), i.e. sludge digestion reactor 3 aeration total amount is 1.6m3/ h, the tail gas of generation is delivered to the emission-control equipment of sewage treatment plant and is uniformly processed.
(2) after the first batch of mud in sludge digestion reactor 3 runs 3d continuously, carrying out semicontinuous operation by the requirement of sludge retention time 4d, every 24 h discharge 0.5m3Digested sludge, and supplementary equal-volume fresh sludge (solid contents 4.9～5.2%), add magnesium oxide 0.4kg simultaneously；After running 10 d, the digested sludge of discharge is delivered to sludge concentration tank 4 and is carried out concentration, sends in sludge press filtration device 5 afterwards and carries out sludge dewatering treatment；Dehydration gained filtrate is containing volatile fatty acid, and SCFAs concentration reaches 8570～9690mg/L；A gained filtering residue dewatered sludge part is discarded another part and is then passed through in feeding-mixing trough 2 with the excess sludge in biochemical treatment system second pond 8 and carries out mixing and allocating, more again sends sludge digestion reactor 3 back to.Run duration, sludge digestion reactor is 60 DEG C by add heat pipe and temperature controller controlling digestion temperature, and digestion system ORP value is-320～-120 mV, and mud volatile organic matter clearance is 34～39%.
Waste water A/O system the effluent index of low-carbon and nitrogen water inlet is as follows: COD 80～91 mg/L, ammonia nitrogen 8～10 mg/L, phosphate 0.3～0.4 mg/L.Waste water A/O system water outlet the ammonia nitrogen concentration not adding sludge-digestion liquid is 18～22 mg/L.Compare the biochemical treatment of wastewater not having supplementary carbon source, add the Waste Water Treatment Nitrogen removal effect after sludge internal carbon source and improve nearly 55%.
Claims (5)
1. the processing method of a mud, it is characterised in that specifically include following steps:
(1) delivering to sludge digestion reactor after being concentrated by sewage plant excess sludge, use microporous aeration device to carry out low intensity aeration, add allogenic material magnesium oxide simultaneously, the consumption of magnesium oxide is 0.5 ~ 0.8 kg/ (m3Mud)；Mud is drawn again to spray from sludge digestion reactor head through sludge reflux pump from sludge digestion reactor bottom and is sent back to sludge digestion reactor；
(2) under the continuous service condition of slaking apparatus, carry out a spoil disposal operation at set intervals, and supplementary isopyknic thickened sludge is determined by mud dischargeable capacity and mud mean residence time 2～4d to digestion reactor, sludge volume；The digested sludge discharged is delivered to sludge concentration tank and is carried out concentration, sends in sludge press filtration device afterwards and carries out sludge dewatering treatment；Dehydration gained filtrate is the sludge internal carbon source containing volatile fatty acid；A gained filtering residue dewatered sludge part is discarded another part and is then passed through in feeding-mixing trough with the excess sludge in biochemical treatment system second pond and carries out mixing and allocating, more again sends sludge digestion reactor back to.
The processing method of mud the most according to claim 1, it is characterised in that: in sludge digestion reactor, feed sludge solid contents is 3.5～6.5%, aeration intensity 0.6～1.0 m3Air/(h m3Mud), the oxidation-reduction potential (ORP) of digestion system maintains-350～-100mV.
The processing method of mud the most according to claim 1, it is characterised in that: in sludge digestion reactor, sludge digestion temperature is 45～60 DEG C.
The processing method of mud the most according to claim 1, it is characterised in that: by 180～300 W/ (m3Mud) energy input density determine the watt level of sludge reflux pump.
The processing method of mud the most according to claim 1, it is characterised in that: obtaining filtrate after digested sludge dehydration can be directly as the additional carbon of low-carbon and nitrogen Waste Water Treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610442808.4A CN106007278A (en) | 2016-06-21 | 2016-06-21 | Sludge treatment method |
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| TWI780585B (en) * | 2021-01-28 | 2022-10-11 | 友達光電股份有限公司 | Method and system for recycling organic sludge as resource |
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