CN105152506B - Organic sludge high-temperature micro-aerobic anaerobic digestion process - Google Patents
Organic sludge high-temperature micro-aerobic anaerobic digestion process Download PDFInfo
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- 239000010802 sludge Substances 0.000 title claims abstract description 160
- 230000029087 digestion Effects 0.000 title claims abstract description 145
- 238000000034 method Methods 0.000 title claims abstract description 88
- 238000010438 heat treatment Methods 0.000 claims abstract description 53
- 238000000855 fermentation Methods 0.000 claims abstract description 38
- 230000001105 regulatory Effects 0.000 claims abstract description 30
- 238000005273 aeration Methods 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 25
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 25
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 25
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000007599 discharging Methods 0.000 claims abstract description 15
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 9
- 239000000463 material Substances 0.000 claims abstract description 5
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 5
- 239000003513 alkali Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 239000007787 solid Substances 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 14
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000006297 dehydration reaction Methods 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 230000004151 fermentation Effects 0.000 claims description 3
- 230000033116 oxidation-reduction process Effects 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 14
- 230000000694 effects Effects 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 238000009413 insulation Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 4
- 239000000523 sample Substances 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 230000001079 digestive Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000002910 solid waste Substances 0.000 description 3
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 3
- 230000037250 Clearance Effects 0.000 description 2
- 241001148470 aerobic bacillus Species 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 230000035512 clearance Effects 0.000 description 2
- 235000014113 dietary fatty acids Nutrition 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 239000000194 fatty acid Substances 0.000 description 2
- 150000004665 fatty acids Chemical class 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000000813 microbial Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000006213 oxygenation reaction Methods 0.000 description 2
- 230000001717 pathogenic Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- XLYOFNOQVPJJNP-ZSJDYOACSA-N water-d2 Chemical compound [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 230000036887 VSS Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000006701 autoxidation reaction Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000005039 chemical industry Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000004059 degradation Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
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- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000010794 food waste Substances 0.000 description 1
- 230000003694 hair properties Effects 0.000 description 1
- 239000004021 humic acid Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 load Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000003550 marker Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 244000052769 pathogens Species 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000009374 poultry farming Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
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- 239000012056 semi-solid material Substances 0.000 description 1
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Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- 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
Abstract
The invention discloses a kind of organic sludge high-temperature micro-aerobic anaerobic digestion process, organic sludge carries out high-temperature micro-aerobic digestion process first, after high-temperature micro-aerobic digestion terminates, postdigestive sludge enters pH value regulating reservoir from discharging opening by pipeline, to the pH that material in alkali lye regulating reservoir is put into pH value regulating reservoir, sludge stops 3~5h to discharge the dissolved oxygen in sludge in pond；Then sludge stops 6~20 days completion anaerobic digestion process by being pumped into anaerobic fermentation reactor.The front half section of organic sludge digestion process of the invention is self-heating high-temperature micro-aerobic digestion process, rather than ATAD process；The air capacity of self-heating high-temperature micro-aerobic digestion process supply is limited, and under oxygen restrictive condition, it is easy to produce VFA, and VFA is under anaerobic, it is easy to methane phase；Further digestion so both beneficial to second half section anaerobic digestion process to sludge produces methane, and aeration rate, reducing energy consumption can be reduced again.
Description
The application is Application No. 201410067635.3, and the applying date is on 2 26th, 2014, and invention and created name is
The divisional application of the application for a patent for invention of " organic sludge high-temperature micro-aerobic-anaerobic digestion device and method ".
Technical field
The present invention relates to the process field of solid waste, and in particular to a kind of organic sludge high-temperature micro-aerobic-anaerobism disappears
Change method.
Background technology
With Chinese society economy and the development of urbanization, the quantity of municipal sewage is constantly increasing.It was predicted that 2010
China's urban wastewater discharge is up to 44,000,000,000 m3/d；The year two thousand twenty is up to 53,600,000,000 m3/d.Current wastewater treatment in China amount and place
Although reason rate is not high, about 300,000 tons of dewatered sludge discharges every year in municipal sewage plant, but also with annual 10% speed
Increase[2]., there is the light mud phenomenon of heavy water in existing sewage treatment plant of China, have a big chunk sludge not have stabilization processes and nothing
Evilization treatment, sludge treatment facilities are not also run effectively, and sludge is not disposed properly, causes environmental pollution, it is suppressed that
The long-term sustainable development of municipal wastewater treatment plant.At present, it is dirty in international coverage for how effectively processing municipal sludge（It is useless）Water process
The mostly important and problem of complexity faced in field.
Sludge digestion technology to organic matter degrade and reaches the stabilisation of sludge and innoxious by microorganism.It is existing
Sludge digestion technique mainly has traditional aerobic sigestion technique, conventional mesophilic anaerobic digestion technique, two-stage anaerobic digestion technique, lacks
Oxygen/aerobic sigestion technique, autothermal thermophilic aerobic digestion technique, two sections of high-temperature aerobic/mesophilic anaerobic digestion techniques.
Two sections of high-temperature aerobics/mesophilic anaerobic digestion technique therein disappears autothermal thermophilic aerobic digestion technique and anaeration in normal temperature
Chemical industry skill is combined, in being entered back into after first being pre-processed to sludge with one section of high load capacity autothermal thermophilic aerobic digestion process system
Warm anaerobic reactor.The technique is remarkably improved the stability run to the clearance of pathogen and follow-up mesophilic anaerobic digestion,
But the technique is still in the experimental stage.
Such as Chinese patent literature CN 100486722C（Application number 200610087577.6）Disclose a kind of two benches
The fertile gas-made technology of semisolid debirs digestion system, semisolid debirs in the high-temperature micro-aerobic and anaeration in normal temperature bar connected
Digested under part, hot stage kills pathogenic bacteria, predecomposition waste, middle thermophase is main to be decomposed waste, produces biogas, and final product is rich
Containing humic acid, nitrogen, phosphorus, potassium；Comprise the concrete steps that semisolid debirs enter high-temperature micro-aerobic first and digest unit, it is micro- to high temperature
Be passed through air in aerobic sigestion unit, maintain the dissolved oxygen concentration of semi-solid waste in high-temperature micro-aerobic digestion unit 0.1~
0.8mg/L, semisolid debirs start under microbial action to decompose again, consume oxygen and release reaction heat, digestive juice temperature
Up to more than 55 DEG C, maintain 55 DEG C~70 DEG C of digestive juice temperature and kept for 1~3 day；From high-temperature micro-aerobic digestion unit discharge
Enter the mesophilic anaerobic digestion unit of second stage after the quiet heat exchanger cooling of high temperature fluid, the used heat that heat exchanger is reclaimed is with recirculated water
For carrier is incubated to mesophilic anaerobic digestion unit；Mesophilic anaerobic digestion cell temperature maintains 35 DEG C~40 DEG C, pH value dimension
Hold 6.5~8, the degradable material in digestive juice is constantly converted into biogas, and second stage is by after 15~20 days, digestion is final
Product from mesophilic anaerobic digestion unit discharge, into precipitation reservoir it is standby or sale.
The high-temperature micro-aerobic stage of the preparation technology has that oxygenation is difficult, in actual job, 55 DEG C~70 DEG C
Under hot conditions, dissolved oxygen concentration is very low, and semisolid material oxygen transfer efficiency is low, and oxygenation is very limited, therefore the method
It is difficult to reach aerobic state according to text disclosure, and is unable to reach if aerobic condition, the first stage cannot discharges foot
Enough heats, the easy anaerobic acidification of organic solid, from the first stage, the sludge pH of outflow is relatively low, causes second stage anaerobic digestion
Process cannot produce biogas, and the anaerobic digestion residence time is long；Further according to the presently disclosed content of the method, anaeration in normal temperature disappears
Change the more difficult control of temperature to target temperature, because the waste heat that heat exchanger is reclaimed is low（I.e. 55 DEG C~70 DEG C to 35 DEG C~40
DEG C temperature difference heat it is little）, it is difficult to reach insulation effect；Anaerobic pond is long due to the residence time, bulky, in the winter time by changing
It is just lower that hot device reaches insulation effect effect.
The content of the invention
The technical problems to be solved by the invention are to provide a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion process.
The technical scheme for realizing the object of the invention is a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion process, the method
Equipment therefor includes high-temperature aerobic reactor and anaerobic fermentation reactor, also including pH value regulating reservoir；The high-temperature aerobic reaction
Device is self-heating high-temperature micro-aerobic reactor；PH value regulating reservoir be arranged on high-temperature micro-aerobic reactor and anaerobic fermentation reactor it
Between, the discharging opening of self-heating high-temperature micro-aerobic reactor is communicated by pipeline with pH value regulating reservoir, and pH value regulating reservoir passes through pipeline
It is connected with pump with the charging aperture of anaerobic fermentation reactor.
Self-heating high-temperature micro-aerobic reactor includes that retort, sludge recirculation system, aerating system, temperature sensor are gentle
Body absorption treating device；The sludge recirculation system is arranged on outside retort, including hypomere pipeline, sludge reflux pump and epimere
Pipeline；Hypomere pipeline, sludge reflux pump, epimere pipeline and retort form a loop for communicating；Aerating system includes exposure
Tracheae, aeration head, pressure gauge, aeration tube are arranged in the bottom of retort；Temperature sensor the top of retort, middle part, under
Portion respectively sets one；Gas absorption treating device is arranged on the top of retort, is communicated with the inside of retort by pipeline.
The anaerobic fermentation reactor includes that retort, agitator, gas collection filter, temperature sensor, gas take
Sample pipe and circulating water line.Agitator includes motor, bar axle and stirrer paddle, and motor is fixedly installed on the top of retort, bar
Axle is penetrated inside retort from the top down, and stirrer paddle sets two-layer on bar axle, and the stirrer paddle of wherein lower floor is arranged on instead
The bottom of tank is answered, the stirrer paddle on upper strata is arranged on the middle part of available depth in retort.
Circulating water line is arranged on reaction pot bottom, is connected with boiler by pipeline, the gas-cooker of boiler by pipeline with
The gas outlet of gas collection filter is connected.
A kind of digestion method of organic sludge high-temperature micro-aerobic-anaerobic digestion device as described above, comprises the following steps：
1. tamed strain, tamed strain is carried out in the retort of self-heating high-temperature micro-aerobic reactor, tamed
To the kind mud containing strain stay 1/4~1/2 inside retort.
2. the high-temperature micro-aerobic digestion process of organic sludge；Sludge delivery pump is opened, is reacted to self-heating high-temperature micro-aerobic
Organic sludge is sent into the retort of device, the conveying capacity of organic sludge is the remaining effective volume of retort；Open sludge reflux
System and aerating system, organic sludge start high-temperature micro-aerobic digestion process, and sludge is in self-heating high-temperature micro-aerobic reactor
Stop 2~3 days and complete high-temperature micro-aerobic digestion process；Digestion temperature is maintained between 45 DEG C~65 DEG C.
After high-temperature micro-aerobic digestion terminates, postdigestive sludge enters pH value regulating reservoir from discharging opening by pipeline, to pH
Alkali lye is put into value regulating reservoir, the pH value of the material in pH value regulating reservoir is transferred between 6.8~7.2, after pH value regulation is finished
Sludge 3~5h is stopped in pond to discharge the dissolved oxygen in sludge.
3. the anaerobic digestion process of organic sludge；Step 2. discharge dissolved oxygen by high-temperature micro-aerobic digest sludge by
It is pumped into anaerobic fermentation reactor and stops 6~20 days completion anaerobic digestion process, discharge mud is directly agricultural after mechanical dehydration.
Above-mentioned steps are 2. in the high-temperature micro-aerobic digestion process of organic sludge, the reaction of self-heating high-temperature micro-aerobic reactor
Oxidation-reduction potential ORP in tank is 0~-100mv.
Above-mentioned steps 3. organic sludge anaerobic digestion process be mesophilic anaerobic digestion process；Anaeration in normal temperature temperature is 33 DEG C
~35 DEG C, sludge is stopped 10~20 days in anaerobic fermentation reactor and completes anaerobic digestion process.
Further, if the sludge temperature flowed out after the digestion of self-heating high-temperature micro-aerobic is more than 60 DEG C, by high-temperature micro-aerobic
Postdigestive sludge 0~40min of extended residence time in pH value regulating reservoir radiates to anaeration in normal temperature temperature range；If anaerobic pond
Temperature does not reach anaeration in normal temperature temperature range, then reduce the aeration rate of high-temperature micro-aerobic digestion, increase sludge reflux to mechanical heat
Amount so that high-temperature micro-aerobic digestion temperature reaches 50 DEG C~60 DEG C, it is ensured that the middle temperature of anaerobic pond.
It is selectable, step 3. organic sludge anaerobic digestion process be thermophilic digestion process；Thermophilic digestion
Temperature be 50 DEG C~55 DEG C, sludge is stopped in anaerobic fermentation reactor 6~10 days completion anaerobic digestion process.
Further, the methane gas that thermophilic digestion process is produced is collected and after-combustion produces steam or hot water to detesting
To maintain 50 DEG C~55 DEG C of high temperature, the steam or hot water that methyl hydride combustion is produced pass through anaerobic fermentation to the heat supply of aerobe fermentation reactor
The circulating water line of reactor bottom is to retort heat supply, while opening the agitator of retort.
Step 2. in organic sludge for solid content 4%~7%, volatility organic solid concentration accounts for 60%~90% liquid
Organic solid castoff.
The present invention has positive effect：（1）Organic sludge self-heating high-temperature micro-aerobic-anaerobic digestion device of the invention
It is in series by self-heating high-temperature micro-aerobic reactor and anaerobic fermentation reactor.Leading portion self-heating high-temperature micro-aerobic reactor leads to
Insulation is crossed, the heat discharged during volatile organic matter aerobic sigestion is incubated, add mechanical heat production, so that
Reactor is reached from being warming up to 45 DEG C~65 DEG C, it is ensured that high-temperature micro-aerobic digestion is smoothed out.
It is selectable in back segment anaerobic fermentation reactor to carry out mesophilic digestion or thermophilic digestion, wherein mesophilic anaerobic digestion profit
The heat that the sludge flowed out with self-heating high-temperature micro-aerobic reactor is carried, is not required to external heat source, cost-effective；And high temperature is detested
The heat that the sludge of self-heating high-temperature micro-aerobic outflow of the thermal source part for oxygen digestion from leading portion is carried, another part thermal source
Source be combustion high temperature anaerobic digestion produce methane obtain, be equally not required to external heat source, it is cost-effective.Anaerobic fermentation reacts
Device can produce the methane gas with energy substance, carry out recycling；And digest after sludge remain nitrogen and phosphorus into
Point, can solve the final outlet of sludge with agricultural after dehydration.
（2）Self-heating high-temperature micro-aerobic digestion process of the invention ensures that the solid content into mud is 4%~7%, reactor body
Product is more than 10m3More than and appropriate aeration rate is set and good immixture is provided, while will be aerobic in digestion process
The heat of digestion reaction release is remained, and supplies the mechanical energy no more than 30% by sludge reflux, so that reactor
Reach and maintain 45 DEG C~65 DEG C of the condition of high temperature so that it is more effective, thorough that high-temperature micro-aerobic digestion is completed.Due to being micro- good
Oxygen digestion process, aeration rate is few relative to aerobic sigestion, and sludge is extremely difficult to more than 70 degree from heating up in reactor；And for having
The micro- Aerobic-anaerobic digestion process of machine sludge high temperature, there are some researches show when the digestion temperature of self-heating high-temperature micro-aerobic digestion process
During more than 65 DEG C, the effect of whole digestion process is deteriorated, and is in particular in that VSS clearances are relatively low, is 20%~30%.
（3）The front half section of organic sludge digestion process of the invention is self-heating high-temperature micro-aerobic digestion process, rather than
ATAD process；The air capacity of self-heating high-temperature micro-aerobic digestion process supply is limited, in oxygen restrictive condition
Under, it is easy to produce volatile fatty acid（Hereinafter referred to as VFA）, and VFA is under anaerobic, it is easy to methane phase；So both
Further digestion beneficial to second half section anaerobic digestion process to sludge produces methane, and aeration rate, reducing energy consumption can be reduced again.Due to
Self-heating high-temperature micro-aerobic digestion process during front half section, accelerates anaerobic digestion process, and general anaerobic digestion will reach more than 40 days,
Or for more time, but the process residence time can be reached within shortening to 20 days.
（4）The present invention is applied to solid content 4%~7%, and the liquid that volatility organic solid concentration accounts for 60%~90% is organic
Solid waste, such as municipal sludge, organic waste, food waste, the animals excrement liquid state organics of the discharge of poultry farming factory.By
High in the sludge concentration in input reactor, viscosity is big, and oxygen demand is more, and the oxygen amount that mass transfer enters reactor is limited, therefore
It is not exclusively aerobic in self-heating high-temperature micro-aerobic reactor, i.e., will be waved by the collective effect of aerobic bacteria, amphimicrobe, anaerobic bacteria
Hair property organic matter degradation, subsequently into anaerobic reactor fermentation methane phase, sludge, can be used as the organic of fertilizer through dehydration after digestion
Solid, solves the final problem of outlet of organic sludge.
（5）The postdigestive sludge of self-heating high-temperature micro-aerobic of the present invention adjusts pH value in pH value regulating reservoir and discharges dissolving
Oxygen, because self-heating high-temperature micro-aerobic digestible energy produces a large amount of VFA, for anaerobic digestion process methane phase, but VFA can cause pH
Value declines, so, before anaerobic pond is entered, alkali lye is added, the pH value in anaerobic digester is transferred between 6.8~7.2,
Do not exceed 7.5.In addition, mixing pit will stay for some time, because the dirt flowed out from self-heating high-temperature micro-aerobic digester
Mud, with some dissolved oxygens, it is necessary to discharge, it is impossible to be brought into anaerobic pond, can otherwise kill anaerobic bacteria.PH value regulating reservoir also rises
To preparing pool effect, it is easy to pump that sludge is taken out from pH value regulating reservoir, is pumped into anaerobic fermentation reactor.
（6）It is slaking apparatus compact conformation of the invention, simple to operate, you can be built on the ground, also can be buried or half buried,
Save the area, beautify the environment.
Brief description of the drawings
Fig. 1 is the structural representation of slaking apparatus of the invention；
Mark in above-mentioned accompanying drawing is as follows：
High-temperature micro-aerobic reactor 1, retort 11, charging aperture 11-1, discharging opening 11-2, drain 11-3, sludge reflux
System 12, aerating system 13, temperature sensor 14, gas absorption treating device 15；
Anaerobic fermentation reactor 2, retort 21, charging aperture 21-1, discharging opening 21-2, drain 21-3, agitator 22,
Gas collection filter 23, temperature sensor 24, gas sample tube 25, circulating water line 26；PH value regulating reservoir 3.
Specific embodiment
（Embodiment 1）
See Fig. 1, the organic sludge high-temperature micro-aerobic-anaerobic digestion device of the present embodiment includes that self-heating high-temperature micro-aerobic is anti-
Answer device 1, anaerobic fermentation reactor 2 and pH value regulating reservoir 3.PH value regulating reservoir 3 is arranged on high-temperature micro-aerobic reactor 1 and anaerobism hair
Between ferment reactor 2, the discharging opening of self-heating high-temperature micro-aerobic reactor 1 is communicated by pipeline with pH value regulating reservoir 3, and pH value is adjusted
Section pond 3 is connected by pipeline with pump with the charging aperture of anaerobic fermentation reactor 2.
Self-heating high-temperature micro-aerobic reactor 1 includes that retort 11, sludge recirculation system 12, aerating system 13, temperature are passed
Sensor 14 and gas absorption treating device 15.
The periphery of the retort 11 is provided with heat-insulation layer, and retort 11 is provided with charging aperture 11-1, discharging opening 11-2 and emptying
Mouth 11-3.Charging aperture 11-1 is arranged on the upper end of retort 11, and discharging opening 11-2 and drain 11-3 are arranged on retort 11
Bottom.Feed zone, reaction zone and discharge zone are provided with inside retort 11, the feed zone is in top, reaction zone in middle part, discharging
Area is in bottom.
Sludge recirculation system 12 is outside retort 11, including hypomere pipeline, sludge reflux pump and epimere pipeline, hypomere pipe
Road is provided with check-valves.The hypomere pipeline of sludge recirculation system 12 is connected with the bottom of retort 11, the discharging of epimere pipeline
End is connected with the top of retort 11.Sludge reflux pump is arranged between hypomere pipeline and epimere pipeline, by sludge from reaction
The bottom of tank 11 is extracted out, is then reentered inside retort 11 from the top of retort 11.
The aerating system 13 includes aeration tube, aeration head, pressure gauge；Aeration tube is arranged in the bottom of retort 11；
Aeration head is evenly distributed on aeration tube and is communicated with aeration tube.Aeration head can provide micro-bubble, to increase connecing for liquid phase
Contacting surface is accumulated and time of contact, and aeration head quantity is relevant with its service area；Pressure gauge can monitor whether aeration head blocks,
So as to dredging in time.In initial reaction stage, organic sludge needs oxygen amount many to the present invention, and aeration rate needs to increase；The phase, organic after the reaction
Sludge oxidation demand is few, and aeration rate demand is few.Flowmeter can be also set up in the aerating system of this reactor, for adjusting aeration tube
Flow.
Temperature sensor 14 respectively sets one in the top of retort 11, middle part, bottom, to detect sludge in retort 11
Temperature.
Gas absorption treating device 15 is arranged on the top of retort 11, is communicated with the inside of retort 11 by pipeline.
The gas absorption treating device 15 is biomembrane absorbing and filtering device, can process H2S、SO2Deng sour gas.
Anaerobic fermentation reactor 2 includes retort 21, agitator 22, gas collection filter 23, temperature sensor 24, gas
Body probe tube 25 and circulating water line 26.
Retort 21 is provided with charging aperture 21-1, discharging opening 21-2 and drain 21-3, and charging aperture is arranged on retort 21
Top, discharging opening 21-2 is arranged on the middle part of retort 21, and drain 21-3 is arranged on the bottom of retort 21.
Three regions are set in retort 21, feed zone, reaction zone and discharge zone is divided into, feed zone is located at top, instead
Area is answered to be located at bottom, discharge zone is located at middle part.
Agitator 22 includes motor, bar axle and stirrer paddle, and motor is fixedly installed on the top of retort 21, and bar axle is from upper
Inside retort 21, stirrer paddle sets two-layer on bar axle, and wherein the stirrer paddle of lower floor is apart from retort 21
Bottom 30cm, the stirrer paddle on upper strata is arranged on the middle part of available depth in retort 21, and motor drives the rotation of two-layer blade
Stirring is sufficiently mixed to sludge in tank.Agitator 22 is not 24 hours always on, but is carrying out heat supply to retort 21
When just open, heat supply terminate after also stop stirring.
Gas collection filter 23 is arranged on the top of retort 21, is communicated with the inside of retort 21 by pipeline.Gas
Body de-entrainment filter 23 collects the methane gas produced in retort 21, is stored after being collected or burning is supplied retort 21
Heat.
Temperature sensor 24 respectively sets one in the top of retort 21, middle part, bottom, to detect the Nei Ge areas of retort 11
The temperature of the sludge in domain.
Gas sample tube 25 respectively sets one in the top of retort 21, middle part, bottom, to detect the Nei Ge areas of retort 11
The gas componant in domain.
Circulating water line 26 is arranged on the bottom of retort 21, is connected with boiler by pipeline, and the gas-cooker of boiler is by pipe
Road is connected with the gas outlet of gas collection filter 23.
High-temperature micro-aerobic-anaerobic digestion process is carried out using above-mentioned slaking apparatus to organic sludge to comprise the following steps：
1. tamed strain.
Take the municipal sludge that solid content is 5%~7% to be fitted into high-temperature micro-aerobic reactor 1, open sludge recirculation system 12
And aerating system 13, aerobic sigestion for a period of time, treat temperature rise, and reach balance after（Sludge temperature is not i.e. in retort 11
Rise again）, 1/2 sludge in retort 11 is discharged, the fresh sludge that solid content is 5%~7% is supplemented with, continue to run with, in repetition
Step is stated until temperature reaches 50 DEG C~55 DEG C in retort 11.Treat that temperature rises to more than 50 DEG C, stop aeration and sludge is returned
Stream, domestication terminates, and discharges a part of sludge, and 1/3 sludge is reserved in retort 11 as kind of a mud.
2. the high-temperature micro-aerobic digestion process of organic sludge.
Sludge delivery pump is opened, to 2/3 of feeding retort 11 in the retort 11 of self-heating high-temperature micro-aerobic reactor 1
Sludge fills reactor after the organic sludge of effective volume, organic sludge and reserved domestication, reaches effective volume, and reactor has
0.5m superelevation；4%~7%, volatility organic solid concentration accounts for 60%~80% to organic sludge solid content；Open sludge recirculation system
12 and aerating system 13, the aeration rate of aerating system 13 is 10~14m3/ h, organic sludge starts high-temperature micro-aerobic digestion process.
Sludge is stopped in self-heating high-temperature micro-aerobic reactor and carries out high-temperature micro-aerobic digestion process in 2~3 days.High-temperature micro-aerobic digests
During, oxidation-reduction potential ORP is 0~-100mv.
In digestion process, sludge aerobic digestion process is no more than 30% mechanical energy from heat release, sludge reflux supply, together
When heat-insulation layer is provided with due to the periphery of the reactor body of self-heating high-temperature micro-aerobic reactor 1 so that digestion temperature is without outer
Heating source, maintains between 45 DEG C~65 DEG C, and organic sludge is sterilized at these elevated temperatures, and sludge is harmless after realizing digestion
Change.If temperature of reactor rises to more than 65 DEG C, aeration rate is increased, close sludge reflux so that radiating increases, to realize drop
Temperature.
Because the sludge concentration in input reactor is high, viscosity is big, and oxygen demand is more, and mass transfer has into the oxygen amount of reactor
Limit, therefore be not exclusively aerobic in self-heating high-temperature micro-aerobic reactor, i.e., it is total to by aerobic bacteria, amphimicrobe, anaerobic bacteria
Same-action degrades volatile organic matter, it is easy to produce volatile fatty acid（VFA）, and VFA is under anaerobic, it is easy to
Methane phase, thus organic sludge high-temperature micro-aerobic digestion process beneficial to back segment organic sludge anaerobic digestion process.
After high-temperature micro-aerobic digestion terminates, postdigestive sludge enters pH value regulating reservoir 3 from discharging opening by pipeline, to pH
Sodium hydroxide solution is put into value regulating reservoir 3, the pH value of the material in pH value regulating reservoir 3 is transferred between 6.8~7.2.PH value
Sludge after regulation is finished stops 3h~5h to discharge the dissolved oxygen in sludge in pond.
3. the mesophilic anaerobic digestion of organic sludge.
Sludge pump is opened, 2. step discharges the sludge by high-temperature micro-aerobic digestion of dissolved oxygen by being pumped into anaerobic fermentation
In reactor 2.Sludge is stopped 10~20 days in anaerobic fermentation reactor 2 and completes anaerobic digestion process, without external heat source, in
Warm anaerobism temperature is 33 DEG C~35 DEG C, and discharge mud is directly agricultural after mechanical dehydration.
If the sludge temperature flowed out after the digestion of self-heating high-temperature micro-aerobic is too high, more than 60 DEG C, high-temperature micro-aerobic is digested
Stop several hours in pH value regulating reservoir 3 of sludge afterwards is radiated more.If anaerobic pond temperature does not reach mesophilic range, can be by self-heating
The sludge temperature of formula high-temperature micro-aerobic digestion is tried one's best raisings, and machinery heat is given by reducing aeration rate, increasing sludge reflux so that
High-temperature micro-aerobic digestion temperature reaches 50 DEG C~60 DEG C, it is ensured that the middle temperature of anaerobic pond.
Slaking apparatus of the invention belong to two-stage series connection reactor, and self-heating high-temperature micro-aerobic reactor passes through sludge reflux
Mixing is stirred, is mixed without dead angle, reach sludge suspension effect, promote microbial biochemical reaction, make microorganism autoxidation
Reaction is complete, in self-heating high-temperature micro-aerobic reactor, discharges enough heats by micro- aerobic sigestion, it is ensured that micro- aerobic reaction
The middle temperature state of sludge in the condition of high temperature and anaerobic fermentation reactor of device.
During actual motion, marker method is fed using semi continuous.The digestion of self-heating high-temperature micro-aerobic is dirty in the present embodiment
The mud residence time is 2 days, and anaerobically digested sludge is stopped 12 days.
If self-heating high-temperature micro-aerobic digestion reactor effective volume is V, first day inputiing mud volume is V/2, is stopped two days, the
Enter within three days mud V/2, spoil disposal V/2.Enter mud and spoil disposal every other day.From self-heating high-temperature micro-aerobic digestion reactor, mud is discharged daily
V, into anaerobic digester, anaerobic digester volume is 12V, so, sludge retention time is 12 days.Anaerobic digester is arranged daily
Mud amount V.So enter mud and spoil disposal is equal.
For the digestion of self-heating high-temperature micro-aerobic, due to being self-heating, temperature rises and is not easy, so in the present embodiment
Reactor volume is 10m3.The self-heating high-temperature micro-aerobic digestion phase temperature of the present embodiment can reach between 45 DEG C~65 DEG C,
Though winter can be relatively low, because the big most low energy of reactor volume maintains 50 DEG C.
Organic sludge high-temperature micro-aerobic-anaerobic digestion process of the invention make use of self-heating high-temperature micro-aerobic digestible energy
The advantage of oneself heat production, is not required to external heat source, cost-effective.
The anaerobic fermentation of slaking apparatus of the invention is mesophilic digestion, and sludge is carried in make use of self-heating high-temperature micro-aerobic
Heat, be not required to external heat source, it is cost-effective.Anaerobic fermentation reactor can produce the methane gas with energy substance, carry out
Recycling；And sludge remains nitrogen and phosphorus composition after digesting, can be solved sludge and finally go out with agricultural after dehydration
Road.
（Embodiment 2）
Remaining is same as Example 1 for the organic sludge high-temperature micro-aerobic-anaerobic digestion device of the present embodiment, and difference exists
In：
3. organic sludge carries out thermophilic digestion to step.
The valve of connecting pipe is opened, 2. step discharges the sludge by high-temperature micro-aerobic digestion of dissolved oxygen by being pumped into
In anaerobic fermentation reactor 2.Sludge is stopped 6~10 days in anaerobic fermentation reactor 2 and completes anaerobic digestion process, high temperature anaerobic
The temperature of digestion is 50 DEG C~55 DEG C, and discharge mud is directly agricultural after mechanical dehydration.
Thermophilic digestion can cause that reaction speed is accelerated.Thermophilic digestion thermal source a part from leading portion from
The heat that the sludge of hot type high-temperature micro-aerobic outflow is carried, the source of another part thermal source is the first for producing thermophilic digestion
Alkane collect after-burning heat up water the steam that obtains or hot water by the circulating water line 26 in anaerobic fermentation reactor 2 in retort 21
Sludge heat supply maintaining 50 DEG C~55 DEG C of high temperature.
When the temperature drop of anaerobic fermentation reactor 2, to conveying steam in circulating water line 26 or hot water with to reaction
Sludge heat supply in tank 21, agitator 22 is opened while 26 heat supply of circulating water line makes heat be uniformly dispersed, and heat supply terminates to stop
Only stir.
（Embodiment 3）
Remaining is same as Example 1 for the organic sludge high-temperature micro-aerobic-anaerobic digestion device of the present embodiment, and difference exists
In：
Self-heating high-temperature micro-aerobic reactor 1 also includes defoaming system, and the defoaming system includes air froth breaking pipe, injection
Mouthful；The air froth breaking pipe is arranged in the top of retort 11, and uniformly aperture is provided with tube wall；The jet is arranged on reaction
The top of device body.When this defoaming system works, the gas blown out by the aperture on air froth breaking tube wall is smashed foam；
The sprayable defoamer of jet, defoamer is ejected into reactor, is distributed on whole liquid level by stirring for agitator,
Play froth breaking.
The step of digestion method, defoaming system was sent into in retort 2. in the high-temperature micro-aerobic digestion process of organic sludge
Air breaks the bubble produced in retort so that digestion process is smoothed out.
Claims (3)
1. a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion process, it is characterised in that：Equipment therefor reacts including high-temperature aerobic
Device and anaerobic fermentation reactor（2）, also including pH value regulating reservoir（3）；The high-temperature aerobic reactor is that self-heating high temperature is micro- good
Oxygen reactor（1）；PH value regulating reservoir（3）It is arranged on high-temperature micro-aerobic reactor（1）And anaerobic fermentation reactor（2）Between, from
Hot type high-temperature micro-aerobic reactor（1）Discharging opening by pipeline and pH value regulating reservoir（3）Communicate, pH value regulating reservoir（3）Pass through
Pipeline and pump and anaerobic fermentation reactor（2）Charging aperture be connected；
Self-heating high-temperature micro-aerobic reactor（1）Including retort（11）, sludge recirculation system（12）, aerating system（13）, temperature
Degree sensor（14）With gas absorption treating device（15）；The sludge recirculation system（12）It is arranged on retort（11）Outside,
Including hypomere pipeline, sludge reflux pump and epimere pipeline；Hypomere pipeline, sludge reflux pump, epimere pipeline and retort form one
The individual loop for communicating；Aerating system（13）Aeration tube, aeration head, pressure gauge are included, aeration tube is arranged in retort（11）'s
Bottom；Temperature sensor（14）In retort（11）Top, middle part, bottom respectively set one；Gas absorption treating device
（15）It is arranged on retort（11）Top, by pipeline and retort（11）Inside communicate；
The digestion method of organic sludge high-temperature micro-aerobic-anaerobic digestion device is comprised the following steps：
1. tamed strain, tamed strain is in self-heating high-temperature micro-aerobic reactor（1）Retort（11）In carry out, domestication
The kind mud containing strain for obtaining stays 1/4~1/2 in retort（11）It is internal；
2. the high-temperature micro-aerobic digestion process of organic sludge；Sludge delivery pump is opened, to self-heating high-temperature micro-aerobic reactor（1）
Retort（11）Middle feeding organic sludge, the organic sludge be solid content 4%~7%, volatility organic solid concentration is accounted for
60%~90% liquid organic solid castoff；The conveying capacity of organic sludge is retort（11）Remaining effective volume；Open
Sludge recirculation system（12）And aerating system（13）, organic sludge starts high-temperature micro-aerobic digestion process, and sludge is high in self-heating
Stopped in the micro- aerobic reactor of temperature 2~3 days and complete high-temperature micro-aerobic digestion process；Digestion temperature maintain 45 DEG C~65 DEG C it
Between；Self-heating high-temperature micro-aerobic reactor（1）Retort（11）In oxidation-reduction potential ORP be 0~-100mv；
After high-temperature micro-aerobic digestion terminates, postdigestive sludge enters pH value regulating reservoir from discharging opening by pipeline（3）, to pH value
Regulating reservoir（3）Middle input alkali lye, by pH value regulating reservoir（3）In the pH value of material be transferred between 6.8~7.2, pH value has been adjusted
Sludge after finishing stops 3~5h to discharge the dissolved oxygen in sludge in pond；
3. the anaerobic digestion process of organic sludge；2. step discharges the sludge by high-temperature micro-aerobic digestion of dissolved oxygen by pumping
Enter anaerobic fermentation reactor（2）Stop and complete within 6~20 days anaerobic digestion process, discharge mud is directly agricultural after mechanical dehydration；Detest
Oxygen digestion process is mesophilic anaerobic digestion process or thermophilic digestion process；Anaeration in normal temperature temperature is 33 DEG C~35 DEG C, sludge
In anaerobic fermentation reactor（2）Middle stop 10~20 days completes anaerobic digestion process；The temperature of thermophilic digestion be 50 DEG C~
55 DEG C, sludge is in anaerobic fermentation reactor（2）Middle stop 6~10 days completes anaerobic digestion process.
2. organic sludge high-temperature micro-aerobic-anaerobic digestion process according to claim 1, it is characterised in that：Anaerobic digestion
When process is mesophilic anaerobic digestion process, if the sludge temperature flowed out after the digestion of self-heating high-temperature micro-aerobic is more than 60 DEG C, by height
Sludge after the micro- aerobic sigestion of temperature is in pH value regulating reservoir（3）Middle 0~40min of extended residence time radiates to anaeration in normal temperature temperature model
Enclose；If anaerobic pond temperature does not reach anaeration in normal temperature temperature range, reduce the aeration rate of high-temperature micro-aerobic digestion, increase sludge time
Flow to mechanical heat so that high-temperature micro-aerobic digestion temperature reaches 50 DEG C~60 DEG C, it is ensured that the middle temperature of anaerobic pond.
3. organic sludge high-temperature micro-aerobic-anaerobic digestion process according to claim 1, it is characterised in that：Anaerobic digestion
Process be thermophilic digestion process when, thermophilic digestion process produce methane gas collect and after-combustion produce steam or
Hot water is to anaerobic fermentation reactor（2）Heat supply to maintain 50 DEG C~55 DEG C of high temperature, the steam or hot water that methyl hydride combustion is produced
By anaerobic fermentation reactor（2）The circulating water line of bottom（26）To anaerobic fermentation retort（21）Heat supply, while opening is detested
Aerobe fermentation retort（21）Agitator.
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| CN105032924B (en) * | 2015-08-06 | 2017-08-25 | 同济大学 | It is a kind of to improve the high technique containing solid anaerobically digested sludge land use performance |
| CN105110590A (en) * | 2015-09-17 | 2015-12-02 | 昆明滇池水务股份有限公司 | Method and device for intensifying high-temperature hydrolysis acidification of excess sludge from sewage treatment plant through aeration |
| CN105647786A (en) * | 2016-01-05 | 2016-06-08 | 江苏理工学院 | Kitchen waste anaerobic-high temperature microaerobic digestion device and method |
| CN106865757B (en) * | 2017-01-24 | 2020-05-05 | 南京大学 | Sewage anaerobic treatment reactor heating system based on direct-fired absorption heat pump |
| CN106865759A (en) * | 2017-03-06 | 2017-06-20 | 南京大学 | A kind of UASB reactor assemblies with self-heating function |
| CN110468033B (en) * | 2019-08-26 | 2020-12-08 | 同济大学 | Anaerobic digestion device for strengthening methane production by utilizing self-sustaining air flotation |
| CN111170462B (en) * | 2020-03-16 | 2021-05-28 | 南京大学 | Alternate starvation micro-aerobic anaerobic coupling filler sludge side flow in-situ reduction strengthening process |
| CN114315073A (en) * | 2021-12-15 | 2022-04-12 | 福建龙净环保股份有限公司 | Starting method of anaerobic digestion reactor |
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| JP2003033780A (en) * | 2001-07-25 | 2003-02-04 | Mitsubishi Kakoki Kaisha Ltd | Method for wastewater treatment |
| CN102070286A (en) * | 2010-11-23 | 2011-05-25 | 广东工业大学 | Method for improving sludge anoxic/aerobic digestion property by utilizing ultrasonic pretreatment |
| CN103304118A (en) * | 2012-03-15 | 2013-09-18 | 李铀 | High-pressure digestion and blasting dehydration process of sludge |
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| JP3636035B2 (en) * | 2000-05-24 | 2005-04-06 | 栗田工業株式会社 | Digestion method of organic sludge |
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| CN100486722C (en) * | 2006-06-15 | 2009-05-13 | 张相锋 | Technique of producing fertilizer, producing gas by digesting organic waste in semi-solid state in two phases |
| CN100500601C (en) * | 2006-12-01 | 2009-06-17 | 华南理工大学 | Sludge hot digesting apparatus for preparing biological solid |
| CN101659506A (en) * | 2009-09-17 | 2010-03-03 | 江苏技术师范学院 | Integrated organic sludge high-temperature micro-aerobic horizontal digestion reactor |
| CN202081089U (en) * | 2011-02-25 | 2011-12-21 | 上海济兴能源环保技术有限公司 | Baffling high-concentration anaerobic fermentation device |
| CN203878041U (en) * | 2014-02-26 | 2014-10-15 | 江苏理工学院 | Organic sludge high-temperature microaerobic-anaerobic digestion device |
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|---|---|---|---|---|
| JP2003033780A (en) * | 2001-07-25 | 2003-02-04 | Mitsubishi Kakoki Kaisha Ltd | Method for wastewater treatment |
| CN102070286A (en) * | 2010-11-23 | 2011-05-25 | 广东工业大学 | Method for improving sludge anoxic/aerobic digestion property by utilizing ultrasonic pretreatment |
| CN103304118A (en) * | 2012-03-15 | 2013-09-18 | 李铀 | High-pressure digestion and blasting dehydration process of sludge |
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