CN103803770B - Organic sludge high-temperature micro-aerobic-anaerobic digestion device and method - Google Patents
Organic sludge high-temperature micro-aerobic-anaerobic digestion device and method Download PDFInfo
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- CN103803770B CN103803770B CN201410067635.3A CN201410067635A CN103803770B CN 103803770 B CN103803770 B CN 103803770B CN 201410067635 A CN201410067635 A CN 201410067635A CN 103803770 B CN103803770 B CN 103803770B
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- 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
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- 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
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- 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 device and method, first organic sludge carries out high-temperature micro-aerobic digestive process, after high-temperature micro-aerobic digestion terminates, postdigestive mud enters pH value equalizing tank from discharge port by pipeline, in pH value equalizing tank, drop into the pH of material in alkali lye equalizing tank, mud stops 3 ~ 5h to discharge the dissolved oxygen in mud in pond; Then mud completes anaerobic digestion process in 6 ~ 20 days by being pumped into anaerobic fermentation reactor stop.The first half section of organic sludge digestive process of the present invention is autothermal high-temperature micro-aerobic digestive process, instead of ATAD process; The air capacity of autothermal high-temperature micro-aerobic digestive process supply is limited, under oxygen restricted condition, be easy to produce VFA, and VFA under anaerobic, is easy to methane phase; So both be beneficial to the further digestion of second half section anaerobic digestion process to mud and produce methane, can aeration rate be reduced again, reduce energy consumption.
Description
Technical field
The present invention relates to the process field of solid waste, be specifically related to a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion device and method.
Background technology
Along with the development of Chinese society economy and urbanization, the quantity of municipal effluent is in continuous growth.It is predicted, within 2010, China's urban wastewater discharge will reach 44,000,000,000 m
3/ d; The year two thousand twenty will reach 53,600,000,000 m
3/ d.Although current wastewater treatment in China amount and processing rate not high, municipal sewage plant discharges about 300,000 tons of dewatered sludge every year, but also with annual 10% speed increment
[2]., there is the light mud phenomenon of heavy water in existing sewage work of China, has mud greatly not have stabilization treatment and harmless treatment, sludge treatment facilities does not also effectively run, mud is not properly disposed, and causes environmental pollution, inhibits the long-term sustainable of municipal wastewater treatment plant to develop.At present, how effectively processing municipal sludge is face in dirty (giving up) water treatment field in international coverage the most important and the problem of complexity.
Sludge digestion technology to be degraded the stabilization that reaches mud and innoxious to organism by microorganism.Existing sludge digestion technique mainly contains traditional aerobic sigestion technique, conventional mesophilic anaerobic digestion technique, two-stage anaerobic digestion technique, anoxic/aerobic sigestion technique, autothermal thermophilic aerobic digestion technique, two sections of high-temperature aerobic/mesophilic anaerobic digestion techniques.
Autothermal thermophilic aerobic digestion technique combines with mesophilic anaerobic digestion technique by two sections of high-temperature aerobics/mesophilic anaerobic digestion technique wherein, enters anaeration in normal temperature reactor again after first carrying out pre-treatment with one section of high loading autothermal thermophilic aerobic digestion process system to mud.This technique can significantly improve the stability run clearance and the follow-up mesophilic anaerobic digestion of pathogenic bacteria, but this technique is still in the experimental phase.
Such as Chinese patent literature CN 100486722C(application number 200610087577.6) disclose a kind of two benches semi-solid state organic waste digestion composting gas-made technology, semi-solid state organic waste are digested under the high-temperature micro-aerobic and anaeration in normal temperature condition of series connection, hot stage kills pathogenic bacterium, predecomposition refuse, the main decomposition refuse of middle thermophase, generation biogas, final product is rich in humic acid, nitrogen, phosphorus, potassium; Concrete steps are that first semi-solid state organic waste enter high-temperature micro-aerobic digestion unit, air is passed in high-temperature micro-aerobic digestion unit, maintain the dissolved oxygen concentration of semi-solid waste in high-temperature micro-aerobic digestion unit at 0.1 ~ 0.8mg/L, semi-solid state organic waste start under microbial process to decompose again, consume oxygen and release reaction is warm, Digestive system temperature can reach more than 55 DEG C, maintains Digestive system temperature 55 DEG C ~ 70 DEG C and keeps 1 ~ 3 day; After the quiet interchanger cooling of high temperature fluid that high-temperature micro-aerobic digestion unit is discharged, enter the mesophilic anaerobic digestion unit of subordinate phase, the used heat that interchanger reclaims is that carrier is incubated mesophilic anaerobic digestion unit with recirculated water; Mesophilic anaerobic digestion cell temperature maintains 35 DEG C ~ 40 DEG C, pH value maintains 6.5 ~ 8, and the easy degradation material in Digestive system is constantly converted into biogas, and subordinate phase is after 15 ~ 20 days, digestion final product from mesophilic anaerobic digestion unit discharge, enter precipitation reservoir for subsequent use or sell.
There is the problem of oxygenation difficulty in the high-temperature micro-aerobic stage of this preparation technology, in actual job, under the hot conditions of 55 DEG C ~ 70 DEG C, dissolved oxygen concentration is very low, and semisolid material oxygen transfer efficiency is low, oxygenation is very limited, therefore the method is difficult to reach oxygen condition according to content disclosed in text, and aerobic condition cannot be reached, first stage cannot discharge enough heats, the easy anaerobic acidification of organic solid, and the sludge pH flowed out from the first stage is lower, cause subordinate phase anaerobic digestion process to produce biogas, and the anaerobic digestion residence time is long; In addition according to the method disclosed content at present, mesophilic anaerobic digestion temperature is more difficult controls to target temperature, this is because the waste heat low (temperature difference heat of namely 55 DEG C ~ 70 DEG C to 35 DEG C ~ 40 DEG C is little) that interchanger reclaims, is difficult to reach insulation effect; Anaerobic pond due to the residence time long, bulky, reach insulation effect effect by interchanger in the winter time just lower.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion device and method.
The technical scheme realizing the object of the invention is a kind of organic sludge high-temperature micro-aerobic-anaerobic digestion device, comprises high-temperature aerobic reactor and anaerobic fermentation reactor, also comprises pH value equalizing tank; Described high-temperature aerobic reactor is autothermal high-temperature micro-aerobic reactor; PH value equalizing tank is arranged between high-temperature micro-aerobic reactor and anaerobic fermentation reactor, the discharge port of autothermal high-temperature micro-aerobic reactor is communicated with pH value equalizing tank by pipeline, and pH value equalizing tank is connected with the opening for feed of anaerobic fermentation reactor with pump by pipeline.
Autothermal high-temperature micro-aerobic reactor comprises retort, sludge recirculation system, aerating system, temperature sensor and gas absorption treating device; Described sludge recirculation system is arranged on retort outside, comprises hypomere pipeline, sludge reflux pump and epimere pipeline; Hypomere pipeline, sludge reflux pump, epimere pipeline and retort form a loop communicated; Aerating system includes aeration tube, aeration head, tensimeter, and aeration tube is arranged in the bottom of retort; Temperature sensor respectively arranges one in the top of retort, middle part, bottom; Gas absorption treatment unit is arranged on the top of retort, is communicated with the inside of retort by pipeline.
Described anaerobic fermentation reactor comprises retort, agitator, collection and confinement of gases strainer, temperature sensor, gas sampling tube and circulating water line.Agitator comprises motor, bar axle and agitating vane, motor is fixedly installed on the top of retort, bar axle penetrates retort inside from the top down, agitating vane arranges two-layer on bar axle, wherein the agitating vane of lower floor is arranged on the bottom of retort, and the agitating vane on upper strata is arranged on the middle part of available depth in retort.
Circulating water line is arranged on bottom retort, is connected with boiler by pipeline, and the gas-cooker of boiler is connected by the air outlet of pipeline with collection and confinement of gases strainer.
A digestion method for organic sludge high-temperature micro-aerobic-anaerobic digestion device as above, comprises the following steps:
1. tamed strain, tamed strain carries out in the retort of autothermal high-temperature micro-aerobic reactor, and the kind mud containing bacterial classification that domestication obtains stays 1/4 ~ 1/2 in retort inside.
2. the high-temperature micro-aerobic digestive process of organic sludge; Open sludge delivery pump, in the retort of autothermal high-temperature micro-aerobic reactor, send into organic sludge, the operational throughput of organic sludge is the residue effective volume of retort; Open sludge recirculation system and aerating system, organic sludge starts high-temperature micro-aerobic digestive process, and mud stops and completes high-temperature micro-aerobic digestive process in 2 ~ 3 days in autothermal high-temperature micro-aerobic reactor; Digestion temperature maintains between 45 DEG C ~ 65 DEG C.
After high-temperature micro-aerobic digestion terminates, postdigestive mud enters pH value equalizing tank from discharge port by pipeline, alkali lye is dropped in pH value equalizing tank, be transferred between 6.8 ~ 7.2 by the pH value of the material in pH value equalizing tank, the mud after pH value regulates stops 3 ~ 5h to discharge the dissolved oxygen in mud in pond.
3. the anaerobic digestion process of organic sludge; The mud through high-temperature micro-aerobic digestion that 2. step discharges dissolved oxygen completes anaerobic digestion process in 6 ~ 20 days by being pumped into anaerobic fermentation reactor stop, and discharge mud is directly agricultural after mechanical dehydration.
In the high-temperature micro-aerobic digestive process of above-mentioned steps 2. organic sludge, the redox potential ORP in the retort of autothermal high-temperature micro-aerobic reactor is 0 ~-100mv.
The anaerobic digestion process of above-mentioned steps 3. organic sludge is mesophilic anaerobic digestion process; Anaeration in normal temperature temperature is 33 DEG C ~ 35 DEG C, and mud stops and completes anaerobic digestion process in 10 ~ 20 days in anaerobic fermentation reactor.
Further, if the mud temperature flowed out after the digestion of autothermal high-temperature micro-aerobic is more than 60 DEG C, postdigestive for high-temperature micro-aerobic mud extended residence time 0 ~ 40min in pH value equalizing tank is dispelled the heat 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, strengthen sludge reflux to mechanical heat, make high-temperature micro-aerobic digest temperature and reach 50 DEG C ~ 60 DEG C, ensure the middle temperature of anaerobic pond.
Selectable, the anaerobic digestion process of step 3. organic sludge is thermophilic digestion process; The temperature of thermophilic digestion is 50 DEG C ~ 55 DEG C, and mud stops and completes anaerobic digestion process in 6 ~ 10 days in anaerobic fermentation reactor.
Further, the methane gas that thermophilic digestion process produces is collected and afterfire produces steam or hot water to anaerobic fermentation reactor heat supply with the high temperature maintaining 50 DEG C ~ 55 DEG C, the steam produce methyl hydride combustion or hot water to retort heat supply, open the agitator of retort by the circulating water line bottom anaerobic fermentation reactor simultaneously.
Step 2. in organic sludge be solid content 4% ~ 7%, volatility organic solid concentration accounts for the liquid organic solid castoff of 60% ~ 90%.
The present invention has positive effect: (1) organic sludge autothermal high-temperature micro-aerobic-anaerobic digestion device of the present invention is in series by autothermal high-temperature micro-aerobic reactor and anaerobic fermentation reactor.Leading portion autothermal high-temperature micro-aerobic reactor passes through Insulation, the heat discharged in volatile organic matter aerobic sigestion process is incubated, add mechanical heat production, thus make reactor reach from being warming up to 45 DEG C ~ 65 DEG C, ensure that high-temperature micro-aerobic digestion is carried out smoothly.
Selectablely in back segment anaerobic fermentation reactor carry out mesophilic digestion or thermophilic digestion, wherein mesophilic anaerobic digestion make use of the heat that mud that autothermal high-temperature micro-aerobic reactor flows out carries, and does not need external heat source, saves cost; And the heat that a part of mud flowed out from the autothermal high-temperature micro-aerobic of leading portion of the thermal source of thermophilic digestion carries, the source of another part thermal source is that the methane that combustion high temperature anaerobic digestion produces obtains, and does not need external heat source equally, saves cost.Anaerobic fermentation reactor can produce the methane gas with energy substance, has carried out recycling; And mud remains nitrogen and phosphorus composition after digestion, can be agricultural after dehydration, solve the final outlet of mud.
(2) autothermal high-temperature micro-aerobic digestive process of the present invention ensure into the solid content of mud be 4% ~ 7%, reactor volume is greater than 10m
3above and suitable aeration rate is set and good mixing effect is provided, in digestive process, the heat of aerobic sigestion reaction release is remained simultaneously, and the mechanical energy of 30% is no more than by sludge reflux supply, thus reactor is reached and maintains the condition of high temperature of 45 DEG C ~ 65 DEG C, high-temperature micro-aerobic has been digested more effectively, thoroughly.Owing to being micro-aerobic sigestion process, aeration rate is few relative to aerobic sigestion, and in reactor, mud is difficult to reach more than 70 degree from heating up; And for organic sludge high-temperature micro-aerobic-anaerobic digestion process, there are some researches show, when the digestion temperature of autothermal high-temperature micro-aerobic digestion process is more than 65 DEG C, the deleterious of whole digestive process, is in particular in that VSS clearance is lower, is 20% ~ 30%.
(3) the first half section of organic sludge digestive process of the present invention is autothermal high-temperature micro-aerobic digestive process, instead of ATAD process; The air capacity of autothermal high-temperature micro-aerobic digestive process supply is limited, under oxygen restricted condition, be easy to produce voltaile fatty acid (hereinafter referred to as VFA), and VFA under anaerobic, is easy to methane phase; So both be beneficial to the further digestion of second half section anaerobic digestion process to mud and produce methane, can aeration rate be reduced again, reduce energy consumption.Due to autothermal high-temperature micro-aerobic digestive process during first half section, accelerate anaerobic digestion process, general anaerobic digestion will reach more than 40 day, or the longer time, but within this process residence time can reach and shorten to 20 days.
(4) the present invention is applicable to solid content 4% ~ 7%, and volatility organic solid concentration accounts for the liquid organic solid castoff of 60% ~ 90%, as the organic waste of municipal sludge, the discharge of poultry farming factory, more than kitchen, the liquid state organics such as animals ight soil.Because the sludge concentration dropped in reactor is high, viscosity is large, oxygen requirement is many, and the oxygen amount that mass transfer enters reactor is limited, is therefore not exclusively aerobic in autothermal high-temperature micro-aerobic reactor, namely by the acting in conjunction of aerobic bacteria, amphimicrobe, anerobe, volatile organic matter is degraded, then anaerobic reactor fermentation methane phase is entered, after digestion, mud is through dehydration, can be used as the organic solid of fertilizer, solves the final problem of outlet of organic sludge.
(5) the postdigestive mud of autothermal high-temperature micro-aerobic of the present invention adjust ph discharge dissolved oxygen in pH value equalizing tank, because autothermal high-temperature micro-aerobic digestible energy produces a large amount of VFA, for anaerobic digestion process methane phase, but VFA can cause pH value to decline, so, before entering anaerobic pond, alkali lye be added, pH value in anaerobic digester is transferred between 6.8 ~ 7.2, does not exceed 7.5.In addition, mixing pit will stay for some time, and is because the mud flowed out from autothermal high-temperature micro-aerobic digester, is with some dissolved oxygen, needs to discharge, can not be brought into anaerobic pond, otherwise can kill anerobe.PH value equalizing tank also plays preparing pool effect, is convenient to pump and is taken out from pH value equalizing tank by mud, be pumped in anaerobic fermentation reactor.
(6) slaking apparatus compact construction of the present invention, simple to operate, can be built on the ground, also can be buried or half buried, saves the area, beautifies the environment.
Accompanying drawing explanation
Fig. 1 is the structural representation of slaking apparatus of the present invention;
Mark in above-mentioned accompanying drawing is as follows:
High-temperature micro-aerobic reactor 1, retort 11, opening for feed 11-1, discharge port 11-2, drain 11-3, sludge recirculation system 12, aerating system 13, temperature sensor 14, gas absorption treatment unit 15;
Anaerobic fermentation reactor 2, retort 21, opening for feed 21-1, discharge port 21-2, drain 21-3, agitator 22, collection and confinement of gases strainer 23, temperature sensor 24, gas sampling tube 25, circulating water line 26; PH value equalizing tank 3.
Embodiment
(embodiment 1)
See Fig. 1, the organic sludge high-temperature micro-aerobic-anaerobic digestion device of the present embodiment comprises autothermal high-temperature micro-aerobic reactor 1, anaerobic fermentation reactor 2 and pH value equalizing tank 3.PH value equalizing tank 3 is arranged between high-temperature micro-aerobic reactor 1 and anaerobic fermentation reactor 2, the discharge port of autothermal high-temperature micro-aerobic reactor 1 is communicated with pH value equalizing tank 3 by pipeline, and pH value equalizing tank 3 is connected with the opening for feed of pump with anaerobic fermentation reactor 2 by pipeline.
Autothermal high-temperature micro-aerobic reactor 1 comprises retort 11, sludge recirculation system 12, aerating system 13, temperature sensor 14 and gas absorption treating device 15.
The periphery of described retort 11 is provided with thermal insulation layer, and retort 11 is provided with opening for feed 11-1, discharge port 11-2 and drain 11-3.Opening for feed 11-1 is arranged on the upper end of retort 11, and discharge port 11-2 and drain 11-3 is arranged on the bottom of retort 11.Retort 11 inside is provided with intake zone, reaction zone and discharge zone, described intake zone on top, reaction zone at middle part, discharge zone is in bottom.
Sludge recirculation system 12 is outside in retort 11, and comprise hypomere pipeline, sludge reflux pump and epimere pipeline, hypomere pipeline is provided with vacuum breaker.The hypomere pipeline of sludge recirculation system 12 is connected with the bottom of retort 11, and the discharge end of epimere pipeline is connected with the top of retort 11.Sludge reflux pump is arranged between hypomere pipeline and epimere pipeline, is extracted out the bottom of mud from retort 11, then reenters retort 11 from the top of retort 11 inner.
Described aerating system 13 includes aeration tube, aeration head, tensimeter; Aeration tube is arranged in the bottom of retort 11; Aeration head to be evenly distributed on aeration tube and to communicate with aeration tube.Aeration head can provide micro-bubble, and to increase contact area and the duration of contact of liquid phase, aeration head quantity is relevant with its service area; Whether tensimeter can monitor aeration head and block, to dredge in time.The present invention is in initial reaction stage, and organic sludge needs oxygen amount many, and aeration rate needs to strengthen; Phase after the reaction, organic sludge oxygen requirement is few, and aeration rate demand is few.Also can set up under meter in the aerating system of this reactor, be used for regulating the flow of aeration tube.
Temperature sensor 14 respectively arranges one in the top of retort 11, middle part, bottom, with the temperature of mud in detection reaction tank 11.
Gas absorption treatment unit 15 is arranged on the top of retort 11, is communicated by the inside of pipeline with retort 11.Described gas absorption treatment unit 15 is microbial film absorbing and filtering device, can process H
2s, SO
2deng sour gas.
Anaerobic fermentation reactor 2 comprises retort 21, agitator 22, collection and confinement of gases strainer 23, temperature sensor 24, gas sampling tube 25 and circulating water line 26.
Retort 21 is provided with opening for feed 21-1, discharge port 21-2 and drain 21-3, and opening for feed is arranged on the top of retort 21, and discharge port 21-2 is arranged on the middle part of retort 21, and drain 21-3 is arranged on the bottom of retort 21.
Establish three regions in retort 21, be divided into intake zone, reaction zone and discharge zone successively, intake zone is located at top, and reaction zone is located at bottom, and discharge zone is located at middle part.
Agitator 22 comprises motor, bar axle and agitating vane, motor is fixedly installed on the top of retort 21, it is inner that bar axle penetrates retort 21 from the top down, agitating vane arranges two-layer on bar axle, the wherein bottom 30cm of the agitating vane distance retort 21 of lower floor, the agitating vane on upper strata is arranged on the middle part of available depth in retort 21, and the two-layer blade of driven by motor rotates the abundant mix and blend of mud in tank.Agitator 22 is not 24 hours direct-opens, but just opens when carrying out heat supply to retort 21, also stops stirring after heat supply terminates.
Collection and confinement of gases strainer 23 is arranged on the top of retort 21, is communicated by the inside of pipeline with retort 21.The methane gas produced in retort 21 collected by collection and confinement of gases strainer 23, and after being collected, storage or burning are to retort 21 heat supply.
Temperature sensor 24 respectively arranges one in the top of retort 21, middle part, bottom, with the temperature of the mud in region each in detection reaction tank 11.
Gas sampling tube 25 respectively arranges one in the top of retort 21, middle part, bottom, with the gaseous constituent in region each in detection reaction tank 11.
Circulating water line 26 is arranged on bottom retort 21, is connected with boiler by pipeline, and the gas-cooker of boiler is connected by the air outlet of pipeline with collection and confinement of gases strainer 23.
Use above-mentioned slaking apparatus to carry out high-temperature micro-aerobic-anaerobic digestion process to organic sludge to comprise the following steps:
1. tamed strain.
Getting solid content is in the municipal sludge loading high-temperature micro-aerobic reactor 1 of 5% ~ 7%, open sludge recirculation system 12 and aerating system 13, aerobic sigestion for some time, treat that temperature rises, and after reaching balance (namely in retort 11, mud temperature no longer rises), 1/2 mud in discharge retort 11, more supplementary solid content is the fresh sludge of 5% ~ 7%, continue to run, repeat above-mentioned steps 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 reflux, domestication terminates, and discharges a part of mud, and in retort 11, reserved 1/3 mud is as kind of a mud.
2. the high-temperature micro-aerobic digestive process of organic sludge.
Open sludge delivery pump, send into the organic sludge of 2/3 effective volume of retort 11 in the retort 11 of autothermal high-temperature micro-aerobic reactor 1, after organic sludge and reserved domestication, mud fills reactor, and reach effective volume, reactor has 0.5m superelevation; Organic sludge solid content is 4% ~ 7%, and volatility organic solid concentration accounts for 60% ~ 80%; Open sludge recirculation system 12 and aerating system 13, the aeration rate of aerating system 13 is 10 ~ 14m
3/ h, organic sludge starts high-temperature micro-aerobic digestive process.Mud stops and carries out high-temperature micro-aerobic digestive process in 2 ~ 3 days in autothermal high-temperature micro-aerobic reactor.In high-temperature micro-aerobic digestive process, redox potential ORP is 0 ~-100mv.
In digestive process, sludge aerobic digestive process is from heat release, sludge reflux supply is no more than the mechanical energy of 30%, simultaneously because the periphery of the reactor body of autothermal high-temperature micro-aerobic reactor 1 is provided with thermal insulation layer, make digestion temperature without the need to external heat source, maintain between 45 DEG C ~ 65 DEG C, at these elevated temperatures sterilizing is carried out to organic sludge, realize the rear sewage sludge harmlessness of digestion.If temperature of reactor rises to more than 65 DEG C, then strengthen aeration rate, close sludge reflux, heat radiation is increased, to realize cooling.
Because the sludge concentration dropped in reactor is high, viscosity is large, oxygen requirement is many, and the oxygen amount that mass transfer enters reactor is limited, is therefore not exclusively aerobic in autothermal high-temperature micro-aerobic reactor, namely by the acting in conjunction of aerobic bacteria, amphimicrobe, anerobe, volatile organic matter is degraded, be easy to produce voltaile fatty acid (VFA), and VFA under anaerobic, be easy to methane phase, therefore the high-temperature micro-aerobic digestive process of organic sludge is beneficial to the anaerobic digestion process of back segment organic sludge.
After high-temperature micro-aerobic digestion terminates, postdigestive mud enters pH value equalizing tank 3 from discharge port by pipeline, in pH value equalizing tank 3, drop into sodium hydroxide solution, the pH value of the material in pH value equalizing tank 3 is transferred between 6.8 ~ 7.2.Mud after pH value regulates stops 3h ~ 5h to discharge the dissolved oxygen in mud in pond.
3. the mesophilic anaerobic digestion of organic sludge.
Open sludge pump, 2. step discharges the mud through high-temperature micro-aerobic digestion of dissolved oxygen by being pumped in anaerobic fermentation reactor 2.Mud stops and completes anaerobic digestion process in 10 ~ 20 days in anaerobic fermentation reactor 2, and without the need to external heat source, anaeration in normal temperature temperature is 33 DEG C ~ 35 DEG C, and discharge mud is directly agricultural after mechanical dehydration.
If the mud temperature flowed out after the digestion of autothermal high-temperature micro-aerobic is too high, more than 60 DEG C, stop heat radiation in several hours by pH value equalizing tank 3 for postdigestive for high-temperature micro-aerobic mud more.If anaerobic pond temperature does not reach mesophilic range, the mud temperature that autothermal high-temperature micro-aerobic can be digested improves as far as possible, by reducing aeration rate, strengthening sludge reflux to mechanical heat, make high-temperature micro-aerobic digest temperature and reach 50 DEG C ~ 60 DEG C, ensure the middle temperature of anaerobic pond.
Slaking apparatus of the present invention belongs to two-stage series connection reactor, autothermal high-temperature micro-aerobic reactor is uniformly mixed by sludge reflux, mixing is without dead angle, reach sludge suspension effect, promote microbial biochemical reaction, microorganism autoxidation is reacted completely, in autothermal high-temperature micro-aerobic reactor, discharge enough heats through micro-aerobic sigestion, guarantee the middle temperature state of mud in the condition of high temperature of micro-aerobic reactor and anaerobic fermentation reactor.
During actual motion, adopt semi continuous charging marker method.In the present embodiment, the autothermal high-temperature micro-aerobic digested sludge residence time is 2 days, and anaerobically digested sludge stops 12 days.
If autothermal high-temperature micro-aerobic digestion reactor effective volume is V, it is V/2 that first day enters mud amount, stops two days, within the 3rd day, enters mud V/2, spoil disposal V/2.Namely mud and spoil disposal is entered every other day.From autothermal high-temperature micro-aerobic digestion reactor, discharge mud V every day, enter anaerobic digester, anaerobic digester volume is 12V, so sludge retention time is 12 days.Anaerobic digester sludge volume every day V.Enter mud like this and spoil disposal is equal.
For the digestion of autothermal high-temperature micro-aerobic, owing to being autothermal, temperature rises and is not easy, so the reactor volume in the present embodiment is 10m
3.The autothermal high-temperature micro-aerobic digestion phase temperature of the present embodiment can reach between 45 DEG C ~ 65 DEG C, though winter can be on the low side, because the large most low energy of reactor volume maintains 50 DEG C.
The advantage that make use of the heat production of autothermal high-temperature micro-aerobic digestible energy oneself of organic sludge high-temperature micro-aerobic-anaerobic digestion process of the present invention, does not need external heat source, saves cost.
The anaerobically fermenting of slaking apparatus of the present invention is mesophilic digestion, make use of the heat that in autothermal high-temperature micro-aerobic, mud carries, does not need external heat source, saves cost.Anaerobic fermentation reactor can produce the methane gas with energy substance, has carried out recycling; And mud remains nitrogen and phosphorus composition after digestion, can be agricultural after dehydration, solve the final outlet of mud.
(embodiment 2)
All the other are identical with embodiment 1 for the organic sludge high-temperature micro-aerobic-anaerobic digestion process of the present embodiment, and difference is:
Step 3. organic sludge carries out thermophilic digestion.
Open the valve of connecting tube, 2. step discharges the mud through high-temperature micro-aerobic digestion of dissolved oxygen by being pumped in anaerobic fermentation reactor 2.Mud stops and completes anaerobic digestion process in 6 ~ 10 days in anaerobic fermentation reactor 2, and the temperature of thermophilic digestion is 50 DEG C ~ 55 DEG C, and discharge mud is directly agricultural after mechanical dehydration.
Thermophilic digestion can make speed of response accelerate.The heat that the thermal source part of thermophilic digestion carries from the mud that the autothermal high-temperature micro-aerobic of leading portion flows out, the source of another part thermal source the methane collection after-burning of thermophilic digestion generation is heated up water the steam or hot water that obtain by the mud heat supply in the 26 pairs of retort 21 of the circulating water line in anaerobic fermentation reactor 2 with the high temperature maintaining 50 DEG C ~ 55 DEG C.
When the temperature of anaerobic fermentation reactor 2 declines, in circulating water line 26, delivering vapor or hot water are with to the mud heat supply in retort 21, and open agitator 22 while circulating water line 26 heat supply and make spread heat even, heat supply terminates to stop stirring.
(embodiment 3)
All the other are identical with embodiment 1 for the organic sludge high-temperature micro-aerobic-anaerobic digestion process of the present embodiment, and difference is:
Autothermal high-temperature micro-aerobic reactor 1 also comprises defoaming system, and described defoaming system comprises air froth breaking pipe, jet orifice; Described air froth breaking pipe is arranged in the top of retort 11, and tube wall evenly has aperture; Described jet orifice is arranged on the top of reactor body.During the work of this defoaming system, by the gas of the aperture blowout on air froth breaking tube wall, foam is smashed; Jet orifice can spray defoamer, and defoamer is ejected in reactor, is distributed on whole liquid level, plays froth breaking effect by stirring of agitator.
In the high-temperature micro-aerobic digestive process of the step of digestion method 2. organic sludge, defoaming system is sent into air and is broken by the bubble produced in retort in retort, and digestive process is carried out smoothly.
Claims (9)
1. organic sludge high-temperature micro-aerobic-anaerobic digestion device, comprises high-temperature aerobic reactor and anaerobic fermentation reactor (2), it is characterized in that: also comprise pH value equalizing tank (3); Described high-temperature aerobic reactor is autothermal high-temperature micro-aerobic reactor (1); PH value equalizing tank (3) is arranged between high-temperature micro-aerobic reactor (1) and anaerobic fermentation reactor (2), the discharge port of autothermal high-temperature micro-aerobic reactor (1) is communicated with pH value equalizing tank (3) by pipeline, and pH value equalizing tank (3) is connected with the opening for feed of pump with anaerobic fermentation reactor (2) by pipeline;
Autothermal high-temperature micro-aerobic reactor (1) comprises retort (11), sludge recirculation system (12), aerating system (13), temperature sensor (14) and gas absorption treating device (15); It is outside that described sludge recirculation system (12) is arranged on retort (11), comprises hypomere pipeline, sludge reflux pump and epimere pipeline; Hypomere pipeline, sludge reflux pump, epimere pipeline and retort form a loop communicated; Aerating system (13) includes aeration tube, aeration head, tensimeter, and aeration tube is arranged in the bottom of retort (11); Temperature sensor (14) on the top of retort (11), middle part, bottom respectively arrange one; Gas absorption treatment unit (15) is arranged on the top of retort (11), is communicated by the inside of pipeline with retort (11).
2. organic sludge high-temperature micro-aerobic-anaerobic digestion device according to claim 1, is characterized in that: anaerobic fermentation reactor (2) comprises anaerobically fermenting retort (21), agitator (22), collection and confinement of gases strainer (23), temperature sensor (24), gas sampling tube (25) and circulating water line (26);
Agitator (22) comprises motor, bar axle and agitating vane, motor is fixedly installed on the top of anaerobically fermenting retort (21), it is inner that bar axle penetrates anaerobically fermenting retort (21) from the top down, agitating vane arranges two-layer on bar axle, wherein the agitating vane of lower floor is arranged on the bottom of anaerobically fermenting retort (21), and the agitating vane on upper strata is arranged on the middle part of anaerobically fermenting retort (21) interior available depth;
Circulating water line (26) is arranged on anaerobically fermenting retort (21) bottom, and be connected with boiler by pipeline, the gas-cooker of boiler is connected by the air outlet of pipeline with collection and confinement of gases strainer (23).
3. a digestion method for organic sludge high-temperature micro-aerobic-anaerobic digestion device as claimed in claim 1, is characterized in that comprising the following steps:
1. tamed strain, tamed strain carries out in the retort (11) of autothermal high-temperature micro-aerobic reactor (1), and the kind mud containing bacterial classification that domestication obtains stays 1/4 ~ 1/2 in retort (11) inside;
2. the high-temperature micro-aerobic digestive process of organic sludge; Open sludge delivery pump, in the retort (11) of autothermal high-temperature micro-aerobic reactor (1), send into organic sludge, the operational throughput of organic sludge is the residue effective volume of retort (11); Open sludge recirculation system (12) and aerating system (13), organic sludge starts high-temperature micro-aerobic digestive process, and mud stops and completes high-temperature micro-aerobic digestive process in 2 ~ 3 days in autothermal high-temperature micro-aerobic reactor; Digestion temperature maintains between 45 DEG C ~ 65 DEG C;
After high-temperature micro-aerobic digestion terminates, postdigestive mud enters pH value equalizing tank (3) from discharge port by pipeline, alkali lye is dropped in pH value equalizing tank (3), be transferred between 6.8 ~ 7.2 by the pH value of the material in pH value equalizing tank (3), the mud after pH value regulates stops 3 ~ 5h to discharge the dissolved oxygen in mud in pond;
3. the anaerobic digestion process of organic sludge; The mud through high-temperature micro-aerobic digestion that 2. step discharges dissolved oxygen completes anaerobic digestion process in 6 ~ 20 days by being pumped into anaerobic fermentation reactor (2) stop, and discharge mud is directly agricultural after mechanical dehydration.
4. method according to claim 3, is characterized in that: in the high-temperature micro-aerobic digestive process of step 2. organic sludge, the redox potential ORP in the retort (11) of autothermal high-temperature micro-aerobic reactor (1) is 0 ~-100mv.
5. method according to claim 3, is characterized in that: the anaerobic digestion process of step 3. organic sludge is mesophilic anaerobic digestion process; Anaeration in normal temperature temperature is 33 DEG C ~ 35 DEG C, and mud stops and completes anaerobic digestion process in 10 ~ 20 days in anaerobic fermentation reactor (2).
6. method according to claim 5, it is characterized in that: if the mud temperature flowed out after the digestion of autothermal high-temperature micro-aerobic is more than 60 DEG C, postdigestive for high-temperature micro-aerobic mud extended residence time 0 ~ 40min in pH value equalizing tank (3) is dispelled the heat 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, strengthen sludge reflux to mechanical heat, make high-temperature micro-aerobic digest temperature and reach 50 DEG C ~ 60 DEG C, ensure the middle temperature of anaerobic pond.
7. method according to claim 3, is characterized in that: the anaerobic digestion process of step 3. organic sludge is thermophilic digestion process; The temperature of thermophilic digestion is 50 DEG C ~ 55 DEG C, and mud stops and completes anaerobic digestion process in 6 ~ 10 days in anaerobic fermentation reactor (2).
8. method according to claim 7, it is characterized in that: the methane gas that thermophilic digestion process produces is collected and afterfire produces steam or hot water to anaerobic fermentation reactor (2) heat supply with the high temperature maintaining 50 DEG C ~ 55 DEG C, the steam produce methyl hydride combustion or hot water to anaerobically fermenting retort (21) heat supply, open the agitator of anaerobically fermenting retort (21) by the circulating water line (26) bottom anaerobic fermentation reactor (2) simultaneously.
9. method according to claim 3, is characterized in that: step 2. in organic sludge be solid content 4% ~ 7%, volatility organic solid concentration accounts for the liquid organic solid castoff of 60% ~ 90%.
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| 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 |
| CN114315073B (en) * | 2021-12-15 | 2023-05-16 | 福建龙净环保股份有限公司 | Starting method of anaerobic digestion reactor |
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