CN107265797A - A kind of residual active sludge depth decrement method - Google Patents
A kind of residual active sludge depth decrement method Download PDFInfo
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- CN107265797A CN107265797A CN201610208323.9A CN201610208323A CN107265797A CN 107265797 A CN107265797 A CN 107265797A CN 201610208323 A CN201610208323 A CN 201610208323A CN 107265797 A CN107265797 A CN 107265797A
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- active sludge
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/06—Sludge reduction, e.g. by lysis
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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
- 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
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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 present invention relates to field of solid waste treating technology, the method that the group technology of specially a kind of utilization sludge disintegration and sludge digestion realizes residual active sludge depth decrement.In order to overcome prior art residual active sludge to crack, efficiency is low, dosing is big and the low problem of reduction rate, and the invention provides the method that the group technology of a kind of utilization sludge disintegration and sludge digestion realizes residual active sludge depth decrement.Sludge disintegration technology carries out depth to sludge using thermokalite and Fenton group technologies and cracked, and be conducive to raising residual active sludge cracks rate, digestibility and overall reduction rate, while reducing soda acid consumption and processing cost.
Description
Technical field
The present invention relates to field of solid waste treating technology, specially one kind utilizes sludge disintegration
The method that residual active sludge depth decrement is realized with the group technology of sludge digestion.
Background technology
With the increase of wastewater treatment in China amount, residual active sludge amount has broken through 30,000,000 t/a
(moisture content 80%).At present, the residual active sludge processing method commonly used both at home and abroad mainly has
Land use, landfill, heat treatment, burning and recycling etc..Relative to flourishing state
For family, the residual active sludge disposition of China falls behind relatively, due to relevant criterion system
Processing that is still unsound, causing residual active sludge not standardized largely.Residual activity
Sludge contains the poisonous and harmful substances such as pathogen, heavy metal and persistent organism, without effective
Processing is discharged into environment, easily causes secondary pollution to underground water, soil etc., is directly threatened
Environmental security and public health.Therefore, how effectively to handle residual active sludge be China urgently
The problem of need to solving.
Sludge reduction is by using physics, chemistry and biochemical means so that whole sewage
The biosolids amount that processing system is outwards discharged reaches at least.Fundamentally reduce sludge quantity technology
More and more paid attention to, while the research of Sludge Reduction Technologies is also to realize sewage sludge harmlessness
With the necessary ways of recycling.Common sludge reduction technology mainly has acid-base method, chemical oxidation
Method, heat treating process, Ultrasonic treatment and digestion method etc., are advantageously implemented sludge disintegration, reduction
The content of organic matter and moisture percentage in sewage sludge in sludge after press filtration, thus realize sludge reduction with stably
Change.Anaerobic sludge digestion is will be biodegradable in sludge using amphimicrobe and anaerobic bacteria
Organic matter resolves into carbon dioxide, methane and water etc., the process for being stablized sludge, is dirty
One of conventional means of mud minimizing, stabilisation and recycling.The content of organic matter and life in sludge
The property changed is to influence the key factor of anaerobic digestion.China's sludge content of organic matter is relative to state's outgoing
Up to national universal relatively low, often occur that difficulty in starting, gas production be low and aerogenesis in anaerobic digestion process
Unstable the problems such as, sludge digestion technology is limited in China's large-scale application.Sludge disintegration skill
Art is conducive to the release dissolution of organic matter in microorganism collagen group, hence it is evident that improve anaerobic sludge digestion
Operating ettectiveness.
(the publication number of patent 1：CN 103011542) and (publication number of patent 2：CN
1021180576) give heating treatment process and carry out sludge disintegration processing；Patent 3 is (open
Number：CN 103172242) give heating and the progress sludge disintegration processing of alkaline cleaning technique；
(the publication number of patent 4：CN 102583917) and (publication number of patent 5：CN 102838262)
Give addition medicament and carry out sludge disintegration processing；(the publication number of patent 6：CN 102603141)、
(the publication number of patent 7：) and (publication number of patent 8 CN101565262：CN 102424507)
Give the techniques such as ultrasound, adding medicine and/or heating and carry out sludge disintegration processing.Above-mentioned patent
Provide sludge disintegration technique and exist and crack that efficiency is low, the big and overall reduction rate of dosing is low
Problem.
The content of the invention
The technical problem to be solved in the present invention：
In order to overcome prior art residual active sludge to crack, efficiency is low, dosing big and decrement
The low problem of rate, the invention provides a kind of utilization sludge disintegration and the group technology of sludge digestion
The method for realizing residual active sludge depth decrement.Sludge disintegration technology uses thermokalite and Fenton
Group technology carries out depth to sludge and cracked.Thermokalite work in sludge disintegration technique of the present invention
Residual active sludge is in alkalescence after skill processing, and residual active sludge after Fenton PROCESS FOR TREATMENTs
The characteristics of in acidity, at the residual active sludge after thermokalite PROCESS FOR TREATMENT and Fenton techniques
Residual active sludge after reason is neutralized, and reduces and residual activity dirt is neutralized after single PROCESS FOR TREATMENT
The soda acid consumption of mud.Therefore, the invention provides a kind of utilization sludge disintegration and sludge digestion
The method that group technology realizes residual active sludge depth decrement, is conducive to improving residual activity dirt
Mud cracks rate, digestibility and overall reduction rate, while reduce soda acid consumption and processing cost.
To achieve the above objectives, the present invention is adopted the technical scheme that：
A kind of residual active sludge depth decrement method, comprises the following steps：
Step one：1 point of residual active sludge is two strands, carry out respectively thermokalite PROCESS FOR TREATMENT and
Fenton PROCESS FOR TREATMENTs；
Step 2：After residual active sludge and Fenton PROCESS FOR TREATMENTs after thermokalite PROCESS FOR TREATMENT
Residual active sludge, in proportion mix carry out neutralisation treatment；
Step 3：Residual active sludge after neutralisation treatment disappears after heat exchange cooling into anaerobism
Change kettle 9；
Step 4：After residual active sludge is handled through anaerobic digestion kettle 9, sludge conditioning is added
Agent 11 is sufficiently stirred for, and then carries out dewater treatment.
On the basis of such scheme, using thermokalite technique and Fenton techniques point in step one
It is other that residual active sludge is carried out to crack processing.
On the basis of such scheme, at thermokalite technique described in step 2 and Fenton techniques
The ratio of reason residual active sludge is determined that proportion is 1 by technological parameter:0.3~2, preferably
Scope is 1:0.5~1.
On the basis of such scheme, the Fenton PROCESS FOR TREATMENTs：To residual active sludge 1
Acid 2, iron salt solutions 3 and oxidant 4 are separately added into, into oxidizing reactor 5.
On the basis of such scheme, pH value range is 3~5 after sour 2 regulation, preferably
Scope is 4~5.
On the basis of such scheme, the acid 2 of the regulation pH value can be H2SO4、HCl
Or HNO3In one or more.
On the basis of such scheme, the iron salt solutions 3 can be FeCl2、FeSO4、
Fe(NO3)2、FeCl3、Fe2(SO4)3With Fe (NO3)3One or more in solution, preferably
For FeSO4Solution.
On the basis of such scheme, the configuration concentration of iron salt solutions 3 is with Fe mass percentages
Content is calculated as 2%, molysite (using Fe content meters) in residual active sludge addition as
0.001~0.015kgFe/kgMLSS, preferred scope is 0.002~0.01kgFe/kgMLSS.
On the basis of such scheme, the oxidant 4 use concentration for 30% H2O2,
Its addition in residual active sludge is 0.2~1L/kgMLSS, and preferred scope is
0.3~0.5L/kgMLSS.
On the basis of such scheme, the Fenton PROCESS FOR TREATMENTs temperature range is
30~70 DEG C, preferred scope is 40~60 DEG C.
On the basis of such scheme, the Fenton process treatment times are 0.5~3h, excellent
It is 1~2h to select the time.
On the basis of such scheme, thermokalite PROCESS FOR TREATMENT：Alkali is added to residual active sludge 1
Liquid 6 adjusts pH value, rear feeding pyrolytic reaction kettle 7.
On the basis of such scheme, pH value range is 9~13 after the alkali lye 6 is adjusted, preferably
Scope is 10~12.
On the basis of such scheme, the alkali lye 6 of the regulation pH value can be NaOH, KOH
With Ca (OH)2One or more in solution, preferably NaOH solution.
On the basis of such scheme, the thermokalite PROCESS FOR TREATMENT temperature range is 60~200 DEG C,
Preferred scope is 70~170 DEG C.
On the basis of such scheme, the thermokalite process treatment time is 1~9h, preferably time
For 2~8h.
On the basis of such scheme, residual active sludge after neutralisation treatment described in step 2
PH value range is 7~8.
On the basis of such scheme, the time of residual active sludge neutralisation treatment described in step 2
For 0.3~1.5h, preferred scope is 0.5~1h.
On the basis of such scheme, anaerobic digestion kettle described in step 39 uses anaeration in normal temperature
Digestion, it is 35 ± 3 DEG C to control temperature range.
On the basis of such scheme, the volumetric loading of anaerobic digestion kettle described in step 39 is
2~4kg/m3·d；Preferred scope is 2.5~3.5kg/m3·d。
On the basis of such scheme, the digestion process time of anaerobic digestion kettle described in step 39
For 10~35d；15~30d of preferred scope.
On the basis of such scheme, in step 3, what residual active sludge digestion process was produced
Biogas 10 is utilized by the recovered overhead of anaerobic digestion kettle 9.
On the basis of such scheme, sludge conditioner 11 described in step 4 can be poly- third
One or more in acrylamide, Sodium Polyacrylate, polyvinyl pyridine salt and polyethyleneimine.
On the basis of such scheme, sludge conditioner 11 described in step 4 is in residual activity
Weight/mass percentage composition in sludge is 0.01%~0.2%, and preferred scope is 0.02%~0.1%.
On the basis of such scheme, in step 4, residual active sludge enters dewatering system
The 12 dehydration liquid 13 produced after dewater treatment, dewater treatment carry out sewage disposal, dehydration
Sludge 14 carries out desiccation or outward transport processing.
On the basis of such scheme, residual active sludge after neutralisation treatment is carried out in step 4
Moisture content and organic component in dewater treatment, effectively reduction residual active sludge, realize minimizing
Purpose.
The beneficial effects of the invention are as follows：
The invention provides a kind of residual active sludge depth decrement method, with reduced training
Good, the low advantage of processing cost, and with technology maturation is reliable and the flow advantage, energy such as simply
Moisture content and organic component in enough effectively reduction residual active sludges, are greatly lowered residual activity
Sludge quantity and processing cost, with preferable economy and application value.
Brief description of the drawings
The present invention has drawings described below：
Fig. 1 residual active sludge depth decrement process flow diagrams.
In figure：1 is residual active sludge；2 be acid；3 be iron salt solutions；4 be oxidant；
5 be oxidizing reactor；6 be alkali lye；7 be pyrolytic reaction kettle；8 be neutralization reaction kettle；9 are
Anaerobic digestion kettle；10 be biogas；11 be sludge conditioner；12 be dewatering system；13 be de-
Aqueous；14 be dewatered sludge.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing.
As shown in figure 1, a kind of implementation of residual active sludge depth decrement method of the present invention
Scheme is as follows：
Step one：1 point of residual active sludge is two strands, carry out respectively thermokalite PROCESS FOR TREATMENT and
Fenton PROCESS FOR TREATMENTs.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
With oxidant 4, into oxidizing reactor 5.PH value range after the regulation of acid 2 is 3~5, excellent
It is 4~5 to select scope；The acid 2 that regulation pH value is used can be H2SO4, HCl or HNO3
In one or more；Iron salt solutions 3 can be FeCl2、FeSO4、Fe(NO3)2、FeCl3、
Fe2(SO4)3With Fe (NO3)3One or more in solution, preferably FeSO4Solution.Iron
The configuration concentration of salting liquid 3 is calculated as molysite in 2%, residual active sludge with Fe weight/mass percentage compositions
The addition of (using Fe content meters) is 0.001~0.015kgFe/kgMLSS, and preferred scope is
0.002~0.01kgFe/kgMLSS；Oxidant 4 use concentration for 30% H2O2, it is surplus
Addition is 0.2~1L/kgMLSS in remaining activated sludge, and preferred scope is
0.3~0.5L/kgMLSS；Oxidizing reactor 5 is heated to temperature range for 30~70 DEG C, excellent
It is 40~60 DEG C to select scope；The reaction time of oxidizing reactor 5 is 0.5~3h, preferred reaction time
For 1~2h.
Thermokalite PROCESS FOR TREATMENT：It is pumped into alkali lye 6 to adjust pH value to residual active sludge 1, and
Pyrolytic reaction kettle 7 is sent into afterwards.PH value range is 9~13, preferred scope in pyrolytic reaction kettle 7
For 10~12, the alkali lye 6 of regulation pH value can be NaOH, KOH and Ca (OH)2Solution
One or more, preferably NaOH solution.Thermokalite Process temperature ranges are 60~200 DEG C,
Preferred scope is 70~170 DEG C；Thermokalite process treatment time is 1~9h, and the preferably time is 2~8h.
Step 2：Residual activity after above-mentioned oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled is dirty
Mud, is pumped into neutralization reaction kettle 8 respectively, according to residual active sludge through thermokalite technique and Fenton
PH value after PROCESS FOR TREATMENT, is mixed in proportion, and stirring carries out neutralisation treatment, ratio model
Enclose for 1:0.3~2, preferred scope is 1:0.5~1.Residual active sludge pH value after neutralisation treatment
Scope is 7~8.Residual active sludge processing time in neutralization reaction kettle 8 is 0.3~1.5h,
Preferred scope is 0.5~1h.
Step 3：Reached when neutralizing residual active sludge in reactor 8 in above-mentioned pH value range,
Again after heat exchange cooling, into anaerobic digestion kettle 9.Anaerobic digestion kettle 9 is disappeared using anaeration in normal temperature
Change, it is 35 ± 3 DEG C to control temperature range；The volumetric loading of anaerobic digestion kettle 9 is 2~4kg/m3·d；
Preferred scope is 2.5~3.5kg/m3·d；The digestion process time is 10~35d；Preferred scope
15~30d.The biogas 10 that sludge digestion process is produced is utilized by the recovered overhead of anaerobic digestion kettle 9；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 can be polyacrylamide, Sodium Polyacrylate, polyethylene pyrrole
One or more in pyridine salt and polyethyleneimine, sludge conditioner 11 is in residual active sludge
In weight/mass percentage composition be 0.01%~0.2%, preferred scope be 0.02%~0.1%.
Embodiment 1
Residual active sludge characteristic：Certain sewage treatment plant's biochemical processing process sludge concentration tank sludge
10t, its sludge index is：Mix suspending solid concentration (MLSS) is that 30.5g/L is (aqueous
Rate 96.95%), mixed liquor volatile suspended solid, MLVSS concentration (MLVSS) is 24.6g/L.
Above-mentioned residual active sludge processing implementation steps are as follows：
Step one：Residual active sludge 1 carries out thermokalite PROCESS FOR TREATMENT and Fenton techniques respectively
Processing.Thermokalite technique and the ratio of Fenton PROCESS FOR TREATMENT residual active sludges are by technological parameter
It is determined that, ratio is 1:0.3.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
After oxidant 4, oxidizing reactor 5 is sent into；PH value is adjusted to 4, adjusts the acid of pH value
Using H2SO4；Molysite is FeSO4And Fe2(SO4)3, molysite (with Fe content meters) is surplus
Addition is 0.002kgFe/kgMLSS in remaining activated sludge；Oxidant uses H2O2, concentration
For 30% H2O2Addition is 0.5L/kgMLSS in residual active sludge；Oxidation reaction
Kettle 5 is heated to temperature for 60 DEG C；The processing time of oxidizing reactor 5 is 2h.
Thermokalite PROCESS FOR TREATMENT：Alkali lye 6 is first pumped into residual active sludge 1, then feeding pyrolysis
Reactor 7.PH value is 12 in pyrolytic reaction kettle 7, and the alkali lye of regulation pH value is NaOH
Solution.Thermokalite technological temperature is 150 DEG C；Thermokalite process treatment time is 2h.
Step 2：Residual active sludge after oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled divides
It is not pumped into neutralization reaction kettle 8, according to residual active sludge through thermokalite technique and Fenton works
PH value after skill processing, is mixed in proportion, and stirring carries out neutralisation treatment.Residual activity
Sludge processing time in neutralization reaction kettle 8 is 1h.Residual active sludge pH after neutralisation treatment
It is worth for 7.
Step 3：After residual active sludge is cooled down through heat exchange again in step 2, into anaerobic digestion
Kettle 9.The volumetric loading of anaerobic digestion kettle 9 is 2kg/m3D, the digestion process time is 15d, temperature
It is 35 ± 3 DEG C to spend scope, and the biogas 10 that sludge digestion process is produced is by the top of anaerobic digestion kettle 9
Recycle；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 is polyacrylamide, the quality of the addition of sludge conditioner 11
Percentage composition is 0.01%.
The characteristic of dewatered sludge 14：Moisture content 59.54%, gross mass is 322kg, sludge quality
Overall reduction rate is 96.7%.
Embodiment 2
Residual active sludge characteristic：Certain sewage treatment plant's biochemical processing process sludge concentration tank sludge
10t, its sludge index is：Mix suspending solid concentration (MLSS) is that 30.5g/L is (aqueous
Rate 96.95%), mixed liquor volatile suspended solid, MLVSS concentration (MLVSS) is 24.6g/L.
Above-mentioned residual active sludge processing implementation steps are as follows：
Step one：Residual active sludge 1 carries out thermokalite PROCESS FOR TREATMENT and Fenton techniques respectively
Processing.Thermokalite technique and the ratio of Fenton PROCESS FOR TREATMENT residual active sludges are by technological parameter
It is determined that, ratio is 1:0.5.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
After oxidant 4, oxidizing reactor 5 is sent into；PH value is adjusted to 5, adjusts the acid of pH value
Using H2SO4And HNO3；Molysite is FeCl2And FeCl3, molysite (with Fe content meters)
Addition is 0.004kgFe/kgMLSS in residual active sludge；Oxidant uses H2O2；
Concentration is 30% H2O2Addition is 0.2L/kgMLSS in residual active sludge；Oxidation
Reactor 5 is heated to temperature for 30 DEG C；The processing time of oxidizing reactor 5 is 2.5h.
Thermokalite PROCESS FOR TREATMENT：Alkali lye 6 is first pumped into residual active sludge 1, then feeding pyrolysis
Reactor 7.PH value is 10 in pyrolytic reaction kettle 7, and the alkali lye of regulation pH value is NaOH
And KOH solution.Thermokalite technological temperature is 200 DEG C；Thermokalite process treatment time is 1h.
Step 2：Residual active sludge after oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled divides
It is not pumped into neutralization reaction kettle 8, according to residual active sludge through thermokalite technique and Fenton works
PH value after skill processing, is mixed in proportion, and stirring carries out neutralisation treatment.Residual activity
Sludge processing time in neutralization reaction kettle 8 is 0.5h.Residual active sludge after neutralisation treatment
PH value is 8.
Step 3：After residual active sludge is cooled down through heat exchange again in step 2, into anaerobic digestion
Kettle 9.The volumetric loading of anaerobic digestion kettle 9 is 3kg/m3D, the digestion process time is 20d, temperature
It is 35 ± 3 DEG C to spend scope.The biogas 10 that sludge digestion process is produced is by the top of anaerobic digestion kettle 9
Recycle；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 is polyacrylamide and Sodium Polyacrylate, sludge conditioner 11
The weight/mass percentage composition of addition is 0.2%.
The characteristic of dewatered sludge 14：Moisture content 63.30%, gross mass is 374kg, sludge quality
Overall reduction rate is 96.3%.
Embodiment 3
Residual active sludge characteristic：Certain sewage treatment plant's biochemical processing process sludge concentration tank is remaining
Activated sludge 10t, its sludge index is that MLSS is 30.5g/L (moisture content 96.95%),
MLVSS is 24.6g/L.
Above-mentioned Treatment of Sludge implementation steps are as follows：
Step one：Residual active sludge 1 carries out thermokalite PROCESS FOR TREATMENT and Fenton techniques respectively
Processing.Thermokalite technique and the ratio of Fenton PROCESS FOR TREATMENT residual active sludges are by technological parameter
It is determined that, ratio is 1:2.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
With oxidant 4.PH value is adjusted to 5, and the acid of regulation pH value is adopted as HCl；Molysite is
Fe(NO3)3And FeSO4, molysite (with Fe content meters) addition in residual active sludge
For 0.01kgFe/kgMLSS；Oxidizing reactor 5 is heated to temperature for 70 DEG C；Oxidant is adopted
With for H2O2, concentration is 30% H2O2Addition is in residual active sludge
1L/kgMLSS；Fenton process treatment times are 0.5h.
Thermokalite PROCESS FOR TREATMENT：Alkali lye 6 is first pumped into residual active sludge 1, then feeding pyrolysis
Reactor 7.PH value is 9 in pyrolytic reaction kettle 7, the alkali lye of regulation pH value for NaOH and
Ca(OH)2Solution.Thermokalite technological temperature is 100 DEG C；Thermokalite process treatment time is 8h.
Step 2：Residual active sludge after oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled divides
It is not pumped into neutralization reaction kettle 8, according to residual active sludge through thermokalite technique and Fenton works
PH value after skill processing, is mixed in proportion, and stirring carries out neutralisation treatment.Residual activity
Sludge processing time in neutralization reaction kettle 8 is 1.5h.Residual active sludge after neutralisation treatment
PH value is 7.
Step 3：After residual active sludge is cooled down through heat exchange again in step 2, into anaerobic digestion
Kettle 9.The volumetric loading of anaerobic digestion kettle 9 is 2.5kg/m3D, the digestion process time is 25d,
Temperature range is 35 ± 3 DEG C, and the biogas 10 that sludge digestion process is produced is pushed up by anaerobic digestion kettle 9
Portion is recycled；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 is Sodium Polyacrylate and polyvinyl pyridine salt, sludge conditioner
The weight/mass percentage composition of 11 additions is 0.1%.
The characteristic of dewatered sludge 14：Moisture content 57.60%, gross mass is 328kg, sludge quality
Overall reduction rate is 96.7%.
Embodiment 4
Residual active sludge characteristic：Certain sewage treatment plant's biochemical processing process sludge concentration tank sludge
10t, its sludge index is that MLSS is 30.5g/L (moisture content 96.95%), and MLVSS is
24.6g/L。
Above-mentioned residual active sludge processing implementation steps are as follows：
Step one：Residual active sludge 1 carries out thermokalite PROCESS FOR TREATMENT and Fenton techniques respectively
Processing.Thermokalite technique and the ratio of Fenton PROCESS FOR TREATMENT residual active sludges are by technological parameter
It is determined that, ratio is 1:1.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
After oxidant 4, oxidizing reactor 5 is sent into；PH value is adjusted to 3, adjusts the acid of pH value
For HNO3；Molysite is Fe2(SO4)3And FeCl3, molysite (with Fe content meters) is remaining living
Property sludge in addition be 0.015kgFe/kgMLSS；Oxidant uses H2O2；Concentration is 30%
H2O2Addition is 0.8L/kgMLSS in residual active sludge；Oxidizing reactor 5 is passed through
Temperature is heated to for 40 DEG C；The processing time of oxidizing reactor 5 is 1h.
Thermokalite PROCESS FOR TREATMENT：Alkali lye 6 is first pumped into residual active sludge 1, then feeding pyrolysis
Reactor 7.PH value is 11 in pyrolytic reaction kettle 7, and the alkali lye of regulation pH value is NaOH
And KOH solution.Thermokalite technological temperature is 60 DEG C；Thermokalite process treatment time is 4h.
Step 2：Residual active sludge after oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled divides
It is not pumped into neutralization reaction kettle 8, according to residual active sludge through thermokalite technique and Fenton works
PH value after skill processing, is mixed in proportion, and stirring carries out neutralisation treatment.Residual activity
Sludge processing time in neutralization reaction kettle 8 is 1.5h.Residual active sludge after neutralisation treatment
PH value is 8.
Step 3：After residual active sludge is cooled down through heat exchange again in step 2, into anaerobic digestion
Kettle 9.The volumetric loading of anaerobic digestion kettle 9 is 4kg/m3D, the digestion process time is 30d, temperature
It is 35 ± 3 DEG C to spend scope, and the biogas 10 that sludge digestion process is produced is by the top of anaerobic digestion kettle 9
Recycle；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 is Sodium Polyacrylate, the quality of the addition of sludge conditioner 11
Percentage composition is 0.02%.
The characteristic of dewatered sludge 14：Moisture content 60.13%, gross mass is 331kg, sludge quality
Overall reduction rate is 96.7%.
Embodiment 5
Residual active sludge characteristic：Certain sewage treatment plant's biochemical processing process sludge concentration tank sludge
10t, its sludge index is that MLSS is 30.5g/L (moisture content 96.95%), and MLVSS is
24.6g/L。
Above-mentioned residual active sludge processing implementation steps are as follows：
Step one：Residual active sludge 1 carries out thermokalite PROCESS FOR TREATMENT and Fenton techniques respectively
Processing.Thermokalite technique and the ratio of Fenton PROCESS FOR TREATMENT residual active sludges are by technological parameter
It is determined that, ratio is 1:1.5.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
After oxidant 4, oxidizing reactor 5 is sent into；PH value is adjusted to 5, and regulation pH value is used
HNO3And H2SO4；Molysite is Fe (NO3)3And FeCl3, molysite (with Fe content meters) exists
Addition is 0.001kgFe/kgMLSS in residual active sludge；Oxidant uses H2O2；It is dense
Spend the H for 30%2O2Addition is 0.6L/kgMLSS in residual active sludge；Oxidation is anti-
Kettle 5 is answered to be heated to temperature for 50 DEG C；The processing time of oxidizing reactor 5 is 3h.
Thermokalite PROCESS FOR TREATMENT：Alkali lye 6 is first pumped into residual active sludge 1, then feeding pyrolysis
Reactor 7.PH value is 13 in pyrolytic reaction kettle 7, and regulation pH value alkali lye is KOH solution.
Thermokalite technological temperature is 170 DEG C；Thermokalite process treatment time is 6h.
Step 2：Residual active sludge after oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled divides
It is not pumped into neutralization reaction kettle 8, according to residual active sludge through thermokalite technique and Fenton works
PH value after skill processing, is mixed in proportion, and stirring carries out neutralisation treatment.Residual activity
Sludge processing time in neutralization reaction kettle 8 is 1h.Residual active sludge pH after neutralisation treatment
It is worth for 7.
Step 3：After residual active sludge is cooled down through heat exchange again in step 2, into anaerobic digestion
Kettle 9.The volumetric loading of anaerobic digestion kettle 9 is 3.5kg/m3D, the digestion process time is 35d,
Temperature range is 35 ± 3 DEG C, and the biogas 10 that sludge digestion process is produced is pushed up by anaerobic digestion kettle 9
Portion is recycled；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 is polyethyleneimine and polyacrylamide, sludge conditioner 11
The weight/mass percentage composition of addition is 0.05%.
The characteristic of dewatered sludge 14：Moisture content 62.11%, gross mass is 369kg, sludge quality
Overall reduction rate is 96.3%.
Embodiment 6
Residual active sludge characteristic：Certain sewage treatment plant's biochemical processing process sludge concentration tank sludge
10t, its sludge index is that MLSS is 30.5g/L (moisture content 96.95%), and MLVSS is
24.6g/L。
Above-mentioned residual active sludge processing implementation steps are as follows：
Step one：Residual active sludge 1 carries out thermokalite PROCESS FOR TREATMENT and Fenton techniques respectively
Processing.Thermokalite technique and the ratio of Fenton PROCESS FOR TREATMENT residual active sludges are by technological parameter
It is determined that, ratio is 1:0.5.
Fenton PROCESS FOR TREATMENTs：Acid 2, iron salt solutions 3 are pumped into respectively to residual active sludge 1
After oxidant 4, oxidizing reactor 5 is sent into；PH value is adjusted to 3, and regulation pH value is used
HCl and H2SO4；Molysite is Fe (NO3)2And FeSO4, molysite (with Fe content meters) exists
Addition is 0.005kgFe/kgMLSS in residual active sludge；Oxidant uses H2O2；It is dense
Spend the H for 30%2O2Addition is 0.3L/kgMLSS in residual active sludge；Oxidation is anti-
Kettle 5 is answered to be heated to temperature for 70 DEG C；The processing time of oxidizing reactor 5 is 2h.
Thermokalite PROCESS FOR TREATMENT：Alkali lye 6 is first pumped into residual active sludge 1, then feeding pyrolysis
Reactor 7.PH value is 9 in pyrolytic reaction kettle 7, and regulation pH value alkali lye is NaOH solution.
Thermokalite technological temperature is 70 DEG C；Thermokalite process treatment time is 9h.
Step 2：Residual active sludge after oxidizing reactor 5 and pyrolytic reaction kettle 7 are handled divides
It is not pumped into neutralization reaction kettle 8, according to residual active sludge through thermokalite technique and Fenton works
PH value after skill processing, is mixed in proportion, and stirring carries out neutralisation treatment.Residual activity
Sludge processing time in neutralization reaction kettle 8 is 0.3h.Residual active sludge after neutralisation treatment
PH value is 8.
Step 3：After residual active sludge is cooled down through heat exchange again in step 2, into anaerobic digestion
Kettle 9.The volumetric loading of anaerobic digestion kettle 9 is 3kg/m3D, the digestion process time is 10d, temperature
It is 35 ± 3 DEG C to spend scope, and the biogas 10 that sludge digestion process is produced is by the top of anaerobic digestion kettle 9
Recycle；
Step 4：After sludge is handled through anaerobic digestion kettle 9, add sludge conditioner 11 and enter
Row is sufficiently stirred for, and then residual active sludge enters the progress dewater treatment of dewatering system 12；It is de-
The dehydration liquid 13 produced after water process carries out sewage disposal, and dewatered sludge 14 carries out desiccation or outer
Fortune processing.Sludge conditioner 11 is polyethyleneimine and polyacrylamide, sludge conditioner 11
The weight/mass percentage composition of addition is 0.15%.
The characteristic of dewatered sludge 14：Moisture content 66.10%, gross mass is 379kg, sludge quality
Overall reduction rate is 96.2%.
Comparative example 1
Using residual active sludge in the same manner as in Example 1, and with step in embodiment 1
Identical condition in thermokalite technique and step 3 in one, it is (after processing remaining only with thermokalite technique
Activated sludge pH value is adjusted to 7) handle residual active sludge with anaerobic digestion process.
Residual active sludge adds sludge conditioner 11 after processing, and sludge conditioner 11 is polyacrylamide
Amine, it is 0.01% to add weight/mass percentage composition.Moisture content is 73.1%, gross mass after dehydration
For 1007kg, sludge quality totality reduction rate is 89.9%.
Comparative example 2
Using residual active sludge in the same manner as in Example 2, and with step in embodiment 2
Identical process conditions in Fenton techniques and step 3 in one, only with Fenton techniques (place
Residual active sludge pH value is adjusted to 8) enter residual active sludge with sludge digestion technique after reason
Row processing.Residual active sludge after processing adds sludge conditioner 11, sludge conditioner 11
For polyacrylamide and Sodium Polyacrylate, it is 0.2% to add weight/mass percentage composition.Remained after processing
Remaining activated sludge moisture content after dehydration is 76.9%, and gross mass is 1257kg, and sludge quality is total
Body reduction rate is 87.4%.
The content not being described in detail in this specification belongs to known in professional and technical personnel in the field
Prior art.
Claims (25)
1. a kind of residual active sludge depth decrement method, it is characterised in that including following step
Suddenly：
Step one：Residual active sludge (1) is divided into two strands, and thermokalite PROCESS FOR TREATMENT is carried out respectively
With Fenton PROCESS FOR TREATMENTs；
Step 2：After residual active sludge and Fenton PROCESS FOR TREATMENTs after thermokalite PROCESS FOR TREATMENT
Residual active sludge, in proportion mix carry out neutralisation treatment；
Step 3：Residual active sludge after neutralisation treatment disappears after heat exchange cooling into anaerobism
Change kettle (9)；
Step 4：After residual active sludge is handled through anaerobic digestion kettle (9), sludge is added
Conditioner (11) is sufficiently stirred for, and then carries out dewater treatment.
2. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：The scope of ratio described in step 2 is 1:0.3~2.
3. residual active sludge depth decrement method as claimed in claim 2, its feature exists
In：The scope of the ratio is 1:0.5~1.
4. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：Fenton PROCESS FOR TREATMENTs：Sour (2), molysite are separately added into residual active sludge (1)
Solution (3) and oxidant (4).
5. residual active sludge depth decrement method as claimed in claim 4, its feature exists
In：PH value range is 3~5 after sour (2) regulation.
6. residual active sludge depth decrement method as claimed in claim 4, its feature exists
In：The acid (2) for adjusting pH value is H2SO4, HCl or HNO3In one or more.
7. residual active sludge depth decrement method as claimed in claim 4, its feature exists
In：Iron salt solutions (3) are FeCl2、FeSO4、Fe(NO3)2、FeCl3、Fe2(SO4)3With
Fe(NO3)3One or more in solution.
8. residual active sludge depth decrement method as claimed in claim 4, its feature exists
In：The configuration concentration of iron salt solutions (3) is calculated as 2% with Fe weight/mass percentage compositions.
9. residual active sludge depth decrement method as claimed in claim 4, its feature exists
In：With Fe content meters, the addition of molysite is in residual active sludge
0.001~0.015kgFe/kgMLSS.
10. residual active sludge depth decrement method as claimed in claim 4, its feature exists
In：Oxidant (4) use concentration for 30% H2O2, it is added in residual active sludge
Measure as 0.2~1L/kgMLSS.
11. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：Fenton PROCESS FOR TREATMENTs temperature range is 30~70 DEG C.
12. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：Fenton process treatment times are 0.5~3h.
13. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：Thermokalite PROCESS FOR TREATMENT：Add alkali lye (6) to adjust pH to residual active sludge (1)
Value, pH value range is 9~13 after regulation.
14. residual active sludge depth decrement method as claimed in claim 13, its feature
It is：The alkali lye (6) for adjusting pH value is NaOH, KOH and Ca (OH)2In solution
It is one or more of.
15. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step one, thermokalite PROCESS FOR TREATMENT temperature range is 60~200 DEG C.
16. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step one, thermokalite process treatment time is 1~9h.
17. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 2, residual active sludge pH value range is 7~8 after neutralisation treatment.
18. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 2, the residual active sludge neutralisation treatment time is 0.3~1.5h.
19. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 3, anaerobic digestion kettle (9) uses mesophilic anaerobic digestion, controls temperature range
For 35 ± 3 DEG C.
20. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 3, anaerobic digestion kettle (9) volumetric loading is 2~4kg/m3·d。
21. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 3, anaerobic digestion kettle (9) the digestion process time is 10~35d.
22. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 3, the biogas (10) that residual active sludge digestion process is produced is by anaerobic digestion
Kettle (9) recovered overhead is utilized.
23. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 4, sludge conditioner (11) is polyacrylamide, Sodium Polyacrylate, poly- second
One or more in annulated pyridine salt and polyethyleneimine.
24. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 4, weight/mass percentage composition of the sludge conditioner (11) in residual active sludge
For 0.01%~0.2%.
25. residual active sludge depth decrement method as claimed in claim 1, its feature exists
In：In step 4, residual active sludge enters dewatering system (12) and carries out dewater treatment, takes off
The dehydration liquid (13) produced after water process carries out sewage disposal, and dewatered sludge (14) is done
Change or outward transport processing.
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| JP2009148749A (en) * | 2007-11-30 | 2009-07-09 | Mitsubishi Materials Corp | Heavy metal-containing water treating method |
| CN104829021A (en) * | 2015-04-29 | 2015-08-12 | 四川和鼎环保工程有限责任公司 | Treating method for organic waste water |
| CN106554140A (en) * | 2015-09-29 | 2017-04-05 | 中国石油化工股份有限公司 | A kind of residual active sludge cracks decrement method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009148749A (en) * | 2007-11-30 | 2009-07-09 | Mitsubishi Materials Corp | Heavy metal-containing water treating method |
| CN104829021A (en) * | 2015-04-29 | 2015-08-12 | 四川和鼎环保工程有限责任公司 | Treating method for organic waste water |
| CN106554140A (en) * | 2015-09-29 | 2017-04-05 | 中国石油化工股份有限公司 | A kind of residual active sludge cracks decrement method |
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