CN112028320B - System for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation and treatment method of sludge anaerobic digestion solution - Google Patents
System for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation and treatment method of sludge anaerobic digestion solution Download PDFInfo
- Publication number
- CN112028320B CN112028320B CN202010911932.7A CN202010911932A CN112028320B CN 112028320 B CN112028320 B CN 112028320B CN 202010911932 A CN202010911932 A CN 202010911932A CN 112028320 B CN112028320 B CN 112028320B
- Authority
- CN
- China
- Prior art keywords
- dosing
- tank
- sedimentation
- zone
- catalytic oxidation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 119
- 230000003647 oxidation Effects 0.000 title claims abstract description 118
- 239000010802 sludge Substances 0.000 title claims abstract description 96
- 230000029087 digestion Effects 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000020477 pH reduction Effects 0.000 title claims abstract description 19
- 238000004062 sedimentation Methods 0.000 claims abstract description 177
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 117
- 230000003197 catalytic effect Effects 0.000 claims abstract description 97
- 230000001112 coagulating effect Effects 0.000 claims abstract description 90
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 61
- 238000006243 chemical reaction Methods 0.000 claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 230000001105 regulatory effect Effects 0.000 claims abstract description 36
- 238000001556 precipitation Methods 0.000 claims abstract description 31
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 13
- 239000011790 ferrous sulphate Substances 0.000 claims description 97
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 97
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 93
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 93
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 91
- 238000002156 mixing Methods 0.000 claims description 89
- 239000003814 drug Substances 0.000 claims description 84
- 239000000701 coagulant Substances 0.000 claims description 46
- 239000007864 aqueous solution Substances 0.000 claims description 42
- 238000005192 partition Methods 0.000 claims description 32
- 239000003054 catalyst Substances 0.000 claims description 29
- 239000000243 solution Substances 0.000 claims description 28
- 230000015271 coagulation Effects 0.000 claims description 21
- 238000005345 coagulation Methods 0.000 claims description 21
- 239000003513 alkali Substances 0.000 claims description 14
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 11
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 11
- 125000000129 anionic group Chemical group 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 229920002401 polyacrylamide Polymers 0.000 claims description 9
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical group [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 8
- -1 polypropylene Polymers 0.000 claims description 6
- 238000010979 pH adjustment Methods 0.000 claims description 5
- 239000004743 Polypropylene Substances 0.000 claims description 4
- 229920001155 polypropylene Polymers 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 125000002887 hydroxy group Chemical group [H]O* 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 6
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000004891 communication Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000009283 thermal hydrolysis Methods 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229920000620 organic polymer Polymers 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- PUKLDDOGISCFCP-JSQCKWNTSA-N 21-Deoxycortisone Chemical compound C1CC2=CC(=O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@@](C(=O)C)(O)[C@@]1(C)CC2=O PUKLDDOGISCFCP-JSQCKWNTSA-N 0.000 description 1
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- FCYKAQOGGFGCMD-UHFFFAOYSA-N Fulvic acid Natural products O1C2=CC(O)=C(O)C(C(O)=O)=C2C(=O)C2=C1CC(C)(O)OC2 FCYKAQOGGFGCMD-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 210000002421 cell wall Anatomy 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000003631 expected effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000002509 fulvic acid Substances 0.000 description 1
- 229940095100 fulvic acid Drugs 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 239000004021 humic acid Substances 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 230000003834 intracellular effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 230000000696 methanogenic effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000002085 persistent effect Effects 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a system for treating sludge anaerobic digestion liquid by non-acidification Fenton oxidation and a treatment method of the sludge anaerobic digestion liquid. The system comprises: the device comprises a regulating tank, a coagulating sedimentation device, a Fenton catalytic oxidation device and a neutralization sedimentation device. The method comprises the following steps: introducing sludge anaerobic digestion solution into the regulating tank; conveying the sludge anaerobic digestion liquid in the regulating tank into a coagulating sedimentation device for coagulating sedimentation treatment; delivering the effluent after coagulating sedimentation treatment into a Fenton catalytic oxidation device for Fenton catalytic oxidation treatment; part of effluent after Fenton catalytic oxidation treatment flows back to the water inlet end of the Fenton catalytic oxidation pond, and the rest of effluent enters a neutralization precipitation device; and (3) regulating the pH value of the rest water entering the neutralization and precipitation device in a neutralization and precipitation tank, and then carrying out neutralization and precipitation treatment. The invention realizes no acidification treatment, reduces the dosage of Fenton reaction reagent, reduces the operation cost, and improves the utilization efficiency of hydroxyl free radicals and the removal rate of organic matters.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a system for treating sludge anaerobic digestion liquid by non-acidification Fenton oxidation and a treatment method of sludge anaerobic digestion liquid.
Background
The anaerobic sludge digestion technology is one of the main technologies for recycling the sludge at present, and after the sludge is subjected to anaerobic digestion, organic components are decomposed by methanogenic bacteria to generate methane, water and carbon dioxide. In order to improve the available organic components in the sludge, the thermal hydrolysis technology is used as a sludge pretreatment technology to be applied to the anaerobic digestion process of the sludge, the sludge is subjected to thermal hydrolysis treatment, cell wall breaking and intracellular substances flowing out, and the concentration of the organic matters in the anaerobic digestion feed can be increased. However, with the process of temperature and pressure increase in the thermal hydrolysis process, the substances such as proteins, polysaccharides and the like contained in the sludge undergo chemical reactions such as caramelization reaction, maillard reaction and the like, so that the concentration of the soluble refractory organic matters is increased. The refractory organic matters cannot be utilized by organisms in the anaerobic sludge digestion process, and can enter plate and frame filtrate after anaerobic sludge digestion along with the soluble humic acid, fulvic acid and the like in the sludge, so that the treatment difficulty of the anaerobic sludge digestion liquid is increased.
A large number of experiments show that the organic matters in the anaerobic digestion of the sludge are difficult to remove by the traditional biological treatment technology. Advanced oxidation techniques, based on hydroxyl radical production (OH), have particular advantages in the removal of refractory organic materials, with Fenton technology being the most widely used. Fenton reaction refers to the use of Fe 2+ Catalytic H 2 O 2 The organic polymer has strong oxidability, OH and OH has no selectivity, and can oxidize and break the conjugated organic polymer system structure, so that persistent refractory organic matters are mineralized into carbon dioxide and water. However, the Fenton reaction is required to be carried out in an acidic environment, acid addition is an indispensable step in the Fenton reaction, and the large dosage of the medicament is one of the main defects of the Fenton process, so that the development of a low-consumption and non-acidification Fenton treatment process for treating the anaerobic digestion liquid of sludge is one of the important works of the current digestion liquid treatment.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a sludge anaerobic digestion liquid treatment process and a system which are low in treatment cost, do not need additional acid and are good in treatment effect.
To achieve the above object, according to an aspect of the present invention, there is provided a system for non-acidizing Fenton oxidation treatment of sludge anaerobic digestion solution, comprising in order: regulating tank, coagulating sedimentation device, fenton catalytic oxidation device and neutralization precipitation device, wherein:
the coagulating sedimentation device comprises: a coagulating sedimentation tank, a coagulant dosing pump and a coagulant aid dosing pump; the coagulating sedimentation tank is communicated with the regulating tank, and the front end of the coagulating sedimentation tank is provided with the coagulant dosing pump and the coagulant aid dosing pump;
the Fenton catalytic oxidation device comprises: a Fenton catalytic oxidation tank and a dosing unit; the Fenton catalytic oxidation pond is communicated with the coagulating sedimentation pond, a tail water return pipe is arranged at the water outlet end of the Fenton catalytic oxidation pond, the tail water return pipe is communicated with the water inlet end of the Fenton catalytic oxidation pond through a tail water return pump, and the dosing unit is used for dosing a medicament into the Fenton catalytic oxidation pond;
the neutralization precipitation device comprises: an alkali adding pump, a pH control unit and a neutralization sedimentation tank; the neutralization sedimentation tank is communicated with the Fenton catalytic oxidation tank, an alkali adding pump is arranged at the front end of the neutralization sedimentation tank, and the alkali adding pump is connected with the pH control unit.
Preferably, the alkali adding pump is electrically connected or in communication with the pH control unit.
The water outlet end of the Fenton catalytic oxidation pond refers to the water outlet end at the extreme end of the Fenton catalytic oxidation pond, and the water inlet end of the Fenton catalytic oxidation pond refers to the water inlet end at the extreme end of the Fenton catalytic oxidation pond. The Fenton catalytic oxidation tank is a plug-flow reactor, and is made of 316L stainless steel or a cement tank with an anti-corrosion coating.
According to the present invention, it is preferable that:
the Fenton catalytic oxidation pond is internally provided with a plurality of reagent mixing areas and reaction areas in sequence alternately; a second partition plate is used for separating each reaction zone from the medicament mixing zone arranged at the front part of each reaction zone, a first opening is formed in the upper part of the second partition plate, a third partition plate is used for separating each reaction zone from the medicament mixing zone arranged at the rear part of each reaction zone, and a second opening is formed in the lower part of the third partition plate;
the medicaments added in a first medicament mixing region of the medicament mixing regions are hydrogen peroxide and ferrous sulfate aqueous solution, and the medicaments added in other medicament mixing regions are only ferrous sulfate aqueous solution; a second stirrer is arranged in each medicament mixing zone; the first medicament mixing area is communicated with the coagulating sedimentation tank;
the lower parts of the reaction areas are respectively provided with a second sludge collecting groove, the bottoms of the second sludge collecting grooves are provided with a second exhaust valve, a catalyst supporting layer is arranged above the second sludge collecting grooves, and the catalyst supporting layers are respectively provided with a catalyst;
the dosing unit comprises a plurality of dosing units, wherein the plurality of dosing units are used for dosing the medicaments to the plurality of medicament mixing areas; and a first dosing unit of the dosing units is used for dosing hydrogen peroxide and ferrous sulfate aqueous solution into the first medicament mixing area, and other dosing units are respectively used for dosing ferrous sulfate aqueous solution into other medicament mixing areas.
According to the present invention, it is preferable that:
the first dosing unit comprises a ferrous sulfate dosing pipe, a hydrogen peroxide dosing pump and a ferrous sulfate dosing pump; the hydrogen peroxide dosing pump is connected with the hydrogen peroxide dosing pipe and is used for conveying hydrogen peroxide to the hydrogen peroxide dosing pipe; the ferrous sulfate dosing pump is connected with the ferrous sulfate dosing pipe and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe; the ferrous sulfate dosing pipe and the hydrogen peroxide dosing pipe of the first dosing unit are communicated with the first medicament mixing area;
the other dosing units comprise ferrous sulfate dosing pipes and ferrous sulfate dosing pumps; the ferrous sulfate dosing pump is connected with the ferrous sulfate dosing pipe and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe; and ferrous sulfate dosing pipes of the other dosing units are respectively communicated with the other medicament mixing areas.
In the invention, the ferrous sulfate dosing pipe and the hydrogen peroxide dosing pipe of the first dosing unit are communicated with the first medicament mixing area by being arranged on the side wall of the first medicament mixing area. The ferrous sulfate dosing pipes of the other dosing units are respectively communicated with the other medicament mixing areas through the mode of being arranged on the side walls of the other medicament mixing areas.
According to the present invention, preferably, the agent mixing zone, the reaction zone and the dosing unit are all four.
According to the invention, preferably, the coagulating sedimentation tank is an cocurrent sedimentation tank or a lateral flow sedimentation tank.
According to the present invention, it is preferable that:
the coagulating sedimentation tank sequentially comprises a coagulating area and a first sedimentation area, wherein the coagulating area is communicated with the regulating tank, and a first partition plate is arranged between the coagulating area and the first sedimentation area; a first stirrer is arranged in the coagulation zone; the utility model discloses a sedimentation tank, including first sedimentation zone, first sedimentation zone lower part is equipped with first mud collection groove, first mud collection groove bottom is provided with first exhaust valve, first mud collection groove top is equipped with first perforation inlet tube, be provided with a plurality of apopores on the first perforation inlet tube, the one end of first perforation inlet tube set up in on the first baffle, with it is connected to coagulate the district, make coagulate the solution in district can pass through first perforation inlet tube gets into first sedimentation zone, first perforation inlet tube top is equipped with first swash plate, first swash plate top is equipped with first overflow mouth.
The coagulant conveyed by the coagulant dosing pump is polymeric ferric sulfate;
the coagulant aid conveyed by the coagulant aid dosing pump is anionic polyacrylamide.
In the invention, the solution in the coagulation zone enters the sedimentation zone through a plurality of water outlet holes on the first perforated water inlet pipe.
In the invention, the pH value of the sludge anaerobic digestion liquid is 6-8, and the combined use of the polymeric ferric sulfate as a coagulant and the anionic polyacrylamide as a coagulant aid can reduce the pH value of effluent water after coagulating sedimentation treatment to below 5, thereby providing an acidic environment for Fenton catalytic oxidation treatment; and simultaneously, a part of effluent after Fenton catalytic oxidation treatment is returned to the water inlet end of the Fenton catalytic oxidation pond, and the pH value of the water inlet end of the Fenton catalytic oxidation pond is adjusted to be lower than 4 by utilizing the characteristic that the pH value of a part of effluent after Fenton catalytic oxidation treatment is lower, so that the optimal reaction condition is provided for Fenton catalytic oxidation treatment.
According to the invention, preferably, the neutralization sedimentation tank sequentially comprises a pH adjusting zone and a second sedimentation zone, wherein the pH adjusting zone is communicated with the Fenton catalytic oxidation tank, and a fourth partition plate is arranged between the pH adjusting zone and the second sedimentation zone; the pH adjusting zone is provided with a third stirrer, a third sludge collecting tank is arranged below the second sedimentation zone, a third emptying valve is arranged at the bottom of the third sludge collecting tank, a second perforated water inlet pipe is arranged above the third sludge collecting tank, a plurality of water outlet holes are formed in the second perforated water inlet pipe, one end of the second perforated water inlet pipe is arranged on the fourth partition board and communicated with the pH adjusting zone, a solution in the pH adjusting zone enters the second sedimentation zone through the second perforated water inlet pipe, a second inclined plate is arranged above the second perforated water inlet pipe, and a second overflow port is formed in the upper portion of the second inclined plate.
In the invention, the solution in the pH adjusting zone enters the precipitation zone through a plurality of water outlet holes on the second perforated water inlet pipe.
According to the invention, preferably, the connecting pipe for the adjusting tank to be communicated with the coagulating sedimentation tank, the connecting pipe for the coagulating sedimentation tank to be communicated with the Fenton catalytic oxidation tank and the connecting pipe for the Fenton catalytic oxidation tank to be communicated with the neutralization sedimentation tank are all polypropylene pipes or 316L stainless steel pipes.
The invention also provides a treatment method of the sludge anaerobic digestion liquid, which adopts the system for treating the sludge anaerobic digestion liquid by non-acidification Fenton oxidation, and comprises the following steps:
(1) Introducing sludge anaerobic digestion solution into the regulating tank, and regulating the water inflow;
(2) Conveying the sludge anaerobic digestion liquid in the regulating tank into the coagulating sedimentation device for coagulating sedimentation treatment;
(3) Delivering the effluent after the coagulating sedimentation treatment into the Fenton catalytic oxidation device for Fenton catalytic oxidation treatment; a part of effluent after Fenton catalytic oxidation treatment flows back to the water inlet end of the Fenton catalytic oxidation pond, and the rest of effluent enters the neutralization precipitation device;
(4) And the rest of effluent entering the neutralization and precipitation device is subjected to pH adjustment in the neutralization and precipitation tank, and then neutralization and precipitation treatment is carried out.
In the invention, the sludge anaerobic digestion liquid in the regulating tank is conveyed to a coagulation area of the coagulation sedimentation tank through a water inlet pump, the coagulant polymeric ferric sulfate and the coagulant aid anionic polyacrylamide are respectively added to the coagulation area of the coagulation sedimentation tank through a coagulant dosing pump and a coagulant aid dosing pump, and then mechanically stirred and coagulated in the coagulation area by using a first stirrer, and then enters a first sedimentation area, so that coagulation sedimentation treatment is completed.
In the invention, the effluent of the first sedimentation tank after coagulating sedimentation treatment is conveyed into the Fenton catalytic oxidation tank by gravity flow, and the solution in each medicament mixing zone is mechanically stirred and mixed by a second stirrer of each medicament mixing zone.
In the invention, the effluent of the second sedimentation zone is discharged through an overflow port arranged in the sedimentation zone.
According to the present invention, it is preferable that:
in the step (1):
the COD concentration in the sludge anaerobic digestion liquid is below 4000 mg/L;
in the step (2):
the coagulation time of the coagulation sedimentation treatment is 10-15 minutes, and the sedimentation time is 1-2 hours;
the coagulant used in the coagulating sedimentation treatment is polymeric ferric sulfate;
the coagulant aid used in the coagulating sedimentation treatment is anionic polyacrylamide.
In the step (3):
the ratio of the concentration of the hydrogen peroxide added to the first medicament mixing zone to the concentration of the COD in the sludge anaerobic digestion liquid added to the regulating tank is 0.8-2.5:1, a step of;
the molar concentration ratio of the hydrogen peroxide to the ferrous sulfate aqueous solution added into the first medicament mixing zone is 40-30:1, a step of;
the dosage of the ferrous sulfate aqueous solution added to the other medicament mixing zone is the same as the dosage of the ferrous sulfate aqueous solution added to the first medicament mixing zone;
the residence time of the effluent after the coagulating sedimentation treatment in each medicament mixing zone is 2-10 minutes, and the residence time in each reaction zone is 25-30 minutes;
the ratio of the water quantity of the water flowing back to the water inlet end of the Fenton catalytic oxidation tank to the water quantity of the rest of the water flowing into the neutralization precipitation device is 1:1 to 5;
the catalyst used in Fenton catalytic oxidation treatment is an iron oxide catalyst, and the addition amount of the catalyst accounts for 5/8-7/8 of the volume of the reaction zone.
In the step (4):
the pH value in the neutralization sedimentation tank is controlled to be 7.0-8.0, and the sedimentation time of the neutralization sedimentation treatment is 1-2 hours.
In the invention, the dosage of the ferrous sulfate aqueous solution added into the other medicament mixing zone is the same as that of the ferrous sulfate aqueous solution added into the first medicament mixing zone, wherein the same refers to that the molar concentrations of the ferrous sulfate aqueous solution in the other medicament mixing zone and the ferrous sulfate aqueous solution in the first medicament mixing zone are the same as that of the ferrous sulfate aqueous solution added into the first medicament mixing zone.
In the invention, the catalyst can accelerate Fenton catalytic oxidation reaction and promote degradation of organic matters. The ferrous sulfate aqueous solution is added into each reaction zone in batches, so that the utilization efficiency of free radicals is improved.
The technical scheme of the invention has the following advantages:
(1) Compared with the traditional Fenton process, the method provided by the invention has the advantages that the pH value of the effluent of the coagulating sedimentation tank can be reduced to below 5 by hydrolyzing the iron ions in the polymeric ferric sulfate added into the coagulating sedimentation tank, the requirement of the subsequent Fenton reaction is just met, the non-acidification treatment is realized, the effluent of the coagulating sedimentation tank contains a small amount of iron ions, the follow-up Fenton reaction is facilitated, the dosage of the Fenton reaction reagent can be reduced, and the running cost is reduced.
(2) Compared with the traditional Fenton process in which hydrogen peroxide and ferrous sulfate reagents are added into a reactor at one time, the method has the advantages that the ferrous sulfate is added in different points, the effect is that the hydroxyl radical generated by the Fenton reaction is excessive compared with organic matters during one-point addition, so that the hydroxyl radical participates in side reaction too much, the oxidation efficiency is reduced, and the hydroxyl radical generated by the Fenton reaction is insufficient compared with the organic matters during multi-point addition, so that the utilization rate of the hydroxyl radical is improved, and the organic matter removal rate is improved.
(3) The system for treating the sludge anaerobic digestion liquid by the acidification-free Fenton oxidation has the advantages of reasonable design, convenience in operation and use, low maintenance cost, stable operation and the like.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The foregoing and other objects, features and advantages of the invention will be apparent from the following more particular descriptions of exemplary embodiments of the invention as illustrated in the accompanying drawings wherein like reference numbers generally represent like parts throughout the exemplary embodiments of the invention.
Fig. 1 shows a schematic diagram of an apparatus for the non-acidified Fenton oxidation treatment of sludge anaerobic digestion solution according to the present invention.
Wherein, 1-equalizing basin, 2-coagulating sedimentation basin, 21-water inlet pump, 22-coagulant dosing pump, 23-coagulant aid dosing pump, 24-coagulating zone, 25-first sedimentation zone, 26-first baffle, 27-first stirrer, 28-first sludge collecting tank, 29-first emptying valve, 210-first perforated water inlet pipe, 211-first sloping plate, 212-first overflow port, 3-Fenton catalytic oxidation basin, 31-medicament mixing zone, 32-reaction zone, 33-catalyst, 34-catalyst supporting layer, 35-second sludge collecting tank, 36-tail water reflux pipe, 37-ferrous sulfate dosing pipe, 38-hydrogen peroxide dosing pipe, 39-drug dosing pump, 310-ferrous sulfate dosing pump, 311-tail water reflux pump, 312-second baffle, 313-first opening, 314-third baffle, 315-second opening, 316-second emptying valve, 317-second stirrer, 4-neutralizing sedimentation basin, 41-alkali adding pump, 42-pH control unit, 43-44-second stirrer, 48-third baffle, 43-third perforation 46-third baffle, 48-third perforation, 48-third sedimentation zone, 48-third baffle, 48-third perforation.
Fig. 2 shows a schematic diagram of a Fenton catalytic oxidation tank in an apparatus for non-acidizing Fenton oxidation treatment of sludge anaerobic digestion liquid according to the present invention.
The device comprises a 3-Fenton catalytic oxidation pond, a 31-medicament mixing area, a 32-reaction area, a 33-catalyst, a 34-catalyst supporting layer, a 35-second mud collecting groove, a 36-tail water return pipe, a 37-ferrous sulfate dosing pipe, a 38-hydrogen peroxide dosing pipe, a 39-hydrogen peroxide dosing pump, a 310-ferrous sulfate dosing pump, a 311-tail water return pump, a 312-second partition plate, a 313-first opening, a 314-third partition plate, a 315-second opening, a 316-second emptying valve and a 317-second stirrer.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the preferred embodiments of the present invention are described below, it should be understood that the present invention may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
Example 1:
anaerobic digestion is carried out on sludge in a certain Beijing sludge treatment center after a thermal hydrolysis process, and sludge after anaerobic digestion is compressed by a plate frame to generate sludge anaerobic digestion liquid, wherein COD is 2000mgThe pH value is 8.0, the ammonia nitrogen concentration is 1500mg/L, BOD 5 200mg/L, lower B/C and poorer biodegradability. The sludge anaerobic digestion liquid is treated by the system for treating the sludge anaerobic digestion liquid by non-acidification Fenton oxidation.
As shown in fig. 1 and 2, the present embodiment provides a system for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation, which sequentially includes: the device comprises a regulating tank 1, a coagulating sedimentation device, a Fenton catalytic oxidation device and a neutralization sedimentation device, wherein:
the coagulating sedimentation device comprises: a coagulating sedimentation tank 2, a coagulant dosing pump 22 and a coagulant aid dosing pump 23; the coagulating sedimentation tank 2 is communicated with the regulating tank 1, and the front end of the coagulating sedimentation tank 2 is provided with the coagulant dosing pump 22 and the coagulant aid dosing pump 23; the coagulating sedimentation tank 2 is a lateral flow sedimentation tank. The coagulating sedimentation tank 2 sequentially comprises a coagulating area 24 and a first sedimentation area 25, wherein the coagulating area 24 is communicated with the regulating tank 1, and a first partition plate 26 is arranged between the coagulating area 24 and the first sedimentation area 25; a first stirrer 27 is arranged in the coagulation zone 24; the lower part of the first sedimentation zone 25 is provided with a first sludge collecting tank 28, the bottom of the first sludge collecting tank 28 is provided with a first emptying valve 29, a first perforated water inlet pipe 210 is arranged above the first sludge collecting tank 28, a plurality of water outlet holes are arranged on the first perforated water inlet pipe 210, one end of the first perforated water inlet pipe 210 is arranged on the first partition 26 and communicated with the coagulation zone 24, so that solution in the coagulation zone 24 can enter the first sedimentation zone 25 through the water outlet holes on the first perforated water inlet pipe 210. A first inclined plate 211 is arranged above the first perforated water inlet pipe 210, and a first overflow port 212 is arranged above the first inclined plate 211. The coagulant conveyed by the coagulant dosing pump 22 is polymeric ferric sulfate; the coagulant aid conveyed by the coagulant aid dosing pump 23 is anionic polyacrylamide.
The Fenton catalytic oxidation device comprises: a Fenton catalytic oxidation tank 3 and a dosing unit; the Fenton catalytic oxidation tank 3 is communicated with the coagulating sedimentation tank 2, a tail water return pipe 36 is arranged at the water outlet end of the Fenton catalytic oxidation tank 3, the tail water return pipe 36 is communicated with the water inlet end of the Fenton catalytic oxidation tank 3 through a tail water return pump 311, and the dosing unit is used for dosing medicament into the Fenton catalytic oxidation tank 3; the Fenton catalytic oxidation tank 3 is sequentially and alternately provided with a reagent mixing zone 31 and a reaction zone 32, wherein the reagent mixing zone 31 and the reaction zone 32 are four; each reaction zone 32 is separated from the medicine mixing zone 31 arranged at the front part by a second partition plate 312, a first opening 313 is arranged at the upper part of the second partition plate 312, each reaction zone 32 is separated from the medicine mixing zone 31 arranged at the rear part by a third partition plate 314, and a second opening 315 is arranged at the lower part of the third partition plate 314;
the medicaments added in the first medicament mixing region 31 of the four medicament mixing regions 31 are hydrogen peroxide and ferrous sulfate aqueous solution, and the medicaments added in the other medicament mixing regions 31 are only ferrous sulfate aqueous solution; a second agitator 317 is provided in each of the medicament mixing sections 31; the first agent mixing zone 31 is in communication with the first sedimentation zone 25 of the coagulating sedimentation tank 2;
the lower parts of the four reaction areas 32 are respectively provided with a second mud collecting groove 35, the bottom of the second mud collecting groove 35 is provided with a second emptying valve 316, a catalyst supporting layer 34 is arranged above the second mud collecting groove 35, and the catalyst supporting layers 34 are respectively provided with a catalyst 33;
the dosing unit comprises four dosing units for dosing the four medicament mixing zones 31; the first dosing unit of the four dosing units is used for adding hydrogen peroxide and ferrous sulfate aqueous solution into the first medicament mixing area 31, and the other dosing units are respectively used for adding ferrous sulfate aqueous solution into the other medicament mixing areas 31. The first dosing unit comprises a ferrous sulfate dosing pipe 37, a hydrogen peroxide dosing pipe 38, a hydrogen peroxide dosing pump 39 and a ferrous sulfate dosing pump 310; the hydrogen peroxide dosing pump 39 is connected with the hydrogen peroxide dosing pipe 38 and is used for conveying hydrogen peroxide to the hydrogen peroxide dosing pipe 38; the ferrous sulfate dosing pump 310 is connected with the ferrous sulfate dosing pipe 37 and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe 37; the ferrous sulfate dosing pipe 37 and the hydrogen peroxide dosing pipe 38 of the first dosing unit are both communicated with the first medicament mixing region 31; the other dosing units comprise a ferrous sulfate dosing tube 37 and a ferrous sulfate dosing pump 310; the ferrous sulfate dosing pump 310 is connected with the ferrous sulfate dosing pipe 37 and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe 37; the ferrous sulfate dosing tubes 37 of the other dosing units are respectively communicated with the other medicament mixing zone 31.
The neutralization precipitation device comprises: an alkali adding pump 41, a pH control unit 42 and a neutralization sedimentation tank 4; the neutralization sedimentation tank 4 is communicated with the Fenton catalytic oxidation tank 3, an alkali adding pump 41 is arranged at the front end of the neutralization sedimentation tank 4, and the alkali adding pump 41 is electrically connected with the pH control unit 42. The neutralization sedimentation tank 4 sequentially comprises a pH adjusting area 43 and a second sedimentation area 44, wherein the pH adjusting area 43 is communicated with the last reaction area 32 of the Fenton catalytic oxidation tank 3, and a fourth partition board 45 is arranged between the pH adjusting area 43 and the second sedimentation area 44; the pH adjusting zone 43 is provided with a third stirrer 46, the lower part of the second sedimentation zone 44 is provided with a third sludge collecting groove 47, the bottom of the third sludge collecting groove 47 is provided with a third emptying valve 48, the upper part of the third sludge collecting groove 47 is provided with a second perforated water inlet pipe 49, the second perforated water inlet pipe 49 is provided with a plurality of water outlet holes, one end of the second perforated water inlet pipe 49 is arranged on the fourth partition board 45 and communicated with the pH adjusting zone 43, the solution in the pH adjusting zone 43 enters the second sedimentation zone 44 through a plurality of water outlet holes on the second perforated water inlet pipe 49, the upper part of the second perforated water inlet pipe 49 is provided with a second inclined plate 410, and the upper part of the second inclined plate 410 is provided with a second overflow port 411.
The connecting pipes of the regulating tank 1 and the coagulating sedimentation tank 2, the connecting pipe of the coagulating sedimentation tank 2 and the Fenton catalytic oxidation tank 3, and the connecting pipe of the Fenton catalytic oxidation tank 3 and the neutralization sedimentation tank 4 are polypropylene pipes.
The treatment method of the sludge anaerobic digestion liquid comprises the following steps:
(1) Introducing sludge anaerobic digestion solution into the regulating tank 1, and regulating the water inflow;
(2) The sludge anaerobic digestion liquid in the regulating tank 1 is conveyed into the coagulating sedimentation device through a water inlet pump 21 for coagulating sedimentation treatment;
the coagulation time of the coagulating sedimentation treatment is 15 minutes, the sedimentation time is 45 minutes, the coagulant used in the coagulating sedimentation treatment is polymeric ferric sulfate, and the coagulant aid used in the coagulating sedimentation treatment is anionic polyacrylamide.
(3) Delivering the effluent after the coagulating sedimentation treatment into the Fenton catalytic oxidation device by utilizing gravity flow to perform Fenton catalytic oxidation treatment; a part of effluent after Fenton catalytic oxidation treatment flows back to the water inlet end of the Fenton catalytic oxidation tank 3, and the rest of effluent enters the neutralization precipitation device;
the ratio of the concentration of hydrogen peroxide added to the first chemical mixing zone 31 to the concentration of COD in the sludge anaerobic digestion solution added to the regulating tank 1 is 2:1, a step of; the molar concentration ratio of the hydrogen peroxide and the ferrous sulfate aqueous solution added into the first medicament mixing zone 31 is 40:1, a step of; the dosage of the ferrous sulfate aqueous solution added to the other agent mixing zone 31 is the same as the molar concentration of the ferrous sulfate aqueous solution added to the first agent mixing zone 31; the residence time of the effluent after the coagulating sedimentation treatment in each reagent mixing region 31 is 5 minutes, and the residence time in each reaction region 32 is 25 minutes; the ratio of the water quantity of the water flowing back to the water inlet end of the Fenton catalytic oxidation tank 3 to the water quantity of the rest of the water flowing into the neutralization precipitation device is 1:3, a step of; the catalyst used in Fenton catalytic oxidation treatment is an iron oxide catalyst, and the addition amount of the catalyst accounts for 3/4 of the volume of the reaction zone.
(4) The rest of the effluent entering the neutralization and precipitation device is subjected to neutralization and precipitation treatment after the pH is adjusted in the neutralization and precipitation tank 4.
The pH in the neutralization sedimentation tank 4 is controlled to be 7.0-8.0, the sedimentation time of the neutralization sedimentation treatment is 1 hour, the concentration of COD in the effluent of the second sedimentation zone 44 is reduced to 442mg/L, and the effluent can be returned to the water plant for water inflow without exceeding the standard of the water plant effluent.
Example 2:
treatment of certain sewageAnaerobic digestion and plate frame dehydration are carried out on the residual sludge of the plant to generate anaerobic digestion solution, after anaerobic ammonia oxidation denitrification treatment, COD is 1000mg/L, pH is 8.0, ammonia nitrogen concentration is 80mg/L, BOD 5 The concentration is 100mg/L, the B/C is lower, and the biodegradability is poorer. The sludge anaerobic digestion liquid is treated by the system for treating the sludge anaerobic digestion liquid by non-acidification Fenton oxidation.
As shown in fig. 1 and 2, the present embodiment provides a system for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation, which sequentially includes: the device comprises a regulating tank 1, a coagulating sedimentation device, a Fenton catalytic oxidation device and a neutralization sedimentation device, wherein:
the coagulating sedimentation device comprises: a coagulating sedimentation tank 2, a coagulant dosing pump 22 and a coagulant aid dosing pump 23; the coagulating sedimentation tank 2 is communicated with the regulating tank 1, and the front end of the coagulating sedimentation tank 2 is provided with the coagulant dosing pump 22 and the coagulant aid dosing pump 23; the coagulating sedimentation tank 2 is a lateral flow sedimentation tank. The coagulating sedimentation tank 2 sequentially comprises a coagulating area 24 and a first sedimentation area 25, wherein the coagulating area 24 is communicated with the regulating tank 1, and a first partition plate 26 is arranged between the coagulating area 24 and the first sedimentation area 25; a first stirrer 27 is arranged in the coagulation zone 24; the lower part of the first sedimentation zone 25 is provided with a first sludge collecting tank 28, the bottom of the first sludge collecting tank 28 is provided with a first emptying valve 29, a first perforated water inlet pipe 210 is arranged above the first sludge collecting tank 28, a plurality of water outlet holes are arranged on the first perforated water inlet pipe 210, one end of the first perforated water inlet pipe 210 is arranged on the first partition 26 and communicated with the coagulation zone 24, so that solution in the coagulation zone 24 can enter the first sedimentation zone 25 through the water outlet holes on the first perforated water inlet pipe 210. A first inclined plate 211 is arranged above the first perforated water inlet pipe 210, and a first overflow port 212 is arranged above the first inclined plate 211. The coagulant conveyed by the coagulant dosing pump 22 is polymeric ferric sulfate; the coagulant aid conveyed by the coagulant aid dosing pump 23 is anionic polyacrylamide.
The Fenton catalytic oxidation device comprises: a Fenton catalytic oxidation tank 3 and a dosing unit; the Fenton catalytic oxidation tank 3 is communicated with the coagulating sedimentation tank 2, a tail water return pipe 36 is arranged at the water outlet end of the Fenton catalytic oxidation tank 3, the tail water return pipe 36 is communicated with the water inlet end of the Fenton catalytic oxidation tank 3 through a tail water return pump 311, and the dosing unit is used for dosing medicament into the Fenton catalytic oxidation tank 3; the Fenton catalytic oxidation tank 3 is sequentially and alternately provided with a reagent mixing zone 31 and a reaction zone 32, wherein the reagent mixing zone 31 and the reaction zone 32 are four; each reaction zone 32 is separated from the medicine mixing zone 31 arranged at the front part by a second partition plate 312, a first opening 313 is arranged at the upper part of the second partition plate 312, each reaction zone 32 is separated from the medicine mixing zone 31 arranged at the rear part by a third partition plate 314, and a second opening 315 is arranged at the lower part of the third partition plate 314;
the medicaments added in the first medicament mixing region 31 of the four medicament mixing regions 31 are hydrogen peroxide and ferrous sulfate aqueous solution, and the medicaments added in the other medicament mixing regions 31 are only ferrous sulfate aqueous solution; a second agitator 317 is provided in each of the medicament mixing sections 31; the first agent mixing zone 31 is in communication with the first sedimentation zone 25 of the coagulating sedimentation tank 2;
the lower parts of the four reaction areas 32 are respectively provided with a second mud collecting groove 35, the bottom of the second mud collecting groove 35 is provided with a second emptying valve 316, a catalyst supporting layer 34 is arranged above the second mud collecting groove 35, and the catalyst supporting layers 34 are respectively provided with a catalyst 33;
the dosing unit comprises four dosing units for dosing the four medicament mixing zones 31; the first dosing unit of the four dosing units is used for adding hydrogen peroxide and ferrous sulfate aqueous solution into the first medicament mixing area 31, and the other dosing units are respectively used for adding ferrous sulfate aqueous solution into the other medicament mixing areas 31. The first dosing unit comprises a ferrous sulfate dosing pipe 37, a hydrogen peroxide dosing pipe 38, a hydrogen peroxide dosing pump 39 and a ferrous sulfate dosing pump 310; the hydrogen peroxide dosing pump 39 is connected with the hydrogen peroxide dosing pipe 38 and is used for conveying hydrogen peroxide to the hydrogen peroxide dosing pipe 38; the ferrous sulfate dosing pump 310 is connected with the ferrous sulfate dosing pipe 37 and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe 37; the ferrous sulfate dosing pipe 37 and the hydrogen peroxide dosing pipe 38 of the first dosing unit are both communicated with the first medicament mixing region 31; the other dosing units comprise a ferrous sulfate dosing tube 37 and a ferrous sulfate dosing pump 310; the ferrous sulfate dosing pump 310 is connected with the ferrous sulfate dosing pipe 37 and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe 37; the ferrous sulfate dosing tubes 37 of the other dosing units are respectively communicated with the other medicament mixing zone 31.
The neutralization precipitation device comprises: an alkali adding pump 41, a pH control unit 42 and a neutralization sedimentation tank 4; the neutralization sedimentation tank 4 is communicated with the Fenton catalytic oxidation tank 3, an alkali adding pump 41 is arranged at the front end of the neutralization sedimentation tank 4, and the alkali adding pump 41 is in communication connection with the pH control unit 42. The neutralization sedimentation tank 4 sequentially comprises a pH adjusting area 43 and a second sedimentation area 44, wherein the pH adjusting area 43 is communicated with the last reaction area 32 of the Fenton catalytic oxidation tank 3, and a fourth partition board 45 is arranged between the pH adjusting area 43 and the second sedimentation area 44; the pH adjusting zone 43 is provided with a third stirrer 46, the lower part of the second sedimentation zone 44 is provided with a third sludge collecting groove 47, the bottom of the third sludge collecting groove 47 is provided with a third emptying valve 48, the upper part of the third sludge collecting groove 47 is provided with a second perforated water inlet pipe 49, the second perforated water inlet pipe 49 is provided with a plurality of water outlet holes, one end of the second perforated water inlet pipe 49 is arranged on the fourth partition board 45 and communicated with the pH adjusting zone 43, the solution in the pH adjusting zone 43 enters the second sedimentation zone 44 through a plurality of water outlet holes on the second perforated water inlet pipe 49, the upper part of the second perforated water inlet pipe 49 is provided with a second inclined plate 410, and the upper part of the second inclined plate 410 is provided with a second overflow port 411.
The connecting pipes of the regulating tank 1 and the coagulating sedimentation tank 2, the connecting pipe of the coagulating sedimentation tank 2 and the Fenton catalytic oxidation tank 3, and the connecting pipe of the Fenton catalytic oxidation tank 3 and the neutralization sedimentation tank 4 are polypropylene pipes.
The treatment method of the sludge anaerobic digestion liquid comprises the following steps:
(1) Introducing sludge anaerobic digestion solution into the regulating tank 1, and regulating the water inflow;
(2) The sludge anaerobic digestion liquid in the regulating tank 1 is conveyed into the coagulating sedimentation device through a water inlet pump 21 for coagulating sedimentation treatment;
the coagulation time of the coagulating sedimentation treatment is 15 minutes, the sedimentation time is 45 minutes, the coagulant used in the coagulating sedimentation treatment is polymeric ferric sulfate, and the coagulant aid used in the coagulating sedimentation treatment is anionic polyacrylamide.
(3) Delivering the effluent after the coagulating sedimentation treatment into the Fenton catalytic oxidation device by utilizing gravity flow to perform Fenton catalytic oxidation treatment; a part of effluent after Fenton catalytic oxidation treatment flows back to the water inlet end of the Fenton catalytic oxidation tank 3, and the rest of effluent enters the neutralization precipitation device;
the ratio of the concentration of hydrogen peroxide added to the first chemical mixing zone 31 to the concentration of COD in the sludge anaerobic digestion solution added to the conditioning tank 1 was 2.5:1, a step of; the molar concentration ratio of the hydrogen peroxide and the ferrous sulfate aqueous solution added into the first medicament mixing zone 31 is 40:1, a step of; the dosage of the ferrous sulfate aqueous solution added to the other agent mixing zone 31 is the same as the molar concentration of the ferrous sulfate aqueous solution added to the first agent mixing zone 31; the residence time of the effluent after the coagulating sedimentation treatment in each reagent mixing region 31 is 5 minutes, and the residence time in each reaction region 32 is 25 minutes; the ratio of the water quantity of the water flowing back to the water inlet end of the Fenton catalytic oxidation tank 3 to the water quantity of the rest of the water flowing into the neutralization precipitation device is 1:3, a step of; the catalyst used in Fenton catalytic oxidation treatment is an iron oxide catalyst, and the addition amount of the catalyst accounts for 3/4 of the volume of the reaction zone.
(4) The rest of the effluent entering the neutralization and precipitation device is subjected to neutralization and precipitation treatment after the pH is adjusted in the neutralization and precipitation tank 4.
The pH in the neutralization sedimentation tank 4 is controlled to be 7.0-8.0, the sedimentation time of the neutralization sedimentation treatment is 1 hour, and the concentration of COD in the effluent of the second sedimentation zone 44 is reduced to 260mg/L, so that the effluent can be directly discharged to a municipal sewage pipeline.
According to the two embodiments, the sludge anaerobic digestion liquid acidification-free Fenton catalytic oxidation treatment system can effectively remove COD in the sludge anaerobic digestion liquid, ensure that the concentration of COD in the effluent can reach the expected effect, and can meet the actual operation requirement.
The foregoing description of embodiments of the invention has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the various embodiments described.
Claims (7)
1. The method for treating the sludge anaerobic digestion liquid by non-acidification Fenton oxidation is characterized in that the adopted system sequentially comprises the following steps: regulating tank, coagulating sedimentation device, fenton catalytic oxidation device and neutralization precipitation device, wherein:
the coagulating sedimentation device comprises: a coagulating sedimentation tank, a coagulant dosing pump and a coagulant aid dosing pump; the coagulating sedimentation tank is communicated with the regulating tank, and the front end of the coagulating sedimentation tank is provided with the coagulant dosing pump and the coagulant aid dosing pump;
the coagulant conveyed by the coagulant dosing pump is polymeric ferric sulfate;
the coagulant aid conveyed by the coagulant aid dosing pump is anionic polyacrylamide;
the Fenton catalytic oxidation device comprises: a Fenton catalytic oxidation tank and a dosing unit; the Fenton catalytic oxidation pond is communicated with the coagulating sedimentation pond, a tail water return pipe is arranged at the water outlet end of the Fenton catalytic oxidation pond, the tail water return pipe is communicated with the water inlet end of the Fenton catalytic oxidation pond through a tail water return pump, and the dosing unit is used for dosing a medicament into the Fenton catalytic oxidation pond;
the neutralization precipitation device comprises: an alkali adding pump, a pH control unit and a neutralization sedimentation tank; the neutralization sedimentation tank is communicated with the Fenton catalytic oxidation tank, an alkali adding pump is arranged at the front end of the neutralization sedimentation tank, and the alkali adding pump is connected with the pH control unit;
the Fenton catalytic oxidation pond is internally provided with a reagent mixing area and a reaction area in sequence alternately, and the number of the reagent mixing area and the reaction area is four; a second partition plate is used for separating each reaction zone from the medicament mixing zone arranged at the front part of each reaction zone, a first opening is formed in the upper part of the second partition plate, a third partition plate is used for separating each reaction zone from the medicament mixing zone arranged at the rear part of each reaction zone, and a second opening is formed in the lower part of the third partition plate;
the medicaments added in the first medicament mixing area of the four medicament mixing areas are hydrogen peroxide and ferrous sulfate aqueous solution, and the medicaments added in the other medicament mixing areas are only ferrous sulfate aqueous solution; a second stirrer is arranged in each medicament mixing zone; the first medicament mixing area is communicated with the coagulating sedimentation tank;
the lower parts of the four reaction areas are respectively provided with a second sludge collecting groove, the bottoms of the second sludge collecting grooves are provided with a second exhaust valve, a catalyst supporting layer is arranged above the second sludge collecting grooves, and the catalyst supporting layers are respectively provided with a catalyst;
the dosing unit comprises four dosing units, and the four dosing units are used for dosing medicaments to the four medicament mixing areas; a first dosing unit of the four dosing units is used for dosing hydrogen peroxide and ferrous sulfate aqueous solution into the first medicament mixing area, and other dosing units are respectively used for dosing ferric sulfate aqueous solution into other medicament mixing areas;
the method comprises the following steps:
(1) Introducing sludge anaerobic digestion solution into the regulating tank, and regulating the water inflow;
(2) Conveying the sludge anaerobic digestion liquid in the regulating tank into the coagulating sedimentation device for coagulating sedimentation treatment;
(3) Delivering the effluent after the coagulating sedimentation treatment into the Fenton catalytic oxidation device for Fenton catalytic oxidation treatment; part of effluent after Fenton catalytic oxidation treatment flows back to the water inlet end of the Fenton catalytic oxidation pond, and the rest of effluent enters the neutralization precipitation device;
(4) The rest of the effluent entering the neutralization and precipitation device is subjected to pH adjustment in the neutralization and precipitation tank, and then neutralization and precipitation treatment is carried out;
the pH value of the sludge anaerobic digestion liquid is 6-8, the pH value of the effluent after coagulating sedimentation treatment is below 5, and the pH value of the inlet water at the water inlet end of the Fenton catalytic oxidation pond is regulated to be below 4 by utilizing part of the effluent after Fenton catalytic oxidation treatment;
the molar concentration ratio of the hydrogen peroxide to the ferrous sulfate aqueous solution added into the first medicament mixing zone is 40-30:1, a step of;
the amount of the ferrous sulfate aqueous solution added to the other agent mixing zone is the same as the amount of the ferrous sulfate aqueous solution added to the first agent mixing zone.
2. The method for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation treatment according to claim 1, wherein,
the first dosing unit comprises a ferrous sulfate dosing pipe, a hydrogen peroxide dosing pump and a ferrous sulfate dosing pump; the hydrogen peroxide dosing pump is connected with the hydrogen peroxide dosing pipe and is used for conveying hydrogen peroxide to the hydrogen peroxide dosing pipe; the ferrous sulfate dosing pump is connected with the ferrous sulfate dosing pipe and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe; the ferrous sulfate dosing pipe and the hydrogen peroxide dosing pipe of the first dosing unit are communicated with the first medicament mixing area;
the other dosing units comprise ferrous sulfate dosing pipes and ferrous sulfate dosing pumps; the ferrous sulfate dosing pump is connected with the ferrous sulfate dosing pipe and is used for conveying ferrous sulfate aqueous solution to the ferrous sulfate dosing pipe; and ferrous sulfate dosing pipes of the other dosing units are respectively communicated with the other medicament mixing areas.
3. The method for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation according to claim 1, wherein the coagulating sedimentation tank is an anisotropic flow sedimentation tank or a lateral flow sedimentation tank.
4. The method for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation treatment according to any one of claims 1 to 3, wherein,
the coagulating sedimentation tank sequentially comprises a coagulating area and a first sedimentation area, wherein the coagulating area is communicated with the regulating tank, and a first partition plate is arranged between the coagulating area and the first sedimentation area; a first stirrer is arranged in the coagulation zone; the utility model discloses a sedimentation tank, including first sedimentation zone, first sedimentation zone lower part is equipped with first mud collection groove, first mud collection groove bottom is provided with first exhaust valve, first mud collection groove top is equipped with first perforation inlet tube, be provided with a plurality of apopores on the first perforation inlet tube, the one end of first perforation inlet tube set up in on the first baffle, with it is connected to coagulate the district, make coagulate the solution in district can pass through first perforation inlet tube gets into first sedimentation zone, first perforation inlet tube top is equipped with first swash plate, first swash plate top is equipped with first overflow mouth.
5. The method for treating sludge anaerobic digestion liquid by non-acidification Fenton oxidation treatment according to claim 1, wherein the neutralization sedimentation tank sequentially comprises a pH adjustment zone and a second sedimentation zone, wherein the pH adjustment zone is communicated with the Fenton catalytic oxidation tank, and a fourth partition plate is arranged between the pH adjustment zone and the second sedimentation zone; the pH adjusting zone is provided with a third stirrer, a third sludge collecting tank is arranged below the second sedimentation zone, a third emptying valve is arranged at the bottom of the third sludge collecting tank, a second perforated water inlet pipe is arranged above the third sludge collecting tank, a plurality of water outlet holes are formed in the second perforated water inlet pipe, one end of the second perforated water inlet pipe is arranged on the fourth partition board and communicated with the pH adjusting zone, a solution in the pH adjusting zone enters the second sedimentation zone through the second perforated water inlet pipe, a second inclined plate is arranged above the second perforated water inlet pipe, and a second overflow port is formed in the upper portion of the second inclined plate.
6. The method for treating sludge anaerobic digestion liquid without acidification Fenton oxidation according to claim 1, wherein the connecting pipe of the regulating tank and the coagulating sedimentation tank, the connecting pipe of the coagulating sedimentation tank and the Fenton catalytic oxidation tank, and the connecting pipe of the Fenton catalytic oxidation tank and the neutralization sedimentation tank are polypropylene pipes or 316L stainless steel pipes.
7. The method for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation treatment according to claim 1, wherein:
in the step (1):
the COD concentration in the sludge anaerobic digestion liquid is below 4000 mg/L;
in the step (2):
the coagulation time of the coagulation sedimentation treatment is 10-15 minutes, and the sedimentation time is 1-2 hours;
in the step (3):
the ratio of the concentration of the hydrogen peroxide added to the first medicament mixing zone to the concentration of the COD in the sludge anaerobic digestion liquid added to the regulating tank is 0.8-2.5:1, a step of;
the residence time of the effluent after the coagulating sedimentation treatment in each reagent mixing zone is 2-10 minutes, and the residence time in each reaction zone is 25-30 minutes;
the ratio of the water quantity of the water flowing back to the water inlet end of the Fenton catalytic oxidation tank to the water quantity of the rest of the water flowing into the neutralization precipitation device is 1: 1-5;
the catalyst used in Fenton catalytic oxidation treatment is an iron oxide catalyst, and the addition amount of the catalyst accounts for 5/8-7/8 of the volume of the reaction zone;
in the step (4):
the pH in the neutralization sedimentation tank is controlled to be 7.0-8.0, and the sedimentation time of the neutralization sedimentation treatment is 1-2 hours.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010911932.7A CN112028320B (en) | 2020-09-02 | 2020-09-02 | System for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation and treatment method of sludge anaerobic digestion solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010911932.7A CN112028320B (en) | 2020-09-02 | 2020-09-02 | System for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation and treatment method of sludge anaerobic digestion solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112028320A CN112028320A (en) | 2020-12-04 |
| CN112028320B true CN112028320B (en) | 2024-02-02 |
Family
ID=73591358
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010911932.7A Active CN112028320B (en) | 2020-09-02 | 2020-09-02 | System for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation and treatment method of sludge anaerobic digestion solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112028320B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115417486B (en) * | 2022-07-28 | 2023-11-03 | 北京城市排水集团有限责任公司 | Device and method for treating sewage by push-flow type multipoint Fenton oxidation |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012167176A (en) * | 2011-02-14 | 2012-09-06 | Aqua Trim:Kk | Cleaning and deodorization treatment method and device for waste plastics using fenton oxidation method |
| CN105399196A (en) * | 2015-12-12 | 2016-03-16 | 沧州泓海化工有限公司 | A sewage Fenton treating agent |
| CN108706787A (en) * | 2018-08-16 | 2018-10-26 | 台州学院 | A kind of Fenton oxidation device |
| CN109879524A (en) * | 2019-01-22 | 2019-06-14 | 广东百川化工有限公司 | Water paint wastewater treatment method |
| CN111268849A (en) * | 2018-12-05 | 2020-06-12 | 苏州苏讯环保科技有限公司 | Efficient wastewater treatment process based on Fenton reaction |
| CN212770243U (en) * | 2020-09-02 | 2021-03-23 | 北京城市排水集团有限责任公司 | System for acidation-free Fenton oxidation treatment of sludge anaerobic digestion liquid |
-
2020
- 2020-09-02 CN CN202010911932.7A patent/CN112028320B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2012167176A (en) * | 2011-02-14 | 2012-09-06 | Aqua Trim:Kk | Cleaning and deodorization treatment method and device for waste plastics using fenton oxidation method |
| CN105399196A (en) * | 2015-12-12 | 2016-03-16 | 沧州泓海化工有限公司 | A sewage Fenton treating agent |
| CN108706787A (en) * | 2018-08-16 | 2018-10-26 | 台州学院 | A kind of Fenton oxidation device |
| CN111268849A (en) * | 2018-12-05 | 2020-06-12 | 苏州苏讯环保科技有限公司 | Efficient wastewater treatment process based on Fenton reaction |
| CN109879524A (en) * | 2019-01-22 | 2019-06-14 | 广东百川化工有限公司 | Water paint wastewater treatment method |
| CN212770243U (en) * | 2020-09-02 | 2021-03-23 | 北京城市排水集团有限责任公司 | System for acidation-free Fenton oxidation treatment of sludge anaerobic digestion liquid |
Non-Patent Citations (1)
| Title |
|---|
| 温青等.环境工程学.哈尔滨工程大学出版社,2008,(第1版),42-45. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112028320A (en) | 2020-12-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201962168U (en) | System for strengthening denitrification and dephosphorization effects of A2/O process | |
| CN101219837B (en) | Ozonation process and equipment for oil-containing alkali wastewater | |
| CN109279740A (en) | One kind being suitable for swag high concentrated organic wastewater advanced treatment system and method | |
| CN104016550B (en) | Sewage water treatment method in Apparel Manufacturing | |
| CN112028320B (en) | System for treating sludge anaerobic digestion solution by non-acidification Fenton oxidation and treatment method of sludge anaerobic digestion solution | |
| CN114133117A (en) | Full-scale treatment system and treatment method for supernatant liquid of sludge dewatering | |
| CN211770809U (en) | High-pollution degradation-resistant wastewater efficient treatment device | |
| CN209567946U (en) | DMF low-pressure distillation recycles column overhead waste water treatment system in film production | |
| CN210795996U (en) | Integrated integrated equipment for treating landfill leachate MBR effluent based on membrane Fenton oxidation technology | |
| CN212770243U (en) | System for acidation-free Fenton oxidation treatment of sludge anaerobic digestion liquid | |
| CN207608391U (en) | A kind of tandem AO collaborations denitrogenation dephosphorizing dosing sewage disposal system | |
| CN108751596A (en) | A kind of processing method of the high phosphorous high organic matter azoic coupling component production waste water of high chroma | |
| CN215403640U (en) | Sewage treatment system for releasing sludge carbon source by utilizing sludge biological method of sewage plant | |
| CN108862849A (en) | The treatment process and processing system of Almond debitterizing wastewater | |
| CN212609953U (en) | Fenton oxidation unit of high-efficient utilization | |
| CN205419926U (en) | Low energy consumption enhanced nitrogen removal phosphorus removal device | |
| CN213012353U (en) | Fenton reaction device for PVA production wastewater treatment | |
| CN103936237A (en) | Sewage treatment device based on cryptic growth and energy uncoupling metabolism combination and sewage treatment method thereof | |
| CN107804933A (en) | One kind is containing hypophosphites, phosphite sewage treatment equipment | |
| CN211770554U (en) | A processing apparatus for leachate short cut nitrification denitrification | |
| CN113880318A (en) | Two-stage advanced oxidation process, system and application for treating chemical wastewater | |
| CN211255496U (en) | High-standard advanced treatment system for refractory organic matters in comprehensive wastewater of industrial park | |
| CN208022809U (en) | One kind is containing hypophosphites, phosphite sewage treatment equipment | |
| CN113060898A (en) | Recycling method for generating carbon source by hydrolyzing and acidifying sludge in sewage plant | |
| CN102249475A (en) | Treatment method of membrane filtration concentrated solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |