CN114684997A - Treatment method for reducing industrial excess sludge - Google Patents
Treatment method for reducing industrial excess sludge Download PDFInfo
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- CN114684997A CN114684997A CN202011594125.3A CN202011594125A CN114684997A CN 114684997 A CN114684997 A CN 114684997A CN 202011594125 A CN202011594125 A CN 202011594125A CN 114684997 A CN114684997 A CN 114684997A
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- 239000010802 sludge Substances 0.000 title claims abstract description 112
- 238000011282 treatment Methods 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 61
- 239000011574 phosphorus Substances 0.000 claims abstract description 61
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 61
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 15
- 230000003750 conditioning effect Effects 0.000 claims abstract description 14
- 239000000701 coagulant Substances 0.000 claims abstract description 12
- 238000005345 coagulation Methods 0.000 claims abstract description 6
- 230000015271 coagulation Effects 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 10
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 8
- 239000000920 calcium hydroxide Substances 0.000 claims description 8
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- 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 7
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 7
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 6
- 239000011790 ferrous sulphate Substances 0.000 claims description 6
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 6
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 6
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 6
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 6
- 238000005352 clarification Methods 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- -1 alum Chemical compound 0.000 claims description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 3
- 239000000292 calcium oxide Substances 0.000 claims description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 3
- 239000002131 composite material Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- URRHWTYOQNLUKY-UHFFFAOYSA-N [AlH3].[P] Chemical compound [AlH3].[P] URRHWTYOQNLUKY-UHFFFAOYSA-N 0.000 claims description 2
- 229940037003 alum Drugs 0.000 claims description 2
- 229960002089 ferrous chloride Drugs 0.000 claims description 2
- 150000002505 iron Chemical class 0.000 claims description 2
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 claims description 2
- 238000010907 mechanical stirring Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 239000010865 sewage Substances 0.000 abstract description 15
- 239000004902 Softening Agent Substances 0.000 abstract description 4
- 230000018044 dehydration Effects 0.000 abstract description 2
- 238000006297 dehydration reaction Methods 0.000 abstract description 2
- 238000002156 mixing Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000002351 wastewater Substances 0.000 description 12
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 11
- 239000011575 calcium Substances 0.000 description 11
- 229920002401 polyacrylamide Polymers 0.000 description 10
- 230000005484 gravity Effects 0.000 description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 6
- 229910052791 calcium Inorganic materials 0.000 description 6
- 229910001424 calcium ion Inorganic materials 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 5
- 239000008394 flocculating agent Substances 0.000 description 5
- 229910001425 magnesium ion Inorganic materials 0.000 description 5
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000010842 industrial wastewater Substances 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 125000000129 anionic group Chemical group 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 159000000014 iron salts Chemical class 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- USHAGKDGDHPEEY-UHFFFAOYSA-L potassium persulfate Chemical compound [K+].[K+].[O-]S(=O)(=O)OOS([O-])(=O)=O USHAGKDGDHPEEY-UHFFFAOYSA-L 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 238000009388 chemical precipitation Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- 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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/143—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
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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
- 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
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/05—Conductivity or salinity
- C02F2209/055—Hardness
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- 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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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
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- Chemical Kinetics & Catalysis (AREA)
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Abstract
The method comprises the steps of adding the excess sludge of a biochemical unit into a reaction zone of a phosphorus removal unit and a coagulation zone of a hardness removal unit, adding the sludge of the phosphorus removal unit and the hardness removal unit into a sludge concentration tank of the biochemical unit, mixing the sludge with other excess sludge in the sludge concentration tank, and then feeding the sludge into a sludge storage tank for conditioning. The invention combines the excess sludge treatment of the biochemical unit with the dephosphorization and hardness removal of the sewage plant, thereby reducing the dosage of dephosphorization agents and coagulants; the sludge of the phosphorus removal unit and the hardness removal unit is added into the sludge concentration tank of the biochemical unit, and the sludge in the sludge concentration tank is subjected to preliminary flocculation-removing and dehydration by using the residual phosphorus removal agent, the softening agent and the coagulant of the phosphorus removal unit and the hardness removal unit, so that the adding amount of the conditioning agent in the sludge storage tank is reduced. The treatment method is suitable for any sewage plant, does not need to change the existing sludge conditioner and structures, and has strong implementability.
Description
Technical Field
The invention relates to the field of sludge treatment, in particular to a treatment method for reducing excess sludge, belonging to the technical field of environmental protection.
Background
In the sewage treatment process, the secondary treatment usually adopts biochemical treatment, excess sludge generated by a biochemical unit needs to be further treated, and for most industrial sewage treatment plants, the excess sludge is concentrated and dehydrated and then is subjected to outsourcing treatment. The excess sludge is usually concentrated by a sludge concentration tank, and the concentrated sludge enters a sludge storage tank for conditioning treatment and then is mechanically dewatered. The conditioning treatment of excess sludge is generally divided into physical conditioning and chemical conditioning. At present, a chemical conditioning method is widely applied to a sewage treatment plant. Chemical conditioners are divided into inorganic conditioners and organic conditioners, wherein the inorganic conditioners mainly comprise aluminum salts, iron salts and calcium salts.
With the increasing strictness of the wastewater discharge standard, the total phosphorus emission concentration is not higher than 0.5mg/L and the total discharge amount of wastewater is required in the discharge standard of partial regions or partial industries. Therefore, for most industrial wastewater treatment plants, the wastewater can reach the standard and be discharged by adding a deep phosphorus removal unit and a wastewater reuse unit on the basis of primary treatment and secondary treatment. At present, a deep phosphorus removal method of a sewage plant is mainly a chemical precipitation phosphorus removal method, and the chemical phosphorus removal method has the advantages of high efficiency, stable effect, difficulty in being influenced by the quality of wastewater and the like, but when the total phosphorus concentration in water is low, the addition amount of a phosphorus removal agent is not in direct proportion to the treatment effect, the total phosphorus concentration of effluent can reach 0.5-1.0 mg/L only when the addition amount of a typical metal salt phosphorus removal agent (such as aluminum salt and iron salt) is 1.0-2.0 mol of metal salt per mol of phosphorus removal, and when the total phosphorus concentration of the effluent is less than 0.5mg/L, the required addition amount is higher. The wastewater reuse unit usually adopts a double-membrane technology (ultrafiltration and reverse osmosis), calcium and magnesium ions of incoming water need to be removed in order to prevent the membrane unit from scaling, and the calcium and magnesium ions are generally chemically precipitated due to the high content of the calcium and magnesium ions in most industrial wastewater. Inorganic flocculants of aluminum salts or iron salts (such as polyaluminium chloride, polyferric sulfate and the like) and macromolecular organic coagulant aids are commonly used in the coagulation process.
CN111453958A discloses a cavitation-based excess sludge dewatering agent decrement adding method, belonging to the field of cavitation technology and application thereof. CN111087163A discloses a preparation method and application of a sludge dewatering conditioner, which is characterized in that the calcined ferric salt sludge and potassium persulfate are compounded into the sludge dewatering conditioner, the dewatered sludge is calcined again, and the residue is compounded with potassium persulfate, so that the sludge dewatering conditioner can be used as the dewatering conditioner again to achieve the purpose of circulation. CN110451768A discloses a method for treating excess sludge in a secondary sedimentation tank by combining a reaction tank and a gravity concentration tank, which combines the reaction tank and the gravity concentration tank, effectively reduces the solid-liquid separation time of the gravity concentration tank, and has the advantages of high efficiency, short settling time, small occupied area, low operation cost and the like. All of the above methods require the introduction of new technologies, new conditioners and new sludge treatment units.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides a treatment method for reducing the industrial excess sludge, which optimizes the excess sludge of a biochemical unit and combines the excess sludge with a phosphorus removal unit and a hardness removal unit on the basis of not changing the existing excess sludge conditioner and structures of a sewage plant, thereby not only optimizing the dosage of the conditioning agent of the biochemical unit, but also reducing the dosage of the phosphorus removal agent of the phosphorus removal unit and the coagulant of the hardness removal (calcium and magnesium ion removal) unit. The method is widely applied to industrial wastewater treatment plants, and can effectively perform sludge reduction treatment.
In order to achieve the technical purpose, the technical scheme adopted by the invention is as follows:
the method comprises the steps of adding the excess sludge of a biochemical unit into a reaction zone of a phosphorus removal unit and a coagulation zone of a hardness removal unit, adding the sludge of the phosphorus removal unit and the hardness removal unit into a sludge concentration tank of the biochemical unit, mixing the sludge with other excess sludge in the sludge concentration tank, and then feeding the sludge into a sludge storage tank for conditioning treatment.
Further, the excess sludge in the biochemical unit is sludge discharged from a reaction tank of the biochemical unit, or concentrated sludge with water content reduced to 98% -95% after concentration treatment. The sludge in the biochemical unit reaction tank can be fed through a pipeline by using gravity, and can also be fed through the pipeline by using a sludge lifting pump; the concentrated sludge can only be added through a pipeline by using gravity.
Further, the sludge of the phosphorus removal unit and the hardness removal unit is added into a sludge concentration tank of the biochemical unit from the upper part to be mixed and reacted with other residual sludge in the sludge concentration tank, and then enters a sludge storage tank for conditioning treatment. Wherein, the sludge storage tank is provided with a stirring system and a dosing system.
Further, in the phosphorus removal unit, the adding amount of the excess sludge is 5-20% of the adding amount of the phosphorus removal medicament, preferably 10-20%; in the hardness removal unit, the addition amount of the excess sludge is 5-30% of the addition amount of the coagulant, preferably 10-15% by weight.
Further, the process flows of the phosphorus removal unit and the hard removal unit are as follows: reaction-coagulation-solid/liquid separation. The dephosphorization unit and the hardness removal unit can be one of a high-density clarification tank, a reaction tank-coagulation tank-sedimentation tank or a reaction tank-mechanical stirring clarification tank, and the high-density clarification tank is preferred.
Further, the phosphorus removing agent of the phosphorus removing unit is selected from one of ferric chloride, ferrous chloride, alum, aluminum chloride, ferric sulfate, ferrous sulfate, polymeric ferric sulfate, polymeric aluminum chloride, or other composite iron salt and aluminum salt phosphorus removing agents.
Furthermore, the coagulant of the hardness removing unit is one of polymeric ferric sulfate, polymeric aluminum chloride or other compound polymeric ferric aluminum salts.
Further, the total phosphorus concentration in the water from the phosphorus removal unit is not higher than 8mg/L, preferably less than 5 mg/L; the pH of the incoming water is in the range of 5 to 8, and the wastewater which is not in this range needs to be adjusted to a pH value in this range by an acid or an alkali.
Furthermore, the softening agent adopted in the reaction zone of the hardness removal unit is one or more selected from sodium hydroxide, sodium carbonate, calcium hydroxide and calcium oxide, and calcium hydroxide or calcium oxide is preferred.
Compared with the prior art, the invention has the following beneficial effects:
the invention provides a treatment method for reducing industrial excess sludge, which combines the excess sludge treatment of a biochemical unit with a phosphorus removal unit and a hardness removal unit of a sewage plant, thereby not only reducing the dosage of a phosphorus removal medicament of the phosphorus removal unit and a coagulant of the hardness removal unit (removing calcium and magnesium ions); the sludge in the sludge concentration tank is primarily subjected to flocculation-removing and dehydration by a mode of adding the sludge in the phosphorus removal unit and the hardness removal unit into the sludge concentration tank of the biochemical unit and by using the residual phosphorus removal agent, softening agent and coagulant in the phosphorus removal unit and the hardness removal unit, so that the adding amount of the conditioning agent in the sludge storage tank is reduced. The treatment method is suitable for any sewage plant, does not need to change the existing sludge conditioner and structures, and has strong implementability.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
FIG. 1 is a schematic process flow diagram of example 1;
FIG. 2 is a schematic process flow diagram of example 2.
Detailed Description
The following non-limiting examples are presented to enable those of ordinary skill in the art to more fully understand the present invention and are not intended to limit the invention in any way.
Example 1
The embodiment discloses a treatment method for reducing excess sludge of petrochemical enterprises, and the treatment method is shown in figure 1, wherein each unit adopts conventional devices or equipment of the enterprises. The effluent quality of the biochemical unit is as follows: COD 48mg/L, total nitrogen 38mg/L, ammonia nitrogen 5.8mg/L, total phosphorus 1.98mg/L, total hardness (CaCO)3Calculated) 380mg/L calcium hard (CaCO)3Meter) 313mg/L, alkalinity (CaCO)3Meter) 18 mM. The water amount is 500m3The output of the excess sludge of the biochemical unit is 75 kg/h.
As shown in FIG. 1, the treatment method for reducing the excess sludge comprises the following steps:
the sewage sequentially passes through a biochemical unit, a phosphorus removal unit and a reclaimed water reuse unit, wherein the reclaimed water reuse unit sequentially comprises a hardness removal unit, a rough filtration unit, an ion exchange unit and an ultrafiltration-reverse osmosis unit, and the biochemical unit is also sequentially connected with a sludge concentration tank and a sludge storage tank; and the sludge of the phosphorus removal unit and the sludge of the hardness removal unit are added to the upper part of a sludge concentration tank through the sludge lifting pump, are fully mixed with the rest sludge, and then enter a sludge storage tank through a gravity pipeline for conditioning treatment.
Wherein, the dephosphorization unit adopts ferric chloride and polyaluminium chloride as dephosphorization agents, the dosage of the ferric chloride, the polyaluminium chloride and the sludge discharged by the biochemical unit is respectively 100kg/d, 9.6kg/d and 12kg/d, and the total phosphorus in effluent is less than 0.5 mg/L; the hardness removing unit adopts sodium hydroxide and calcium hydroxide as softeners, and the adding amount is 2400kg/d and 1200kg/d respectively; polyaluminium chloride is used as a flocculating agent and anionic polyacrylamide is used as a coagulant aid, the dosage of the polyaluminium chloride, the dosage of the polyacrylamide and the dosage of sludge discharge of a biochemical unit are 240kg/d, 6kg/d and 28kg/d respectively, and the total hardness of effluent is less than 100 mg/L; the conditioner of the sludge storage tank adopts polyaluminium chloride, and the adding amount is 120 g/d.
Example 2
The embodiment discloses a treatment method for reducing excess sludge of petrochemical enterprises, and as shown in figure 2, sewage sequentially passes through a hardness removal unit, a biochemical unit and a phosphorus removal unit, and the biochemical unit is further sequentially connected with a sludge concentration tank and a sludge storage tank; and the sludge of the phosphorus removal unit and the sludge of the hardness removal unit are added to the upper part of a sludge concentration tank through the sludge lifting pump, are fully mixed with the rest sludge, and then enter a sludge storage tank through a gravity pipeline for conditioning treatment.
The wastewater amount is 150m3The water quality is as follows: COD586mg/L, total nitrogen 338mg/L, ammonia nitrogen 332mg/L, total phosphorus 3.3mg/L, total hardness (CaCO)3Calculated) 1090mg/L calcium hard (CaCO)3Calculated) 1079mg/L, alkalinity (CaCO)3Gauge) 20 mM. In order to ensure the stable operation of the biochemical unit, calcium ions in the wastewater need to be removed by the wastewater through a hardness removal unit, calcium hydroxide and sodium carbonate are adopted as softening agents in the hardness removal unit, and the adding amount is 5000kg/d and 4500kg/d respectively; the polyferric sulfate and the polyacrylamide are used as flocculating agents, the dosage of the polyferric sulfate, the polyacrylamide and the sludge discharge of the biochemical unit is 288kg/d, 3kg/d and 30kg/d respectively, and the hardness of effluent is controlled below 400 mg/L.
After the biochemical unit is processed, the effluent quality of the biochemical unit is as follows: COD 56mg/L, total nitrogen 38mg/L, ammonia nitrogen 2.2mg/L, total phosphorus 2.5mg/L, total hardness (CaCO)3Calculated) 255mg/L, calcium hard (CaCO)3Calculated) 251mg/L, alkalinity (CaCO)3Meter) 16mM, and the yield of the excess sludge is 27 kg/h. The effluent of the biochemical unit enters a phosphorus removal unit, the phosphorus removal unit adopts ferrous sulfate as a phosphorus removal agent, the dosage of the ferrous sulfate and the sludge discharged by the biochemical unit is respectively 35kg/d and 5kg/d, and the total phosphorus content of the effluent is below 0.5 mg/L.
The conditioner of the sludge storage tank adopts cationic polyacrylamide, and the adding amount is 3.5 g/d.
Comparative example 1
The comparative example discloses a conventional method for treating sewage of petrochemical enterprises, which comprises the following steps: sewage passes through biochemical unit, dephosphorization unit, reuse of reclaimed water unit in proper order, reuse of reclaimed water unit includes in proper order and removes hard unit, coarse filtration unit, ion exchange unit and ultrafiltration-reverse osmosis unit, and this process does not carry out the integration of each unit mud and handles to quality of water is up to standard as the purpose:
the effluent quality of the biochemical unit is as follows as in example 1: COD 48mg/L, total nitrogen 38mg/L, ammonia nitrogen 5.8mg/L, total phosphorus 1.98mg/L, total hardness (CaCO)3Calculated) 380mg/L calcium hard (CaCO)3Calculated) 313mg/L, alkalinity (CaCO)3Meter) 18 mM. The water amount is 500m3The output of the excess sludge of the biochemical unit is 75 kg/h. Biochemical unit sewageWater enters a dephosphorization unit, the dephosphorization unit adopts ferric chloride and polyaluminium chloride as dephosphorization agents, the dosage of the ferric chloride and the polyaluminium chloride is 240kg/d and 10kg/d respectively, and the total phosphorus content of effluent is about 0.5 mg/L; the hardness removing unit adopts sodium hydroxide and calcium hydroxide as softeners, and the adding amount is 2400kg/d and 1200kg/d respectively; polyaluminium chloride is used as a flocculating agent and anionic polyacrylamide is used as a coagulant aid, the adding amount of the polyaluminium chloride and the adding amount of the polyacrylamide are 240kg/d and 12kg/d respectively, and the total hardness of effluent is less than 100 mg/L; the conditioner of the sludge storage tank adopts polyaluminium chloride, and the adding amount is 150 g/d.
Comparative example 2
The comparative example discloses a conventional method for treating sewage of petrochemical enterprises, which comprises the following steps: the sewage sequentially passes through the hardness removal unit, the biochemical unit and the phosphorus removal unit, and the integrated treatment of sludge of each unit is not carried out in the process, so that the purpose of reaching the standard of water quality is achieved:
the amount of wastewater was 150m as in example 23The water quality is as follows: COD586mg/L, total nitrogen 338mg/L, ammonia nitrogen 332mg/L, total phosphorus 3.3mg/L, total hardness (CaCO)3Calculated) 1090mg/L calcium hard (CaCO)3Calculated) 1079mg/L, alkalinity (CaCO)3Meter) 20mM, and the yield of the excess sludge of the biochemical unit is 27 kg/h. The wastewater enters a hardness removal unit, calcium hydroxide and sodium carbonate are adopted as softeners in the hardness removal unit, and the adding amount is 5000kg/d and 4500kg/d respectively; polymeric ferric sulfate and polyacrylamide are used as flocculating agents, the dosage of the polymeric ferric sulfate and the dosage of the polyacrylamide are respectively 360kg/d and 3.6kg/d, and the hardness of effluent is controlled below 400 mg/L. The effluent quality of the biochemical unit is as follows: COD 56mg/L, total nitrogen 38mg/L, ammonia nitrogen 2.2mg/L, total phosphorus 2.5mg/L, total hardness (CaCO)3Calculated) 255mg/L, calcium hard (CaCO)3Calculated) 251mg/L, alkalinity (CaCO)3Meter) 16 mM. The effluent enters a dephosphorization unit, the dephosphorization unit adopts ferrous sulfate as a dephosphorization agent, the dosage of the ferrous sulfate is 80kg/d respectively, and the total phosphorus content of the effluent is 0.5-1 mg/L.
The conditioner of the sludge storage tank adopts cationic polyacrylamide, and the adding amount is 4.5 g/d.
Claims (10)
1. The method is characterized in that the excess sludge of a biochemical unit is added into a reaction zone of a phosphorus removal unit and a coagulation zone of a hardness removal unit, and the sludge of the phosphorus removal unit and the hardness removal unit is added into a sludge concentration tank of the biochemical unit to be mixed with other excess sludge in the sludge concentration tank, and then enters a sludge storage tank for conditioning treatment.
2. The treatment method according to claim 1, wherein the excess sludge in the biochemical unit is sludge discharged from a reaction tank of the biochemical unit or concentrated sludge with water content reduced to 98% -95% after concentration treatment.
3. The treatment method according to claim 1, characterized in that in the phosphorus removal unit, the amount of the excess sludge is 5-20%, preferably 10-20% by weight of the amount of the phosphorus removal agent.
4. A treatment method according to claim 1, characterized in that in the hardness removal unit the excess sludge is dosed in an amount of 5-30%, preferably 10-15% by weight of the coagulant dosing.
5. The treatment method of claim 1, wherein the dephosphorization unit and the de-hardening unit are both: reaction-coagulation-solid/liquid separation; the dephosphorization unit and the hardness removal unit can be one of a high-density clarification tank, a reaction tank-coagulation tank-sedimentation tank or a reaction tank-mechanical stirring clarification tank.
6. The treatment method according to claim 3, wherein the phosphorus removing agent of the phosphorus removing unit is selected from one of ferric chloride, ferrous chloride, alum, aluminum chloride, ferric sulfate, ferrous sulfate, polymeric ferric sulfate, polymeric aluminum chloride, or other composite iron salt and aluminum salt phosphorus removing agents.
7. The treatment method according to claim 4, wherein the coagulant of the hardness-removing unit is one of polyferric sulfate, polyaluminium chloride or other composite polyaluminium-ferric salts.
8. The treatment method as claimed in claim 1, wherein the total phosphorus concentration in the water from the phosphorus removal unit is not higher than 8mg/L and the pH value is 5-8.
9. The treatment method according to claim 5, wherein the agent used in the reaction zone of the hardness-removing unit is one or more selected from sodium hydroxide, sodium carbonate and calcium hydroxide.
10. The process of claim 9, wherein the agent used in the reaction zone of the hardness-removing unit is calcium hydroxide or calcium oxide.
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| JP2008238015A (en) * | 2007-03-27 | 2008-10-09 | Daiyanitorikkusu Kk | Dephosphorization method |
| CN101434445A (en) * | 2008-12-19 | 2009-05-20 | 天津大学 | Processing system and operation method for phosphor-containing organic wastewater |
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| JP2008238015A (en) * | 2007-03-27 | 2008-10-09 | Daiyanitorikkusu Kk | Dephosphorization method |
| CN101434445A (en) * | 2008-12-19 | 2009-05-20 | 天津大学 | Processing system and operation method for phosphor-containing organic wastewater |
| CN109867415A (en) * | 2019-03-27 | 2019-06-11 | 四川恒泰环境技术有限责任公司 | A kind of energy-saving semiconductor new material GaAs production wastewater treatment process |
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