CN110143727B - Treatment method of municipal sludge incineration process condensation wastewater - Google Patents
Treatment method of municipal sludge incineration process condensation wastewater Download PDFInfo
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- CN110143727B CN110143727B CN201910514747.1A CN201910514747A CN110143727B CN 110143727 B CN110143727 B CN 110143727B CN 201910514747 A CN201910514747 A CN 201910514747A CN 110143727 B CN110143727 B CN 110143727B
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- 238000000034 method Methods 0.000 title claims abstract description 77
- 239000002351 wastewater Substances 0.000 title claims abstract description 64
- 239000010802 sludge Substances 0.000 title claims abstract description 63
- 238000009833 condensation Methods 0.000 title claims abstract description 15
- 230000005494 condensation Effects 0.000 title claims abstract description 15
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 54
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000001914 filtration Methods 0.000 claims abstract description 30
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000000706 filtrate Substances 0.000 claims abstract description 17
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 13
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 13
- 238000004821 distillation Methods 0.000 claims abstract description 12
- 230000003647 oxidation Effects 0.000 claims abstract description 12
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 12
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 11
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims abstract description 11
- 238000001694 spray drying Methods 0.000 claims abstract description 10
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000002253 acid Substances 0.000 claims abstract description 7
- 239000003513 alkali Substances 0.000 claims abstract description 6
- 239000000203 mixture Substances 0.000 claims abstract description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 21
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 16
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 11
- 239000007864 aqueous solution Substances 0.000 claims description 10
- 239000008394 flocculating agent Substances 0.000 claims description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 5
- 239000000920 calcium hydroxide Substances 0.000 claims description 5
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 5
- 238000005189 flocculation Methods 0.000 claims description 5
- 230000016615 flocculation Effects 0.000 claims description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 5
- 230000014759 maintenance of location Effects 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 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 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 4
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 4
- 239000000347 magnesium hydroxide Substances 0.000 claims description 4
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 4
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 4
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- RQMIWLMVTCKXAQ-UHFFFAOYSA-N [AlH3].[C] Chemical compound [AlH3].[C] RQMIWLMVTCKXAQ-UHFFFAOYSA-N 0.000 claims description 3
- BPKGOZPBGXJDEP-UHFFFAOYSA-N [C].[Zn] Chemical compound [C].[Zn] BPKGOZPBGXJDEP-UHFFFAOYSA-N 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000007772 electrode material Substances 0.000 claims description 2
- 239000010881 fly ash Substances 0.000 claims description 2
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical group [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims description 2
- VMWYVTOHEQQZHQ-UHFFFAOYSA-N methylidynenickel Chemical compound [Ni]#[C] VMWYVTOHEQQZHQ-UHFFFAOYSA-N 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims description 2
- 239000003344 environmental pollutant Substances 0.000 abstract description 9
- 231100000719 pollutant Toxicity 0.000 abstract description 9
- 230000003311 flocculating effect Effects 0.000 abstract description 6
- 238000003756 stirring Methods 0.000 description 16
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 238000004065 wastewater treatment Methods 0.000 description 11
- 238000002485 combustion reaction Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 239000010865 sewage Substances 0.000 description 7
- 239000011790 ferrous sulphate Substances 0.000 description 6
- 235000003891 ferrous sulphate Nutrition 0.000 description 6
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000001035 drying Methods 0.000 description 4
- 230000001376 precipitating effect Effects 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 150000007524 organic acids Chemical class 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 241000700605 Viruses Species 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009264 composting Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 229910001448 ferrous ion Inorganic materials 0.000 description 1
- 230000004720 fertilization Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000003864 humus Substances 0.000 description 1
- 239000012535 impurity Substances 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
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 244000045947 parasite Species 0.000 description 1
- 230000003071 parasitic effect Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
-
- 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
- C02F1/66—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
- C02F1/725—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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F3/30—Aerobic and anaerobic processes
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)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a method for treating condensation wastewater of a municipal sludge incineration process, which comprises the following steps: adding acid into the municipal sludge incineration process condensed wastewater to adjust the pH value to 1-6, and adding FeSO4Performing Fenton oxidation treatment on the mixture and hydrogen peroxide; then filtering, adding alkali to adjust the pH value to 7-10, flocculating and filtering to obtain filtrate; carrying out reduced pressure distillation or vacuum spray drying on the filtrate, and then recovering heat through a heat exchanger to obtain condensate; the obtained condensate is treated by ozone or micro-electrolysis, biochemical treatment and active carbon, then the pH is adjusted to 6-9, and finally the condensate is discharged after reaching the standard after security filtration and reverse osmosis treatment. The method can reduce the CODcr of the condensed wastewater after municipal sludge incineration from hundreds of thousands to 100mg/L and below, the ammonia nitrogen from hundreds of thousands to 15mg/L and BOD5The chroma is reduced to 10 and below and other pollutants are reduced to trace amount from hundreds of thousands to 50mg/L and below.
Description
Technical Field
The invention relates to a method for treating condensation wastewater generated by a municipal sludge incineration process, in particular to a method for treating condensation wastewater generated by a municipal sludge incineration process, belonging to the technical field of wastewater treatment.
Background
A large amount of sludge is generated in the municipal sewage treatment process, wherein the sludge contains a large amount of organic matters, heavy metals, parasitic ova, bacteria, viruses and the like, and if the treatment, the disinfection and the sterilization are not carried out in time, the sludge causes secondary pollution to the environment.
At present, the following treatment technologies are available for municipal sludge:
1) the sanitary landfill disposal technology comprises the following steps: the sanitary landfill work of the sludge belongs to anaerobic landfill. Before the landfill work is started, the surface of the sewage sludge is in contact with the surrounding air of the drainage and exhaust pipes of the landfill area sufficiently, so that the operation mode of partial aerobic landfill is formed after the landfill. Although the sludge is treated in a sewage treatment plant in a series of processes, because the degradation of organic matters in the sludge is insufficient in the treatment process, the sludge still has a process of decomposing the organic matters when the landfill work is carried out, and the time required by the process is longer; therefore, the method has the problems of large occupied area and easy generation of odor.
2) The composting technology comprises the following steps: the utilization of the accumulated sludge in agriculture is one of the important embodiments of resource reuse. The sludge can be used by stacking alone or together with other municipal wastes. The method generally utilizes the environmental preference of bacteria to treat the sludge, creates a favorable environment for the bacteria, decomposes the organic matters which are not completely decomposed in the sludge, and then utilizes a high-temperature technology to kill some parasites. Organic matters, humus, nitrogen, phosphorus, potassium and the like in the sludge can improve the soil and are beneficial to the yield increase of crops; however, the method needs to be matched with the seasonality of farmland fertilization, and the normal operation of a sewage treatment plant is influenced by excessive accumulation of mud fertilizers.
3) The heat drying and burning treatment technology comprises the following steps: the sludge drying and incineration treatment can make the sludge beneficial and can reduce the accumulation of the sludge. The development of such techniques is very promising, since they have a very significant effect on the treatment of sludge. The drying and burning processes of the sludge supplement each other; the sludge is dried to make the water content less than 30 percent, and then is incinerated. The method does not need additional supplementary fuel in the normal production process, can ensure the furnace temperature to be 1000-1200 ℃ after heat recovery, can realize autonomous combustion of sludge, and is a development direction of municipal sludge treatment. However, the method can generate high-concentration waste water in the high-temperature combustion process, the CODcr of the waste water is even as high as 40 to over ten thousand mg/L, and the components are complex. The invention is proposed for the treatment of the above-mentioned waste water.
In the prior art, there are many methods for wastewater treatment, for example, chinese patent document CN106186275A discloses a triethylamine wastewater treatment method, which comprises the following steps: triethylamine wastewater is continuously pumped into a wastewater treatment tank; introducing a treating agent consisting of a ferrous sulfate solution and hydrogen peroxide residual liquid; adjusting the pH value of the sewage to be 3.5-4.0; according to the volume ratio of the treating agent to the triethylamine wastewater of 0.29: 1, carrying out sewage treatment reaction; the reaction time is controlled to be 6 hours, the oxidation digestion process is a continuous process, the waste water amount of triethylamine continuously enters a waste water treatment tank according to 6 hours, and a treating agent continuously enters until COD in the waste water is less than 7140. The invention utilizes the hydrogen peroxide residual liquid and the ferrous sulfate to treat the triethylamine sewage, so that the hydrogen peroxide residual liquid is changed into valuable, and the COD digestion rate can reach 80 percent; but the degradation of organic matters is still insufficient, the wastewater treatment is not thorough, the COD of the treated wastewater reaches 7140mg/L, and the index of municipal drainage requirements is far from being reached; and ferrous ions added in the treatment process are not removed, which is equivalent to secondary pollution.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a method for treating municipal sludge incineration process condensation wastewater. The wastewater treatment method can reduce the CODcr of the condensed wastewater after municipal sludge incineration from hundreds of thousands to 100mg/L or less, the ammonia nitrogen from hundreds of thousands to 15mg/L or less, and the BOD5The chroma is reduced to 10 or below from hundreds of thousands to 50mg/L, and other pollutants are reduced to trace amount; the effective treatment and standard discharge of the condensation waste water after municipal sludge incineration are realized.
Description of terms:
municipal sludge incineration process condensation waste water: a large amount of municipal sludge is generated in the municipal sewage treatment process, and high-concentration wastewater is generated in the incineration treatment process in the municipal sludge heat drying and incineration treatment process, wherein the wastewater is the municipal sludge incineration process condensation wastewater; the wastewater has complex components, CODcr is 3-40 ten thousand mg/L, BOD51-20 ten thousand mg/L, ammonia nitrogen 500-20000mg/L, and chroma 500-4000.
The technical scheme of the invention is as follows:
a method for treating municipal sludge incineration process condensation wastewater comprises the following steps:
(1) adding acid into the municipal sludge incineration process condensed wastewater to adjust the pH value to 1-6, and adding FeSO4Performing Fenton oxidation treatment on the mixture and hydrogen peroxide; then filtering, adding alkali to adjust the pH value to 7-10, flocculating and filtering to obtain filtrate;
(2) carrying out reduced pressure distillation or vacuum spray drying on the filtrate, and then recovering heat through a heat exchanger to obtain condensate; the obtained condensate is treated by ozone or micro-electrolysis, biochemical treatment and active carbon, then the pH is adjusted to 6-9, and finally the condensate is discharged after reaching the standard after security filtration and reverse osmosis treatment.
Preferably according to the invention, the acid in step (1) is an aqueous sulfuric acid solution, an aqueous hydrochloric acid solution or a spent acid solution; preferably, the mass concentration of the sulfuric acid aqueous solution or the hydrochloric acid aqueous solution is 2-6 mol/L.
According to the invention, the FeSO is preferably used in step (1)4The mass ratio of the hydrogen peroxide to the hydrogen peroxide is 0.1-1.5g/mL, and the mass concentration of the hydrogen peroxide is 25-35%; preferably, the FeSO in step (1)4The mass ratio of the hydrogen peroxide to the hydrogen peroxide is 0.2-0.5g/mL, and the mass concentration of the hydrogen peroxide is 28%.
According to the invention, preferably, the volume of the hydrogen peroxide in the step (1) is 0.5-7% of the volume of the municipal sludge incineration process condensed wastewater; preferably, the volume of the hydrogen peroxide is 0.5-2% of the volume of the municipal sludge incineration process condensed wastewater.
According to the present invention, it is preferable that the temperature of the Fenton oxidation treatment in the step (1) is 20 to 30 ℃ and the time is 20 to 40 minutes.
Preferably according to the invention, the base in step (1) is sodium hydroxide, potassium hydroxide, calcium hydroxide, magnesium hydroxide, sodium carbonate or sodium bicarbonate.
According to the invention, in step (1), after adding alkali to adjust the pH to 7-10, Fe (OH) is generated3Which itself may act as a flocculant to produce flocculation.
According to the invention, preferably, the flocculation in step (1) can be added with a flocculating agent, and the flocculating agent is polymeric ferric sulfate or polymeric aluminum chloride; the volume ratio of the mass of the flocculating agent to the condensed wastewater of the municipal sludge incineration process is 0.001-0.003 g/mL.
Preferably, the vacuum degree of the reduced pressure distillation or vacuum spray drying in the step (2) is (-0.05MPa) - (-0.1 MPa); the temperature of the reduced pressure distillation is 40-100 ℃, and the reduced pressure distillation is carried out until no condensate is generated. The reduced pressure distillation of the vacuum degree can boil the liquid at low temperature, thereby saving energy and reducing consumption. The purpose of the reduced pressure distillation or vacuum spray drying is to remove 90% or more of salt substances (including ammonium salts of organic acids) and the like by distilling off water and part of high-temperature non-condensable organic substances (i.e., high-temperature volatile organic substances).
According to the invention, the ozone treatment in step (2) can be carried out according to the prior art. Preferably, the ozone treatment in the step (2) is to perform ozone deep oxidation treatment on the condensate, wherein the ozone introducing amount is 5-35g/L (5-35 g is introduced into each liter of condensate), and the ozone deep oxidation treatment time is 5-15 h. The ozone introducing amount and the oxidation treatment time are controlled according to the content of pollutants in the condensate, and the ozone amount is generally 0.1-0.5mg/L when the CODcr is reduced by 100 mg/L. The ozone is generated by an ozone generator, and the generated ozone is preferably pumped into the condensate through a venturi ejector to be intensively mixed.
According to the invention, the microelectrolytic treatment in step (2) can be carried out as known in the art. Preferably, the voltage of the micro-electrolysis treatment in the step (2) is controlled to be 2-8v, and the residence time of the condensate is 2-6 hours; the electrode material is carbon-iron, carbon-aluminum, carbon-zinc or carbon-nickel. And a step of filtering is also needed after the micro-electrolysis treatment. The micro-electrolysis treatment time is determined according to the content of the pollutants in the condensate. In general, the electricity consumption is required to be 0.01-0.05 degree when the CODcr is reduced by 100 mg/L.
Preferably, according to the present invention, the biochemical treatment in step (2) is an anaerobic-aerobic treatment or an anaerobic-anoxic-aerobic treatment. The anaerobic-aerobic treatment or anaerobic-anoxic-aerobic treatment is carried out according to the prior art. Preferably, the anaerobic treatment is to introduce the condensate into an anaerobic pool for treatment, the retention time of the condensate is 72 hours, and the CODcr is reduced by 100 mg/L; the aerobic treatment is to introduce the condensate into an aerobic pool for treatment, wherein the residence time of the condensate is 140 and 170 hours; the anoxic treatment is to introduce the condensate into an anoxic tank for treatment, wherein the residence time of the condensate is 72 hours.
According to the invention, the activated carbon treatment in the step (2) is preferably carried out by adding activated carbon into the condensate after biochemical treatment, and treating at the temperature of 0-50 ℃ for 10-30 minutes; the active carbon can be powdered active carbon, granular active carbon, columnar active carbon or fly ash; the adding amount of the active carbon is 10-30kg per ton of the condensate after biochemical treatment. The condensate is treated by activated carbon, and the pollutants are adsorbed.
According to the invention, the reagent used for adjusting the pH in step (2) is preferably sodium hydroxide, potassium hydroxide, calcium hydroxide, magnesium hydroxide, sodium carbonate or sodium bicarbonate.
According to the invention, preferably, the security filtration in the step (2) is to filter out solid particles with the particle size of 0.05 micron or more.
According to the invention, the reverse osmosis treatment in step (2) can be carried out according to the prior art. Preferably, the pressure of the reverse osmosis treatment in the step (2) is 0.1-10 MPa.
The invention has the following technical characteristics and beneficial effects:
1. the invention adds FeSO into the municipal sludge incineration process condensed wastewater4The wastewater is subjected to Fenton oxidation treatment with hydrogen peroxide, so that COD, BOD, ammonia nitrogen and the like in the wastewater can be greatly reduced; removing most of the precipitate by filtration, and adjusting pH to 7-10 by adding alkali, wherein Fe in the wastewater is3+Formation of Fe (OH)3The flocculant is used as a flocculant or a flocculant can be additionally added for flocculation, and then the flocculate is removed by filtration to obtain filtrate; the obtained filtrate is subjected to reduced pressure distillation or vacuum spray drying to remove more than 90% of salt substances (including ammonium salt of organic acid) and the like, heat is recovered through a heat exchanger, and the evaporated water and part of high-temperature non-condensable organic substances (namely high-temperature volatile organic substances) are collected to obtain condensate. The obtained condensate can change most organic matters into organic acid, even carbon dioxide and water through ozone or micro-electrolysis treatment and biochemical treatment; then, organic matters and inorganic matters in the wastewater are further adsorbed through activated carbon treatment, and decolorization is realized; after the pH value is adjusted, suspended matters or fine impurity particles are removed through security filtration, and then 99.9% of organic matters with molecular weight more than 100 can be removed through reverse osmosis, so that the standard discharge of the wastewater is finally realized.
2. The wastewater treatment method is designed aiming at specific wastewater, namely municipal sludge incineration process condensed wastewater, and all the steps are indispensable and are based on the previous step, otherwise, the steps are difficult to realize; the wastewater treatment method can reduce the CODcr of the condensed wastewater after municipal sludge incineration from hundreds of thousands to 100mg/L or less, the ammonia nitrogen from hundreds of thousands to 15mg/L or less, and the BOD5The chroma is reduced to 10 or below from hundreds of thousands to 50mg/L, and other pollutants are reduced to trace amount; the effective treatment and standard discharge of the condensation waste water after municipal sludge incineration are realized.
Detailed Description
The present invention is further illustrated by, but not limited to, the following examples.
Meanwhile, the experimental methods described in the following examples are all conventional methods unless otherwise specified; the reagents and equipment are commercially available, unless otherwise specified.
Example 1
The municipal sludge incineration process condensed wastewater comprises the following components: CODcr of 51200mg/L, BOD513000mg/L, NH3-N (ammonia nitrogen) 6000mg/L, conductivity 46300 mus/cm, color of 500, pH 8.75.
The treatment method of the municipal sludge incineration process condensed wastewater comprises the following steps:
taking 1000ml of the wastewater, and adjusting the pH value to 3.5-4 by using 6mol/L sulfuric acid aqueous solution; adding 3.0g of ferrous sulfate, and stirring for dissolving; adding 10ml of 28 wt% hydrogen peroxide, stirring for 10 minutes at 25 ℃, standing for 10 minutes, and then filtering to obtain black liquid. Adding sodium hydroxide to adjust the pH value to 8-9, adding 2g of flocculating agent polymeric ferric sulfate, quickly stirring and dispersing for 40 seconds, slowly stirring and flocculating for 20 seconds, precipitating for 5 minutes, and filtering to obtain filtrate. Distilling the filtrate at low pressure (low pressure-0.075 Mpa, temperature 58 deg.C), and recovering heat via heat exchanger to obtain condensate until no condensate is generated; ozone is pumped into the condensate through a Venturi ejector to be strongly mixed for 10h (the ozone introduction amount is 10g/L, namely 10g of ozone is introduced into each liter of condensate), and then the condensate after biochemical treatment is obtained through anaerobic-aerobic treatment (the anaerobic treatment is carried out in an anaerobic tank, the residence time of the condensate is 72 hours, and the CODcr is reduced by 100 mg/L; the aerobic treatment is carried out in an aerobic tank, and the residence time of the condensate is 144 hours); then adding powdered activated carbon (the adding amount of the activated carbon is 20 kg/ton of the condensate subjected to biochemical treatment), and treating for 20 minutes at 25 ℃; then Ca (OH) is added2Adjusting pH to 7-8, filtering to remove solid particles with particle size of 0.05 μm or more by security filtration; and then carrying out reverse osmosis treatment under the pressure of 5MPa, wherein the outlet water is qualified discharge water reaching the standard, and spray drying or sending the concentrated solution obtained by the reverse osmosis treatment to a combustion furnace for combustion treatment.
After the treatment by the method of the embodiment, the water quality condition of the up-to-standard discharged water is as follows: CODcr of 90mg/L, BOD550mg/L, 15mg/L NH3-N, 99.8 mu s/cm conductivity, 10 chroma, 7.5 pH and trace amount of other pollutants; the above data demonstrate that the wastewater treatment process of the present invention achieves effective treatment and standard discharge of wastewater.
Example 2
The municipal sludge incineration process condensed wastewater comprises the following components: CODcr of 52000mg/L, BOD513500mg/L, NH 3-N5000 mg/L, conductivity 46600. mu.s/cm, color 550, pH 9.15.
The treatment method of the municipal sludge incineration process condensed wastewater comprises the following steps:
taking 1000ml of the wastewater, and adjusting the pH value to 3.5-4 by using a 4mol/L sulfuric acid aqueous solution; adding 4.0g of ferrous sulfate, and stirring for dissolving; adding 15ml of 28 percent hydrogen peroxide, stirring for 15 minutes at the temperature of 20 ℃, standing for 15 minutes, and then filtering to obtain black liquid. Adding calcium hydroxide to adjust pH to 8-9, adding flocculant polyaluminium chloride 1g, rapidly stirring and dispersing for 30 s, slowly stirring and flocculating for 30 s, precipitating for 10 min, and filtering to obtain filtrate. Distilling the filtrate under low pressure (low pressure-0.055 Mpa, temperature 82 deg.C), and recovering heat via heat exchanger to obtain condensate until no condensate is generated; ozone is pumped into condensate through a Venturi ejector to be strongly mixed for 12h (the ozone introduction amount is 10g/L), and then the condensate after biochemical treatment is obtained through anaerobic-anoxic-aerobic treatment (the anaerobic treatment is carried out in an anaerobic tank, the residence time of the condensate is 72h, and the CODcr is reduced by 100 mg/L; the aerobic treatment is carried out in an aerobic tank, the residence time of the condensate is 144 h; the anoxic treatment is carried out in an anoxic tank, and the residence time of the condensate is 72 h); then adding granular activated carbon (the adding amount of the activated carbon is 30 kg/ton of the condensate subjected to biochemical treatment), and treating for 30 minutes at 20 ℃; then Ca (OH) is added2Adjusting pH to 7-8, filtering to remove solid particles with particle size of 0.05 μm or more by security filtration; and then carrying out reverse osmosis treatment under 10MPa, wherein the effluent is qualified discharge water reaching the standard, and the concentrated solution obtained by the reverse osmosis treatment is subjected to spray drying or is sent to a combustion furnace for combustion treatment.
After the treatment by the method of the embodiment, the water quality condition of the up-to-standard discharged water is as follows: CODcr of 100mg/L, BOD5Is 60mg/L, NH3the-N is 15mg/L, the conductivity is 108 mu s/cm, the chroma is 10, the pH is 7.2, and other pollutants are reduced to trace amount.
Example 3
The municipal sludge incineration process condensed wastewater comprises the following components: CODcr of 101200mg/L, BOD5130000mg/L, NH3-N (ammonia nitrogen) 15000mg/L, conductivity 87300 mus/cm, color 1000, pH 9.30.
The treatment method of the municipal sludge incineration process condensed wastewater comprises the following steps:
taking 1000ml of the wastewater, and adjusting the pH value to 3.5-4 by using 2mol/L sulfuric acid aqueous solution; adding 10.0g of ferrous sulfate, and stirring for dissolving; adding 20ml of 28 wt% hydrogen peroxide, stirring for 20 minutes at 30 ℃, standing for 20 minutes, and then filtering to obtain black liquid. Adding sodium hydroxide to adjust pH to 8-9, adding flocculant polyaluminium chloride 2g, rapidly stirring and dispersing for 40 s, slowly stirring and flocculating for 20 s, precipitating for 5 min, and filtering to obtain filtrate. Distilling the filtrate under low pressure (low pressure-0.1 Mpa, temperature 48 deg.C), and recovering heat via heat exchanger to obtain condensate until no condensate is generated; introducing the condensate into a micro-electrolysis cell, adding a carbon-aluminum electrode, controlling the voltage to be 4-6v, and controlling the residence time of the condensate to be 4h, and carrying out micro-electrolysis treatment; then filtering, and carrying out anaerobic-aerobic treatment on the filtrate (wherein the anaerobic treatment is carried out in an anaerobic pool, the retention time of the condensate is 72 hours, and the CODcr is reduced by 100 mg/L; the aerobic treatment is carried out in an aerobic pool, and the retention time of the condensate is 168 hours) to obtain the condensate after biochemical treatment; then adding columnar activated carbon (the adding amount of the activated carbon is 30 kg/ton of the condensate subjected to biochemical treatment), and treating for 30 minutes at 35 ℃; then Ca (OH) is added2Adjusting pH to 7-8, filtering to remove solid particles with particle size of 0.05 μm or more by security filtration; and then carrying out reverse osmosis treatment under 10MPa, wherein the effluent is qualified discharge water reaching the standard, and the concentrated solution obtained by the reverse osmosis treatment is subjected to spray drying or is sent to a combustion furnace for combustion treatment.
After the treatment by the method of the embodiment, the water quality condition of the up-to-standard discharged water is as follows:CODcr of 95mg/L, BOD555mg/L, 15mg/L NH3-N, 103 mu s/cm conductivity, 10 chroma, 7.8 pH, and trace amount of other pollutants; the above data demonstrate that the wastewater treatment process of the present invention achieves effective treatment and standard discharge of wastewater.
Comparative example 1
The composition of the municipal sludge incineration process condensed wastewater is as in example 1;
taking 1000ml of the wastewater, and adjusting the pH value to 3.5-4 by using 6mol/L sulfuric acid aqueous solution; adding 3.0g of ferrous sulfate, and stirring for dissolving; adding 10ml of 28 wt% hydrogen peroxide, stirring for 10 minutes at 25 ℃, standing for 10 minutes, and then filtering to obtain black liquid. Adding sodium hydroxide to adjust the pH value to 8-9, adding 2g of flocculating agent polymeric ferric sulfate, quickly stirring and dispersing for 40 seconds, slowly stirring and flocculating for 20 seconds, precipitating for 5 minutes, and filtering to obtain filtrate. Distilling the filtrate at low pressure (low pressure-0.075 Mpa, temperature 58 deg.C), and recovering heat via heat exchanger to obtain condensate until no condensate is generated; the composition of the resulting condensate was as follows: CODcr of 9800mg/L, ammonia nitrogen of 4000mg/L and BOD54500mg/L, conductivity 5400 μ s/cm, chroma of 50, and pH 9; if the ozone treatment is not carried out, the subsequent biochemical treatment cannot be carried out at all because the content of the organic component is too high. Therefore, the ozone treatment step is indispensable in the method of the present invention.
Claims (7)
1. A method for treating municipal sludge incineration process condensation wastewater comprises the following steps:
(1) adding acid into the municipal sludge incineration process condensed wastewater to adjust the pH value to 1-6, and adding FeSO4Performing Fenton oxidation treatment on the mixture and hydrogen peroxide; then filtering, adding alkali to adjust the pH value to 7-10, wherein the Fe in the wastewater is3+Formation of Fe (OH)3The flocculant is used as a flocculating agent, and a filtrate is obtained by flocculation and filtration; the FeSO4The mass ratio of the hydrogen peroxide to the hydrogen peroxide is 0.1-1.5g/mL, and the mass concentration of the hydrogen peroxide is 25-35%;
the temperature of the Fenton oxidation treatment is 20-30 ℃, and the time is 20-40 minutes; in the municipal sludge incineration process condensed wastewater, CODcr is 51200-40 ten thousand mg/L and BOD513000-20 ten thousand mg/L, ammonia nitrogen 5000-20000mg/L, the chroma is 500-;
(2) carrying out reduced pressure distillation or vacuum spray drying on the filtrate, and then recovering heat through a heat exchanger to obtain condensate; treating the obtained condensate with ozone or micro-electrolysis, performing biochemical treatment and active carbon treatment, adjusting pH to 6-9, and performing security filtration and reverse osmosis treatment to reach discharge standard;
the ozone treatment is to carry out ozone deep oxidation treatment on the condensate, wherein the ozone introduction amount is 5-35g/L, and the ozone deep oxidation treatment time is 5-15 h; the voltage of the micro-electrolysis treatment is controlled to be 2-8v, and the retention time of the condensate is 2-6 hours; the electrode material adopted by the micro-electrolysis treatment is carbon-iron, carbon-aluminum, carbon-zinc or carbon-nickel; the biochemical treatment is anaerobic-aerobic treatment; the anaerobic treatment is to introduce the condensate into an anaerobic tank for treatment, the retention time of the condensate is 72 hours, and the CODcr is reduced by 100 mg/L; the aerobic treatment is to introduce the condensate into an aerobic pool for treatment, wherein the residence time of the condensate is 140 and 170 hours; the activated carbon treatment is to add activated carbon into the condensate and treat the mixture for 10 to 30 minutes at the temperature of between 0 and 50 ℃; the active carbon is powdered active carbon, granular active carbon, columnar active carbon or fly ash; the adding amount of the active carbon is 10-30kg per ton of the condensate after biochemical treatment; the security filtration is to filter out solid particles with the particle size of more than or equal to 0.05 micron; the pressure of the reverse osmosis treatment is 0.1-10 MPa.
2. The method for treating the municipal sludge incineration process condensed wastewater according to claim 1, wherein the step (1) comprises one or more of the following conditions:
a. the acid is sulfuric acid aqueous solution, hydrochloric acid aqueous solution or waste acid solution;
b. the volume of the hydrogen peroxide is 0.5-7% of the volume of the municipal sludge incineration process condensed wastewater.
3. The method for treating the municipal sludge incineration process condensed wastewater according to claim 2, wherein the step (1) comprises one or more of the following conditions:
a. the mass concentration of the sulfuric acid aqueous solution or the hydrochloric acid aqueous solution is 2-6 mol/L;
b. the FeSO4The mass ratio of the hydrogen peroxide to the hydrogen peroxide is 0.2-0.5g/mL, and the mass concentration of the hydrogen peroxide is 28%;
c. the volume of the hydrogen peroxide is 0.5-2% of the volume of the municipal sludge incineration process condensed wastewater.
4. The method for treating the municipal sludge incineration process condensation wastewater according to claim 1, wherein the alkali in step (1) is sodium hydroxide, potassium hydroxide, calcium hydroxide, magnesium hydroxide, sodium carbonate or sodium bicarbonate.
5. The method for treating the municipal sludge incineration process condensation wastewater according to claim 1, wherein a flocculating agent is added in the flocculation in the step (1), and the flocculating agent is polymeric ferric sulfate or polymeric aluminum chloride; the volume ratio of the mass of the flocculating agent to the condensed wastewater of the municipal sludge incineration process is 0.001-0.003 g/mL.
6. The method for treating the condensed wastewater of the municipal sludge incineration process according to claim 1, wherein the vacuum degree of the reduced pressure distillation or the vacuum spray drying in the step (2) is (-0.05MPa) - (-0.1 MPa); the temperature of the reduced pressure distillation is 40-100 ℃, and the reduced pressure distillation is carried out until no condensate is generated.
7. The method for treating the municipal sludge incineration process condensation wastewater according to claim 1, wherein the agent for adjusting the pH in the step (2) is sodium hydroxide, potassium hydroxide, calcium hydroxide, magnesium hydroxide, sodium carbonate or sodium bicarbonate.
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