CN115925186B - A treatment process for barium slag leachate - Google Patents
A treatment process for barium slag leachate Download PDFInfo
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- CN115925186B CN115925186B CN202310005532.3A CN202310005532A CN115925186B CN 115925186 B CN115925186 B CN 115925186B CN 202310005532 A CN202310005532 A CN 202310005532A CN 115925186 B CN115925186 B CN 115925186B
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- leachate
- sulfate
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- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 239000002893 slag Substances 0.000 title claims abstract description 66
- 229910052788 barium Inorganic materials 0.000 title claims abstract description 64
- 238000000034 method Methods 0.000 title claims abstract description 64
- 239000010802 sludge Substances 0.000 claims abstract description 87
- 238000004062 sedimentation Methods 0.000 claims abstract description 76
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 64
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 62
- 230000003647 oxidation Effects 0.000 claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- 238000005189 flocculation Methods 0.000 claims abstract description 40
- 230000016615 flocculation Effects 0.000 claims abstract description 40
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 38
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000000126 substance Substances 0.000 claims abstract description 29
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 26
- 239000011593 sulfur Substances 0.000 claims abstract description 26
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000002351 wastewater Substances 0.000 claims abstract description 21
- 229910001422 barium ion Inorganic materials 0.000 claims abstract description 19
- 239000002957 persistent organic pollutant Substances 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 230000001105 regulatory effect Effects 0.000 claims abstract description 14
- 238000003860 storage Methods 0.000 claims abstract description 14
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 13
- 231100000719 pollutant Toxicity 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 230000001590 oxidative effect Effects 0.000 claims abstract description 12
- 230000003311 flocculating effect Effects 0.000 claims abstract description 6
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 47
- 238000003756 stirring Methods 0.000 claims description 47
- 229920002401 polyacrylamide Polymers 0.000 claims description 37
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 28
- 239000003638 chemical reducing agent Substances 0.000 claims description 26
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 24
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 24
- 239000010865 sewage Substances 0.000 claims description 23
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 claims description 22
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Inorganic materials [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 claims description 21
- 230000003750 conditioning effect Effects 0.000 claims description 20
- 239000011790 ferrous sulphate Substances 0.000 claims description 19
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 19
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 19
- 239000003513 alkali Substances 0.000 claims description 13
- 238000001556 precipitation Methods 0.000 claims description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 238000006477 desulfuration reaction Methods 0.000 claims description 8
- 230000023556 desulfurization Effects 0.000 claims description 8
- 230000001143 conditioned effect Effects 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052698 phosphorus Inorganic materials 0.000 claims description 6
- 239000011574 phosphorus Substances 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 6
- 238000005262 decarbonization Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 claims description 4
- 238000011001 backwashing Methods 0.000 claims description 4
- 238000009388 chemical precipitation Methods 0.000 claims description 4
- 239000000701 coagulant Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 230000001376 precipitating effect Effects 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims description 3
- 229960004887 ferric hydroxide Drugs 0.000 claims description 3
- IEECXTSVVFWGSE-UHFFFAOYSA-M iron(3+);oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Fe+3] IEECXTSVVFWGSE-UHFFFAOYSA-M 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 238000004140 cleaning Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 239000013589 supplement Substances 0.000 claims description 2
- 238000000265 homogenisation Methods 0.000 claims 2
- CUPCBVUMRUSXIU-UHFFFAOYSA-N [Fe].OOO Chemical compound [Fe].OOO CUPCBVUMRUSXIU-UHFFFAOYSA-N 0.000 claims 1
- 239000003153 chemical reaction reagent Substances 0.000 claims 1
- 230000001112 coagulating effect Effects 0.000 claims 1
- 229910021519 iron(III) oxide-hydroxide Inorganic materials 0.000 claims 1
- 238000012806 monitoring device Methods 0.000 claims 1
- 230000008719 thickening Effects 0.000 claims 1
- 239000003403 water pollutant Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000013049 sediment Substances 0.000 description 11
- 239000003814 drug Substances 0.000 description 8
- 239000000149 chemical water pollutant Substances 0.000 description 6
- 238000003475 lamination Methods 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- 229940037003 alum Drugs 0.000 description 4
- 238000005261 decarburization Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000007800 oxidant agent Substances 0.000 description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229910001448 ferrous ion Inorganic materials 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 230000001360 synchronised effect Effects 0.000 description 3
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 2
- 159000000009 barium salts Chemical class 0.000 description 2
- 230000003851 biochemical process Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000593 degrading effect Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 150000004763 sulfides Chemical class 0.000 description 2
- 150000003463 sulfur Chemical class 0.000 description 2
- -1 sulfur ion Chemical class 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- CJDPJFRMHVXWPT-UHFFFAOYSA-N barium sulfide Chemical compound [S-2].[Ba+2] CJDPJFRMHVXWPT-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 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
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 229910001447 ferric ion Inorganic materials 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000011272 standard treatment Methods 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention relates to a treatment process of barium slag percolate, which comprises a percolate collecting and regulating tank, a chemical pre-sedimentation tank, an oxidation flocculation reaction tank, a first sedimentation tank, a deep oxidation tank, a second sedimentation tank, a laminated filter and a clear water temporary storage tank, wherein the percolate collecting and regulating tank is sequentially arranged and sequentially used for treating percolate, the chemical pre-sedimentation tank is used for synchronously removing sulfur and barium, the oxidation flocculation reaction tank is used for oxidizing sulfide into elemental sulfur and flocculating and settling, the first sedimentation tank is used for solid-liquid separation, the deep oxidation tank is used for deep oxidation removal of organic pollutants and ammonia nitrogen, the second sedimentation tank is used for solid-liquid separation, the laminated filter and the clear water temporary storage tank are used for treating suspended matters in percolate wastewater, and the sludge treatment system is used for treating sludge separated by each sedimentation tank. The method has reasonable sequential connection among the process sections, has the advantages of high efficiency, low energy consumption and easy operation and management, can realize the effective combined removal of pollutants such as sulfide, barium ions, CODcr, ammonia nitrogen, TP and SS in the barium slag leachate, and ensures that the yielding water meets the direct emission standard requirement in the water pollutant emission limit in the emission standard of inorganic chemical industry pollutants.
Description
Technical Field
The invention belongs to the field of slag field leachate treatment, and particularly relates to a treatment process of slag field leachate, wherein various pollution indexes of the treatment process can reach direct discharge standards.
Background
In the national hazardous waste directory, barium slag generated by the barium salt industry belongs to hazardous solid waste, waste category HW47 and waste codes 261-088-47, a large amount of barium slag is temporarily accumulated in a slag yard, and a large amount of soluble barium salt such as barium sulfide is dissolved out through rainwater leaching, so that percolate wastewater containing a large amount of barium ions and sulfide is generated, and the percolate wastewater can cause a certain degree of pollution threat to the surface water environment and the groundwater environment if the percolate wastewater is not effectively collected and treated.
The barium slag leachate has complex components, and main pollutants are usually barium ions and sulfides with higher concentration, and are accompanied by certain concentration of CODcr and ammonia nitrogen. The treatment method for the percolate wastewater mainly comprises a flocculation precipitation method, an adsorption method, an advanced oxidation method, a membrane filtration method and a biochemical method, however, the barium slag percolate contains more pollutant species, the treatment is carried out by adopting the above process singly, a plurality of pollutant species in the barium slag percolate cannot be treated at the same time, the treatment effect is poor, and the input cost is high.
The prior art for treating the leachate wastewater usually adopts a mode of pretreatment, biochemistry and advanced treatment, wherein the pretreatment process is required to have higher sulfur removal capability, because the barium residue leachate wastewater contains higher sulfide and total salt, which exceeds the concentration which can be born by biological treatment, and the biochemical process needs to put more labor cost and larger occupied area, and in addition, for the related direct discharge standard, the discharge indexes of the total barium and sulfide are higher, and the standard treatment cannot be finished by simple physicochemical pretreatment or advanced treatment.
Regarding the treatment of slag percolate, there are also many patent documents reporting that, for example, CN114684950a discloses an integrated treatment device and method for slag field percolate, and proposes a method for treating slag field percolate by single-stage synchronous oxidation and chemical precipitation, firstly, adding alkaline oxidant and ferrous sulfate into slag field percolate at the same time, pretreating the slag field percolate under normal temperature condition to obtain pretreatment liquid, then adding flocculant into the pretreatment liquid to obtain mixed liquid, and finally precipitating the mixed liquid to obtain sludge and treated water on the upper layer of the sludge, wherein the treatment device is shown in fig. 1; the device and the process aim at solving the problems that the steps are complicated when the traditional chemical oxidation method is used for treating the slag field leachate, so that the synchronous oxidation and chemical precipitation mode is adopted to fulfill the aims of synchronous decarburization, nitrogen removal, sulfur removal, barium removal and the like, but the method has a great defect in the practical application of treating the barium slag field leachate, and is characterized in that the method is only provided with a single-stage reactor, all dosing steps of an oxidant, ferrous sulfate, a coagulant and the like are simultaneously carried out, so that ferrous ions are firstly oxidized into ferric ions by the oxidant rapidly, the sulfur ion removing capability is greatly reduced, a great amount of oxidant is consumed, the method can not achieve good effects of decarburization, nitrogen removal, sulfur removal and barium removal in the practical treatment process of the barium slag field leachate, the medicament cost is increased, and further, the requirement on the direct discharge standard in the water pollutant discharge standard in the inorganic chemical industry pollutant discharge standard (GB 31573-2015) is a great difference and a short plate.
CN112551756a discloses a method and a system for removing sulfide in landfill leachate, which propose a pretreatment process scheme for the landfill leachate containing sulfur, the landfill leachate is mixed with a desulfurizing agent and then enters a desulfurization reaction tower for reaction, sulfide in the landfill leachate is converted into insoluble sulfur salt precipitate, meanwhile, flocculant is added into the desulfurization reaction tower to accelerate flocculation of the sulfur salt precipitate, the mixture is stirred and mixed uniformly by a stirring device, overflow enters a sedimentation tank for sedimentation separation, desulfurization clear liquid can be subjected to subsequent treatment after sedimentation separation, bottom sediment sludge enters a mud-water separation device for treatment through sludge discharge, finally, the desulfurization purpose is achieved, and a treatment system is shown in fig. 2, however, a complete scheme is not provided for meeting the standard of all pollutant indexes of the landfill leachate, sulfide pretreatment is designed for meeting the requirement of biochemical treatment, so that the proposal of the technology still needs to be combined treatment by matching a biochemical technology, the treatment requirement of the leachate of an actual barium slag field, the biochemical technology means that more manpower is required for operation and maintenance is required, and the investment of labor cost is increased.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a treatment process of barium slag percolate. The invention has small occupied area, high efficiency and easy operation and management, and can effectively remove pollutants such as sulfide, barium ions, CODcr, ammonia nitrogen, total phosphorus, SS and the like in the percolate.
In order to achieve the above object, the present invention provides the following technical solutions:
the treatment process of the barium slag percolate comprises a percolate collecting and regulating tank, a chemical pre-sedimentation tank, an oxidation flocculation reaction tank, a first sedimentation tank, a deep oxidation tank, a second sedimentation tank, a laminated filter and a clear water temporary storage tank, wherein the percolate collecting and regulating tank is sequentially arranged and sequentially used for treating percolate, the chemical pre-sedimentation tank is used for synchronously removing sulfur and barium, the oxidation flocculation reaction tank is used for oxidizing sulfide into elemental sulfur and flocculating and settling, the first sedimentation tank is used for solid-liquid separation, the deep oxidation tank is used for deep oxidation removal of organic pollutants and ammonia nitrogen, the second sedimentation tank is used for solid-liquid separation, the laminated filter and the clear water temporary storage tank are used for treating suspended solids in percolate wastewater, and the sludge treatment system is used for treating sludge separated by each sedimentation tank.
According to the invention, preferably, the percolate collecting tank collects barium slag percolate wastewater with certain residence time, wherein stirring equipment is arranged for stirring and mixing the wastewater in the tank to achieve the purpose of homogenizing the average amount, and then the wastewater in the tank is lifted to a chemical pre-sedimentation tank by a lifting water pump, and further preferably, a QJB type submersible stirrer is used as the stirring equipment.
According to the invention, preferably, the chemical pre-sedimentation tank for synchronously removing sulfur and barium comprises a sulfur and barium removing area capable of adding ferrous sulfate to fully mix and react with sulfide and barium ions in percolate, a flocculation area capable of adding polyaluminum sulfate to play a coagulation promoting role and supplement the effect of removing barium ions, and a sedimentation area for solid-liquid separation, wherein sludge separated by the sedimentation area is discharged into a sludge treatment system;
Further preferably, the ratio of the adding amount of the ferrous sulfate to the mass content of the vulcanized material is 5-7.5:1, the ferrous sulfate medicament is calculated by ferrous sulfate heptahydrate, and the adding amount of the polyaluminium sulfate is 0.1-2 mg/L;
Most preferably, the chemical pre-sedimentation tank comprises a chemical reaction area and a sedimentation area, wherein the chemical reaction area is divided into two grids, ferrous sulfate is added into the first grid, polymeric flocculant polyaluminum sulfate is added into the second grid, stirring equipment is respectively arranged between the two grids and used for mixing and stirring medicaments and wastewater, sulfide, barium ions and sulfate radicals react to respectively form ferrous sulfide and barium sulfate sediment, simultaneously tiny sediment substances form larger flocs under the action of the polyaluminum sulfate and sediment in the sedimentation area, and a mud level meter is arranged in the sedimentation area and used for controlling automatic mud discharge. Preferably, the stirring equipment arranged in the first lattice reaction zone is a vertical blade stirrer, the matched speed reducer is a helical gear speed reducer, the stirring equipment arranged in the second lattice reaction zone is a vertical frame stirrer, and the matched speed reducer is a helical gear speed reducer.
According to the invention, preferably, the concentration of sulfide in the barium slag percolate is 20-1000 mg/L, the concentration of barium ions is 20-1000 mg/L, CODcr, the concentration of ammonia nitrogen is 10-200 mg/L, the concentration of total phosphorus is 0.1-200 mg/L, SS, and the concentration is 50-1000 mg/L.
According to the invention, preferably, the oxidation and flocculation reaction tank for oxidizing sulfide into elemental sulfur and flocculating and precipitating comprises a decarbonization and sulfur removal reaction zone and a flocculation reaction zone, wherein the decarbonization and sulfur removal reaction zone is divided into two compartments, hydrogen peroxide is added to fully mix and oxidize sulfide and organic pollutants in percolate, alkali liquor and polyacrylamide are added to the flocculation reaction zone to adjust the pH value, and the elemental sulfur and a small amount of ferric hydroxide generated in the front zone are subjected to flocculation reaction;
Further preferably, the ratio of the adding amount of the hydrogen peroxide to the mass content of the organic pollutants is 0.3-4:1, the alkali liquor is sodium hydroxide solution, the pH value is regulated to 8-11, the adding amount of the polyacrylamide is 0.001-0.01 mg/L, and the hydrogen peroxide is hydrogen peroxide solution with the mass concentration of 10-30%.
Most preferably, the oxidation flocculation reaction tank is divided into three grids, stirring devices are respectively arranged, hydrogen peroxide is added into the first grid and the second grid, sulfides in the sewage are oxidized into elemental sulfur by the hydrogen peroxide, alkali liquor and polyacrylamide are added into the third grid, formed fine flocs form larger flocs under the action of the polyacrylamide, the adding amount of the hydrogen peroxide and the alkali liquor is controlled by an online ORP meter and a pH meter, preferably, the stirring devices arranged in the first grid and the second grid are vertical blade stirrers, a matched speed reducer is a helical gear speed reducer, the stirring devices arranged in the third grid are vertical frame stirrers, and the matched speed reducer is a helical gear speed reducer.
According to the invention, preferably, the first sedimentation tank is an upflow inclined plate sedimentation tank, and is used for settling floc alum flocs generated in the oxidation flocculation sedimentation tank.
According to the invention, preferably, the deep oxidation pond for removing organic pollutants and ammonia nitrogen by deep oxidation comprises an oxidation area capable of adding sodium hypochlorite for decarburization and nitrogen removal, and a flocculation reaction area capable of adding polyaluminium sulfate and polyacrylamide;
Further preferably, the mass ratio of the adding amount of sodium hypochlorite to the ammonia nitrogen content in the percolate is 80-120:1, preferably, the sodium hypochlorite is sodium hypochlorite solution with the mass concentration of 10%, the adding amount of polyaluminum sulfate is 0.1-2 mg/L, and the adding amount of polyacrylamide is 0.001-0.1 mg/L;
Most preferably, the deep oxidation pond is divided into three grids, stirring devices are respectively arranged, sodium hypochlorite is added into the first grid, sodium hypochlorite and polyaluminium sulfate are added into the second grid, polyacrylamide is added into the third grid, sodium hypochlorite is used for removing ammonia nitrogen in sewage and oxidizing organic pollutants, polyaluminium sulfate and polyacrylamide are combined to act together to remove suspended matters in the sewage, meanwhile, reliable standard reaching of barium ions can be guaranteed, ORP and pH meters are preferably arranged in the deep oxidation pond, the sodium hypochlorite adding amount is controlled on line, preferably, vertical blade stirrers are selected for the stirring devices of the first grid and the second grid, helical gear reducers are selected for the stirring devices of the third grid, and helical gear reducers are selected for the stirring devices of the third grid.
According to the invention, preferably, the second sedimentation tank is an upflow inclined plate sedimentation tank, and is used for settling floc alum flocs generated in the deep oxidation tank.
According to the invention, the laminated filter preferably adopts the existing equipment, and comprises a turbine guide disc and a laminated sheet, wherein sewage passes through the turbine guide disc to form a centrifugal effect, and then the raw water passes through the compressed laminated sheet for surface and deep filtration. Suspended pollutants are trapped on the surface and deep layer areas of the laminated sheets, and filtered water flows out through a water outlet pipe;
preferably, the laminated filter is further provided with a plurality of treatment laminated filter units, when backwashing operation is carried out, water inlet is controlled to be closed through a two-position three-way valve, a water outlet pipe is communicated with a sewage discharge pipe, after the flow direction is changed, produced water of other laminated filter units is used for cleaning, and backwash water outlet is connected into a sludge treatment system through a sludge discharge pipe;
according to the invention, preferably, the outlet water of the laminated filter enters the clear water temporary storage tank, the clear water temporary storage tank is internally provided with water quality on-line monitoring equipment, the outlet water is directly discharged if the water quality is monitored to be qualified, and if the outlet water is not qualified, the outlet water is returned and lifted to the sewage collecting tank for secondary treatment.
According to the invention, preferably, the sludge treatment system comprises a sludge concentration tank for receiving backwash water of each sedimentation tank and a lamination filter, a sludge conditioning tank for condensing and dehydrating the concentrated sludge and a plate-and-frame filter press for press-filtering and dehydrating the conditioned sludge;
The sludge conditioning tank is further preferably provided with stirring equipment for conditioning and stirring and a dosing device for dosing polyaluminium chloride and polyacrylamide, wherein the stirring equipment for conditioning is preferably a vertical frame type stirrer, and the matched speed reducer is preferably a helical gear speed reducer;
preferably, the adding amount of polyaluminium chloride in the sludge conditioning tank is 0.05-1 mg/L, and the adding amount of polyacrylamide is 0.001-0.1 mg/L.
According to the invention, the treatment process of the barium slag percolate is preferably carried out, and a preferred embodiment comprises the following steps:
A1, firstly, allowing slag field percolate to enter a collecting and regulating tank for homogenizing and homogenizing, and ensuring stable water inflow of a subsequent process;
A2, adding ferrous sulfate into the slag field leachate, removing sulfur and barium through chemical precipitation reaction, then adding polyaluminium sulfate to perform flocculation precipitation, and separating flocculated sludge of the ferrous sulfate and the barium sulfate;
A3, adding hydrogen peroxide into the slag field leachate, removing sulfur and degrading organic pollutants through chemical oxidation reaction, then adding alkali liquor and polyacrylamide for flocculation precipitation, and separating a sulfur simple substance and flocculated sludge of ferric hydroxide;
A4, adding sodium hypochlorite into the slag field leachate to perform deep oxidation reaction, further degrading organic pollutants and ammonia nitrogen, then adding polyaluminium sulfate and polyacrylamide to perform flocculation precipitation, and separating flocculated sludge containing a small amount of barium sulfate and sulfur simple substances;
A5, filtering and discharging;
a6, treating the sludge separated in the steps A2, A3 and A4.
According to the present invention, preferably, step A6 includes:
B1, concentrating the sludge separated from the A2, the A3 and the A4 in a sludge concentration tank, reducing the water content, and refluxing the supernatant to a collecting and regulating tank;
B2, feeding the sludge subjected to sludge concentration into a sludge conditioning tank for stirring and conditioning, and adding polyacrylamide into the sludge to improve the sludge dewatering property;
And B3, pumping the conditioned sludge to a plate-and-frame filter press to complete sludge dehydration.
The invention is not described in detail, but is in accordance with the prior art.
The beneficial effects of the invention are as follows:
1. The invention has small occupied area, high efficiency and easy operation and management, and can effectively remove pollutants such as sulfide, barium ions, CODcr, ammonia nitrogen, total phosphorus, SS and the like in the percolate.
2. According to the method, two-stage oxidation is adopted for removing CODcr, meanwhile, a mode of adding chlorine at a folding point is adopted for removing ammonia nitrogen, a biochemical process is not required to be arranged for biological decarburization and nitrogen removal, the operation difficulty and the labor cost of operation and maintenance are reduced, and greater operability is provided for process debugging.
3. The design of process connection in the invention can fully utilize the addition of the medicament, the addition of the ferrous sulfate medicament in the chemical pre-precipitation tank is not only used for removing barium ions and sulfur ions, but also used for catalyzing the hydrogen peroxide added in the oxidation flocculation reaction tank to form Fenton advanced oxidation reaction, thereby further improving oxidation efficiency and realizing high-efficiency treatment of pollutants.
Drawings
FIG. 1CN114684950A is a schematic diagram of an integrated treatment device for slag field leachate.
FIG. 2CN112551756A is a schematic diagram showing a desulfurization pretreatment device for landfill leachate.
FIG. 3 is a process flow diagram of the barium slag leachate of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following specific examples, but is not limited thereto.
Example 1
The embodiment adopts the leachate of a certain barium slag field of a Guizhou Tianzhu, wherein the concentration of COD Cr of the barium slag leachate is 1500mg/L, the concentration of ammonia nitrogen is 85mg/L, the concentration of total phosphorus is 0.05mg/L, the concentration of total barium is 100mg/L, and the concentration of sulfide is 600mg/L.
A treatment process of barium slag percolate comprises a percolate collecting and regulating tank, a chemical pre-sedimentation tank, an oxidation flocculation reaction tank, a first sedimentation tank, a deep oxidation tank, a second sedimentation tank, a laminated filter and a clear water temporary storage tank, wherein the percolate collecting and regulating tank is sequentially arranged and sequentially used for treating percolate, the chemical pre-sedimentation tank is used for synchronously removing sulfur and barium, the oxidation flocculation reaction tank is used for oxidizing sulfide into elemental sulfur and flocculating and settling, the first sedimentation tank is used for solid-liquid separation, the deep oxidation tank is used for deep oxidation and removal of organic pollutants and ammonia nitrogen, the second sedimentation tank is used for solid-liquid separation, the laminated filter and the clear water temporary storage tank are used for treating suspended matters in percolate wastewater, and the sludge treatment system is used for treating sludge separated by each sedimentation tank;
The method comprises the steps that the barium slag percolate wastewater with certain residence time is collected in a percolate collecting tank, stirring equipment is arranged to stir and mix sewage in the percolate collecting tank, the purpose of homogenizing the uniform quantity is achieved, then the wastewater in the tank is lifted to a chemical pre-sedimentation tank through a lifting water pump, and a QJB type submersible stirrer is selected as the stirring equipment;
The chemical pre-sedimentation tank comprises a chemical reaction area and a sedimentation area, wherein the chemical reaction area is divided into two grids, ferrous sulfate is added into the first grid, polymeric flocculant polymeric aluminum sulfate is added into the second grid, stirring equipment is respectively arranged between the two grids and used for mixing and stirring the medicament and the wastewater, wherein sulfide, barium ions and sulfate react to respectively form ferrous sulfate and barium sulfate sediment, simultaneously fine sediment substances form larger flocs under the action of the polymeric aluminum sulfate and are sedimentated in the sedimentation area, and a mud level meter is arranged in the sedimentation area and used for controlling automatic mud discharge. The stirring equipment arranged in the first lattice reaction zone adopts a vertical blade stirrer and a matched speed reducer adopts a bevel gear speed reducer, the stirring equipment arranged in the second lattice reaction zone adopts a vertical frame stirrer and a matched speed reducer adopts a bevel gear speed reducer, the ratio of the adding amount of ferrous sulfate to the mass content of sulfide is 5-7.5:1, the ferrous sulfate medicament is calculated by ferrous sulfate heptahydrate, and the adding amount of polyaluminium sulfate is 1-20 mg/L;
The oxidation flocculation reaction tank is divided into three grids, stirring equipment is respectively arranged, hydrogen peroxide is added into the first grid and the second grid, the hydrogen peroxide oxidizes sulfide in the sewage into elemental sulfur, alkali liquor and polyacrylamide are added into the third grid, the formed tiny flocs form larger flocs under the action of the polyacrylamide, the addition of the hydrogen peroxide and the alkali liquor is controlled by an online ORP meter and a pH meter, the stirring equipment arranged in the first grid and the second grid reaction area adopts a vertical blade stirrer, a matched speed reducer adopts a bevel gear speed reducer, the stirring equipment arranged in the third grid adopts a vertical frame stirrer, the matched speed reducer adopts a bevel gear speed reducer, the hydrogen peroxide is hydrogen peroxide solution with the mass concentration of 27.5%, the ratio of the addition of the hydrogen peroxide to the mass content of the organic pollutant is 0.3-4:1, the alkali liquor is sodium hydroxide solution, the adjustment pH value is 8-11, and the addition of the polyacrylamide is 0.001-0.01mg/L;
The first sedimentation tank is an upflow inclined plate sedimentation tank and is used for settling floc alum blossom generated in the oxidation flocculation sedimentation tank;
The deep oxidation pond is divided into three grids, stirring devices are respectively arranged, sodium hypochlorite is added into the first grid, sodium hypochlorite and polyaluminium sulfate are added into the second grid, polyacrylamide is added into the third grid, the sodium hypochlorite is used for removing ammonia nitrogen in sewage and oxidizing organic pollutants, the polyaluminium sulfate and the polyacrylamide are combined to act together to remove suspended matters in the sewage, meanwhile, the reliable standard reaching of barium ions can be guaranteed, ORP and pH meters are arranged in the deep oxidation pond, the adding amount of the sodium hypochlorite is controlled on line, vertical blade stirrers are selected for the stirring devices of the first grid and the second grid, helical gear reducers are selected for the stirring devices of the third grid, and helical gear reducers are selected for the stirring devices of the third grid. The mass ratio of the adding amount of sodium hypochlorite to the ammonia nitrogen content in the percolate is 80-120:1, the sodium hypochlorite is sodium hypochlorite solution with the mass concentration of 10%, the adding amount of polyaluminum sulfate is 0.1-2mg/L, and the adding amount of polyacrylamide is 0.001-0.1mg/L;
The second sedimentation tank is an upflow inclined plate sedimentation tank and is used for settling floc alum blossom generated in the deep oxidation tank;
The laminated filter comprises a turbine guide disc and a laminated sheet; the sewage passes through the turbine guide plate to form a centrifugal effect, and then the raw water passes through the compressed lamination to carry out surface and deep filtration, suspended pollutants are trapped on the surface and deep areas of the lamination, and filtered water flows out through the water outlet pipe;
The water discharged from the lamination filter enters a clear water temporary storage tank, water quality on-line monitoring equipment is arranged in the clear water temporary storage tank, the discharged water is directly discharged if the water quality is monitored to be qualified, and if the discharged water is not qualified, the discharged water is returned and lifted to a sewage collecting tank for secondary treatment.
The sludge treatment system comprises a sludge concentration tank for receiving backwash water of each sedimentation tank and a lamination filter, a sludge conditioning tank for condensing and dehydrating the concentrated sludge and a plate-and-frame filter press for performing filter pressing and dehydrating on the conditioned sludge, wherein the sludge conditioning tank is provided with stirring equipment for conditioning and stirring and a dosing device for dosing polyaluminium chloride and polyacrylamide, the stirring equipment for conditioning is a vertical frame type stirrer, the matched speed reducer is a helical gear speed reducer, the conditioned sludge is conveyed to the plate-and-frame filter press by using a screw pump, the dosing amount of the polyaluminium chloride in the sludge conditioning tank is 0.05-1mg/L, and the dosing amount of the polyacrylamide is 0.001-0.1mg/L.
Referring to fig. 3, the barium residue percolate firstly enters a collecting and regulating tank, and homogeneous average quantity regulation and control are carried out under the action of a submerged stirrer in the collecting and regulating tank, so that stable water inflow of the subsequent process is ensured;
Pumping the percolate into a chemical pre-sedimentation tank through a lifting water pump, adding ferrous sulfate into a sulfur removal and barium removal area for chemical sedimentation reaction, mechanically stirring, reacting sulfide in the percolate with ferrous ions to generate ferrous sulfide sediment, reacting barium ions with sulfate ions to generate barium sulfate sediment, adding coagulant aid polyaluminum sulfate into a flocculation area, forming larger flocs by the sediment so as to facilitate sedimentation, separating obtained sediment sludge in a sedimentation area, and periodically discharging the sediment sludge into a sludge concentration tank, wherein supernatant fluid of the sedimentation area automatically flows into an oxidation flocculation sedimentation tank;
The pH range of the percolate wastewater in the oxidation flocculation reaction tank is 4-5.5 due to the addition of the medicament in the previous process section, at the moment, the residual sulfide in the oxidized sewage is elemental sulfur by adding hydrogen peroxide in the oxidation area, meanwhile, the residual ferrous ions from the previous process section react with the hydrogen peroxide in Fenton reaction, the reaction of the oxidized sulfide is further enhanced, then, the pH is regulated by adding alkaline solution in the flocculation area, and the polyacrylamide as an auxiliary coagulant is added, so that elemental sulfur and a small amount of Fenton sludge as oxidation products are flocculated into larger flocs;
Allowing the percolate after flocculation reaction to enter a first sedimentation tank, separating elemental sulfur and Fenton sludge in the tank, periodically discharging the separated elemental sulfur and Fenton sludge to a sludge concentration tank, and allowing the supernatant fluid of the first sedimentation tank to flow into a deep oxidation tank;
The percolate fully reacts with the added sodium hypochlorite in an oxidation zone of the deep oxidation pond, ammonia nitrogen is removed, the degradation of the residual COD Cr is completed, and then polyaluminium sulfate and polyacrylamide are added in a flocculation zone for flocculation reaction;
The percolate of the deep oxidation pond enters a second sedimentation pond, sludge containing a small amount of barium sulfate and sulfur simple substances is separated, and the sludge is periodically discharged into a sludge concentration pond;
pumping supernatant of the second sedimentation tank into a lamination filter through a booster pump after the supernatant is discharged from the water tank, removing suspended matters deeply, regularly backwashing the filter, and discharging backwash water into a sludge concentration tank;
the sewage filtered by the laminated filter is discharged into a clear water temporary storage tank, the sewage is discharged up to the standard, and if the process effluent does not reach the standard due to the impact of the water quality of the incoming water, the clear water temporary storage tank is provided with a standby lifting water pump to pump the sewage back to a collecting and regulating tank;
the sludge is concentrated in the sludge concentration tank for more than or equal to 15 hours, the water content of the sludge is reduced, the sludge enters the sludge conditioning tank, the polyacrylamide is added to improve the sludge dewatering performance, and finally the sludge is dewatered by a plate-and-frame filter press and then is transported to the outside for disposal.
In this embodiment, the treatment process effluent indexes of the barium slag percolate are as follows:
COD Cr concentration is below 50mg/L, ammonia nitrogen concentration is below 10mg/L, total phosphorus concentration is below 0.5mg/L, total barium concentration is below 2mg/L, sulfide concentration is below 0.5 mg/L. The emission standard of the water pollutant emission limit value in the emission standard of inorganic chemical industry (GB 31573-2015) is reached.
The above-described embodiments are merely illustrative of the present invention and are not intended to be limiting, and modifications may be made to the embodiments by those skilled in the art without creative contribution as required after reading the present specification, but are protected by patent laws within the scope of the appended claims.
Claims (22)
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| CN102001770A (en) * | 2010-11-30 | 2011-04-06 | 大连化工研究设计院 | A method for removing high organic pollutants in landfill leachate |
| CN114684950A (en) * | 2020-12-31 | 2022-07-01 | 江苏艾特克环境工程设计研究院有限公司 | Integrated treatment device and method for slag yard leachate |
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| CN102786183B (en) * | 2012-03-29 | 2013-06-12 | 波鹰(厦门)科技有限公司 | Method for processing garbage leachate |
| CN113443735A (en) * | 2020-03-26 | 2021-09-28 | 深圳市长隆科技有限公司 | Method for resource utilization of landfill leachate concentrated solution |
| CN112551744A (en) * | 2020-11-20 | 2021-03-26 | 联合环境技术(天津)有限公司 | Method for treating wastewater by utilizing acidic coagulated Fenton oxidation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102001770A (en) * | 2010-11-30 | 2011-04-06 | 大连化工研究设计院 | A method for removing high organic pollutants in landfill leachate |
| CN114684950A (en) * | 2020-12-31 | 2022-07-01 | 江苏艾特克环境工程设计研究院有限公司 | Integrated treatment device and method for slag yard leachate |
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