CN205170548U - Sintering wet -type magnesium method desulfuration purification effluent disposal system - Google Patents
Sintering wet -type magnesium method desulfuration purification effluent disposal system Download PDFInfo
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- CN205170548U CN205170548U CN201520779686.9U CN201520779686U CN205170548U CN 205170548 U CN205170548 U CN 205170548U CN 201520779686 U CN201520779686 U CN 201520779686U CN 205170548 U CN205170548 U CN 205170548U
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Abstract
The utility model discloses a sintering wet -type magnesium method desulfuration purification effluent disposal system, include and wash waste water treatment's wet -type electrostatic precipitator waste water treatment subsystem, the dehydration waste water treatment's that obtains desulfurizing tower output flue gas desulfurizing tower waste water treatment subsystem to wet -type electrostatic precipitator after mechanical dewatering handles, wet -type electrostatic precipitator waste water treatment subsystem washes the first waste water equalizing basin of waste water, first neutralization pond, initial response pond, first flocculation basin and clarifier, clean water basin including the storage that communicates in proper order, wherein be equipped with chlorine ion concentration measurement device in the clean water basin, the clean water basin with desulfurizing tower waste water reclamation subsystem intercommunication, the clean water basin communicates with the thick liquid make -up system of purifying column, desulfurizing tower waste water reclamation subsystem washes second waste water equalizing basin, second neutralization pond, second reaction tank, second flocculation basin, clarifier, the clean water basin of waste water including the storage that communicates in proper order to and big particle diameter impurity filtering device, granule footpath impurity and chlorion filter equipment.
Description
Technical field
The present invention relates to environmental engineering and sewage treatment area, be specifically related to a kind of sintering wet-type magnesium method desulfurization and purify liquid waste treatment system.
Background technology
Due to wet-type magnesium method desulfurization because working cost is low, desulfuration efficiency is high, so sintered by domestic iron and steel enterprises or engineer applied that pelletizing is a large amount of, simultaneously in order to reduce investment and working cost, existing desulfurizer is without GGH (flue gas heat-exchange unit), and the funnel temperature after desulfurization only about 50 DEG C, although carry out anticorrosion to chimney, but preservative effect is poor, chimney low temperature SO
3seriously corroded.Containing a large amount of water smoke, sulfuric acid mist and fine aerosol in flue gas after desulfurization, these materials descend slowly and lightly near chimney, are easily formed " dust-shower " or " little snowflake " when temperature is low." view " pollutes very serious.
Adopt high-efficient wet-type electrostatic precipitator can effectively remove this type of phenomenon, and effectively can remove SO
3, heavy metal, fine dust (PM2.5), fine drop etc., greatly reduce the opaqueness (opacity) of flue gas, smoke emissioning concentration also will reduce greatly, meets higher environmental requirement; In addition, SO
3with a large amount of removals of water smoke, effectively can reduce the anticorrosion grade of chimney anticorrosion, socialbenefit and economic effect is remarkable.
Wet electrical dust precipitator grows up on the basis of dry electric precipitation device.Because its efficiency of dust collection is high, be applicable to containing high resistivity dust flue gas process, and can purify some obnoxious flavour, therefore, wet electrical dust precipitator has large development in recent years.Enter the flue gas before wet electrical dust precipitator, generally all will be humidified in spray tower or entrance expansion section, and make it saturated.After saturated flue gas enters electric field; grit in air-flow or droplet bring electric charge soon, under the effect of electrical forces, shift to dust collecting electrode, and the droplet be attached on pole plate connects in flakes; form liquid film, liquid film is fallen in the slush-pit launder of fly-ash separator bottom under gravity together with grit.
Wet method deashing is that wet electrical dust precipitator is different from one of feature of dry electric precipitation device.Because wet electrical dust precipitator is the liquid film current dusting out that utilizes on pole plate, without the need to rapping apparatus, because this eliminating the secondary fly-up of dust, improve efficiency of dust collection.Wet electrical dust precipitator adopts liquid film current to remove pole plate dust, generally this deashing water is called wash-down water.Owing to containing the SO that wet electrical dust precipitator traps in wash-down water
3, heavy metal, fine dust (PM2.5), therefore, flush discharge just becomes the sewage being similar to desulfurization wastewater.
The main contamination index of domestic iron and steel enterprises sintering desulfuration water has: easily cause the calcium ion 1000-4000 (mg/l) of fouling and easily cause corrode chlorion 15000-20000 (mg/l).Through measuring and calculating and on-the-spot assay, the main contamination index of wet electrical dust precipitator flush discharge has: easily cause the calcium ion 1000-4000 (mg/l) of fouling and easily cause corrosion chlorion 500-1500 (mg/l).Can the required flushing of wet electrical dust precipitator adds the sewage quantity of wet desulfurization system, effectively purify, reuse to this wash-down water, will largely affect application and the popularization of wet electrical dust precipitator.
Summary of the invention
For the problems referred to above, the invention provides a kind of reasonable recovery, the wet sintering wet-type magnesium method desulfurization of setting up the waste water that wet electrical dust precipitator produces after magnesium processes desulfurization of process, utilization purifies liquid waste treatment system and method.
To achieve the above object of the invention, the present invention sinters wet-type magnesium method desulfurization and to purify liquid waste treatment system, comprises the wet electrical dust precipitator wastewater treatment subsystem of the flushing waste water process to wet electrical dust precipitator, wet electrical dust precipitator waste water reclamation subsystem and thionizer is exported to thionizer wastewater treatment subsystem, the thionizer waste water reclamation subsystem of the dehydration wastewater treatment that flue gas obtains after mechanical dehydration process;
Wherein,
Described wet electrical dust precipitator wastewater treatment subsystem, comprise the first wastewater equalization pond of the storage flushing waste water be communicated with successively, the first neutralization tank, the first reaction tank, the first flocculation basin and settler, clean water basin, be provided with chlorine ion concentration proofing unit in wherein said clean water basin, described clean water basin are communicated with described thionizer waste water reclamation subsystem;
Described wet electrical dust precipitator waste water reclamation subsystem comprises and is communicated with slurries supply pipeline with the slurries make up system of described vulcanization tower and is arranged on the valve on described slurries supply pipeline;
Described thionizer wastewater treatment subsystem, comprise the second wastewater equalization pond of the storage flushing waste water be communicated with successively, the second neutralization tank, the second reaction tank, the second flocculation basin, settler, clean water basin, and Large stone device for filtering impurities, small particle size impurity and chlorion filtration unit;
Thionizer waste water reclamation subsystem comprises industrial water purification transport pipeline and Large stone device for filtering impurities, and described industrial water purification transport pipeline is communicated with the water supply tank of small particle size impurity and chlorion filtration unit and wet scrubber;
Described clean water basin are communicated with described second wastewater equalization pond;
Described flushing waste water at the uniform velocity inputs the first neutralization tank through the first wastewater equalization pond with predetermined amount of flow and carries out acid-base neutralisation reaction, input the first reaction tank again and lime carries out chemical reaction, input the first flocculation basin again to flocculate, input settler again, obtain supernatant liquor, supernatant liquor exports clean water basin to, detect the flushing waste water chlorine ion concentration in clean water basin, if chlorine ion concentration is higher than 20000mg/L, then export described supernatant liquor to second wastewater equalization pond, if chlorine ion concentration is lower than 20000mg/L, then described supernatant liquor is exported to the slurries make up system of scavenging tower,
Described dehydration waste water at the uniform velocity inputs the second neutralization tank through the second wastewater equalization pond with predetermined amount of flow and carries out acid-base neutralisation reaction, input the second reaction tank and lime and heavy metal complexing agent again and carry out chemical reaction, input the second flocculation basin again to flocculate, input settler again, obtain supernatant liquor, supernatant liquor exports clean water basin to, porcelain filter is adopted by supernatant liquor to carry out the contaminant filter reaction of Large stone again, the particle diameter of described Large stone impurity is 0.01 μm ~ 1 μm, adopt reverse osmosis membrane to filter the filtered liquid obtained, obtain industrial water purification.
Further, described Large stone device for filtering impurities is porcelain filter.
The present invention sinters wet-type magnesium method desulfurization and to purify liquid waste treatment system, and in scavenging tower, wash water returns in thionizer and carries out desulphurization circulating use as slurry makeup water after purification.The interior waste water of discharging according to concentration of slurry needs of thionizer returns through purification and rinses make up water as in scavenging tower.Thionizer internal drainage adopts purpose ceramic-film filter purification, has the advantage such as antipollution, long service life.The strong brine that membranous system removes delivers to sintered material as mixing water, and the closed cycle of whole desulphurization system water system, does not produce harmful waste water.
Accompanying drawing explanation
Fig. 1 is present invention process schema.
Embodiment
Below in conjunction with accompanying drawing, the present invention will be further described.
The scheme that wet desulphurization increases wet electrical dust precipitator is: a newly-increased wet electrical dust precipitator tower and discharge flue near thionizer, saturated flue gas after desulfurization is introduced wet electrical dust precipitator bottom in the middle part of tower, first after mechanical dehydration, after entering wet electrical dust precipitator purification, pass through discharge of pipes.Mechanical dehydration and wet electrical dust precipitator wash-down water are outside former desulphurization system water balance, newly-increased flushing waste water.The present invention is the purification of this effluent part, reuse, and system water yield reequilibrate provides a kind of sintering wet-type magnesium method desulfurization and to purify liquid waste treatment system.
Wet electrical dust precipitator rinses and enters water supply tank with industrial water purification by moisturizing pipeline, through water pump, electrically operated valve access scavenging tower (purification deentrainment tower) for rinsing wet electrical dust precipitator pole plate polar curve; Waste water after flushing enters 1# wastewater equalization pond through electrically operated valve, in equalizing tank, waste water rises to neutralization tank through pump and adds soda acid, after inflow reaction tank, flocculation basin fully react, enter settler clarification, top clear water flows into clean water basin, with pump, the wash-down water handled well is squeezed into thionizer lower slurry pond, be correspondingly reduced by the new water yield that moisturizing enters thionizer.
Embodiment 1
As shown in Figure 1, the present embodiment sintering wet-type magnesium method desulfurization is purified liquid waste treatment system, comprises the wet electrical dust precipitator wastewater treatment subsystem of the flushing waste water process to wet electrical dust precipitator, thionizer is exported to the thionizer wastewater treatment subsystem of the dehydration wastewater treatment that flue gas obtains after mechanical dehydration process;
Wherein,
Comprise the wet electrical dust precipitator wastewater treatment subsystem of the flushing waste water process to wet electrical dust precipitator, wet electrical dust precipitator waste water reclamation subsystem and thionizer is exported to thionizer wastewater treatment subsystem, the thionizer waste water reclamation subsystem of the dehydration wastewater treatment that flue gas obtains after mechanical dehydration process;
Wherein,
Described wet electrical dust precipitator wastewater treatment subsystem, comprise the first wastewater equalization pond of the storage flushing waste water be communicated with successively, the first neutralization tank, the first reaction tank, the first flocculation basin and settler, clean water basin, be provided with chlorine ion concentration proofing unit in wherein said clean water basin, described clean water basin are communicated with described thionizer waste water reclamation subsystem;
Described wet electrical dust precipitator waste water reclamation subsystem comprises and is communicated with slurries supply pipeline with the slurries make up system of described vulcanization tower and is arranged on the valve on described slurries supply pipeline;
Described thionizer wastewater treatment subsystem, comprise the second wastewater equalization pond of the storage flushing waste water be communicated with successively, the second neutralization tank, the second reaction tank, the second flocculation basin, settler, clean water basin, and Large stone device for filtering impurities, small particle size impurity and chlorion filtration unit;
Thionizer waste water reclamation subsystem comprises industrial water purification transport pipeline and Large stone device for filtering impurities, and described industrial water purification transport pipeline is communicated with the water supply tank of small particle size impurity and chlorion filtration unit and wet scrubber;
Described clean water basin are communicated with described second wastewater equalization pond;
Described flushing waste water at the uniform velocity inputs the first neutralization tank through the first wastewater equalization pond with predetermined amount of flow and carries out acid-base neutralisation reaction, input the first reaction tank again and lime carries out chemical reaction, input the first flocculation basin again to flocculate, input settler again, obtain supernatant liquor, supernatant liquor exports clean water basin to, detect the flushing waste water chlorine ion concentration in clean water basin, if chlorine ion concentration is higher than 20000mg/L, then export described supernatant liquor to second wastewater equalization pond, if chlorine ion concentration is lower than 20000mg/L, then described supernatant liquor is exported to the slurries make up system of vulcanization tower,
Described dehydration waste water at the uniform velocity inputs the second neutralization tank through the second wastewater equalization pond with predetermined amount of flow and carries out acid-base neutralisation reaction, input the second reaction tank again and lime carries out chemical reaction, input the second flocculation basin again to flocculate, input settler again, obtain supernatant liquor, supernatant liquor exports clean water basin to, porcelain filter is adopted by supernatant liquor to carry out the contaminant filter reaction of Large stone again, the particle diameter of described Large stone impurity is 0.01 μm ~ 1 μm, adopt reverse osmosis membrane to filter the filtered liquid obtained, obtain industrial water purification.
The purify liquid waste technical process for the treatment of system of above-mentioned sintering wet-type magnesium method desulfurization is as follows:
Thionizer is exported dehydration waste water that flue gas obtains after mechanical dehydration process and inputs the second wastewater equalization pond and store by S4.11;
S4.12 at the uniform velocity exports with predetermined flow velocity the potential of hydrogen neutralizing treatment that the second neutralization tank carries out dehydration waste water by described wastewater equalization pond to;
S4.13 exports described dehydration waste water to reaction tank, in described reaction tank, add lime, and described dehydration waste water and described lime carry out chemical reaction;
S4.14 exports described dehydration waste water to flocculation basin, in described flocculation basin, add flocculation agent, and described dehydration waste water carries out flocculation reaction;
S4.15 exports described dehydration waste water to settler, and described settler exports supernatant liquor to clean water basin;
Supernatant liquor adopts porcelain filter to carry out the contaminant filter reaction of Large stone by S4.16, and the particle diameter of described Large stone impurity is 0.01 μm ~ 1 μm;
Supernatant liquor adopts porcelain filter to carry out the contaminant filter reaction of Large stone by S4.17, and the particle diameter of described Large stone impurity is 0.001mm-0.5mm;
S4.17 adopts reverse osmosis membrane to filter by obtaining filtered liquid in step S4.16, obtains industrial water purification;
The process of the described flushing waste water to wet electrical dust precipitator comprises:
Thionizer is exported dehydration waste water that flue gas obtains after mechanical dehydration process and inputs the first wastewater equalization pond and store by S4.21;
S4.22 at the uniform velocity exports with predetermined flow velocity the potential of hydrogen neutralizing treatment that the first neutralization tank carries out dehydration waste water by described wastewater equalization pond to;
S4.23 exports described dehydration waste water to reaction tank, adds lime and heavy metal complexing agent in described reaction tank, and described dehydration waste water and described lime carry out chemical reaction;
S4.24 exports described dehydration waste water to flocculation basin, in described flocculation basin, add flocculation agent, and described dehydration waste water carries out flocculation reaction;
S4.25 exports described dehydration waste water to settler, and described settler exports supernatant liquor to clean water basin;
S4.26 detects the chloride ion-containing concentration of the supernatant liquor in clean water basin,
If the chloride ion-containing concentration in supernatant liquor is greater than 20000mg/L, then export described supernatant liquor to second wastewater equalization pond, carry out step S4.11 to S4.18.
If the chloride ion-containing concentration in supernatant liquor is less than or equal to 20000mg/L, then described supernatant liquor is exported to the slurries supplementary feed that thionizer is used for thionizer.
Described industrial water purification is back to described wet electrical dust precipitator, for the wash-down water of described wet electrical dust precipitator;
Adopted by step S4.16 supernatant liquor porcelain filter to carry out the contaminant filter reaction of Large stone, in the impurity step S4.18 obtained, filtered liquid adopts reverse osmosis membrane to filter, and the impurity obtained is for sintered material.
Specific examples illustrates:
Certain iron and steel enterprise 360m2 sinter machine, flue gas mark condition air quantity 1305000Nm
3/ h, temperature 120 DEG C, water vapour volume ratio 12%, a set of magnesium processes wet desulfurization system of original design employing, present former thionizer is other increases the scavenging tower that adopts mechanical dehydration and wet electrical dust precipitator, needs to purify wash-down water in scavenging tower, utilize.
Determine as calculated: machinery is except fog+washing water quantity=1350+800=2150 ton/sky
As shown in Figure 1, wet type desulfurizing described in the embodiment of the present invention sets up novel treatment and the reuse method new processing method of the flushing waste water that wet electrical dust precipitator produces, and comprises the following steps:
The new waterworks operating mode of scavenging tower
Pattern 1:F1 valve closes, F2 valve opening, new demist working shaft supplies water to deentrainment tower;
Pattern 2:F4 valve opening, reflux pump are opened, discontinuous, control liquid level in thionizer;
Mode 3: in clean water basin, liquid level is controlled automatically by valve;
When absorption liquid chlorine ion concentration reaches 15000-20000mg/L in thionizer, open valve F5 to the discharge opeing of 2# wastewater equalization pond, terminate rear supplementary fresh absorption liquid;
When starting to discharge absorption liquid in thionizer, reflux pump stops backflow;
When waste strength reaches 20000mg/L in deentrainment tower, open the discharge opeing of valve F5, F6, F7 item 1# wastewater equalization pond.
Before transformation, thionizer runs to be needed to the continuous supplementation water yield in tower 1350 tons/day, wash-down water amount of makeup water 800 tons/day in purification deentrainment tower, and wash-down water and mechanical dehydration, wet electrical dust precipitator dehydration add up to draining 2150 tons/day.After present invention process transformation, thionizer does not need 1350 tons/day, supplementary new water, once industrial water purification 800 tons is supplemented in every circumference purification deentrainment tower, 120 tons of strong brines are discharged to sintering by film filter timing every day, stock ground mixing dosage uses, greatly reduce new water consumption, do not produce new externally discharged waste water.
Wet electrical dust precipitator rinses and enters water supply tank with industrial water purification by moisturizing pipeline, through water pump, electrically operated valve access purification deentrainment tower for rinsing wet electrical dust precipitator pole plate polar curve; Waste water after flushing enters 1# wastewater equalization pond through electrically operated valve, in equalizing tank, waste water rises to neutralization tank through pump and adds soda acid, after inflow reaction tank, flocculation basin fully react, enter settler clarification, top clear water flows into clean water basin, with pump, the wash-down water handled well is squeezed into thionizer lower slurry pond, be correspondingly reduced by the new water yield that moisturizing enters thionizer.
According to sulfur removal technology needs, when absorption liquid chlorine ion concentration reaches 15000-20000mg/L in thionizer, open electrically operated valve to the discharge opeing of 2# wastewater equalization pond, terminate rear supplementary fresh absorption liquid; The 2# wastewater equalization pond of thionizer draining squeezed into by the waste water pump that clean water basin and settler bottom do not meet reuse requirement.In equalizing tank, waste water rises to neutralization tank through pump and adds soda acid, after inflow reaction tank, flocculation basin fully react, enter settler clarification, top clear water flows into clean water basin, this clear water chlorine ion concentration, higher than 20000 (mg/l), needs to adopt the recycle of membranous system desalination ability.
Common PVDF material ultra-filtration membrane can not be suitable for the desulfurization wastewater of high pollution index SDI, its ultra-filtration membrane easily blocks up, work-ing life is short, pre-processing requirements is high, and the high anti-soil ultra-filtration membrane of ceramic membrane sintering can be suitable for desulfurization wastewater process, but cost of equipment is higher than PVDF material membrane module, because desulfurization wastewater discharge capacity is less, technical feasibility serviceability is most important factor, and add that ceramic membrane filter can reach more than 5 years work-ing life, comprehensive cost performance is higher.Ceramic membrane adds high pressure ro treatment technology, and the water purification after membrane filtration process is as wash-down water moisturizing, and under the strong brine under film removes and settler and clean water basin, waste water pump is got to sintered material and done mixing water.
Above; be only preferred embodiment of the present invention, but protection scope of the present invention is not limited thereto, is anyly familiar with those skilled in the art in the technical scope that the present invention discloses; the change that can expect easily or replacement, all should be encompassed within protection scope of the present invention.Therefore, the protection domain that protection scope of the present invention should define with claim is as the criterion.
Claims (2)
1. a sintering wet-type magnesium method desulfurization is purified liquid waste treatment system, it is characterized in that, comprise the wet electrical dust precipitator wastewater treatment subsystem of the flushing waste water process to wet electrical dust precipitator, wet electrical dust precipitator waste water reclamation subsystem and thionizer is exported to thionizer wastewater treatment subsystem, the thionizer waste water reclamation subsystem of the dehydration wastewater treatment that flue gas obtains after mechanical dehydration process;
Wherein,
Described wet electrical dust precipitator wastewater treatment subsystem, comprise the first wastewater equalization pond of the storage flushing waste water be communicated with successively, the first neutralization tank, the first reaction tank, the first flocculation basin and settler, clean water basin, be provided with chlorine ion concentration proofing unit in wherein said clean water basin, described clean water basin are communicated with described thionizer waste water reclamation subsystem;
Described wet electrical dust precipitator waste water reclamation subsystem comprises and is communicated with slurries supply pipeline with the slurries make up system of scavenging tower and is arranged on the valve on described slurries supply pipeline;
Described thionizer wastewater treatment subsystem, comprise the second wastewater equalization pond of the storage flushing waste water be communicated with successively, the second neutralization tank, the second reaction tank, the second flocculation basin, settler, clean water basin, and Large stone device for filtering impurities, small particle size impurity and chlorion filtration unit;
Thionizer waste water reclamation subsystem comprises industrial water purification transport pipeline and Large stone device for filtering impurities, and described industrial water purification transport pipeline is communicated with the water supply tank of small particle size impurity and chlorion filtration unit and wet scrubber;
Described clean water basin are communicated with described second wastewater equalization pond;
Described flushing waste water at the uniform velocity inputs the first neutralization tank with predetermined amount of flow and carries out acid-base neutralisation reaction after the first wastewater equalization pond buffering, input the first reaction tank again and lime carries out chemical reaction, input the first flocculation basin again to flocculate, input settler again, obtain supernatant liquor, supernatant liquor exports clean water basin to, detect the flushing waste water chlorine ion concentration in clean water basin, if chlorine ion concentration is higher than 20000mg/L, then export described supernatant liquor to second wastewater equalization pond, if chlorine ion concentration is lower than 20000mg/L, then described supernatant liquor is exported to the slurries make up system of scavenging tower,
Described dehydration waste water at the uniform velocity inputs the second neutralization tank through the second wastewater equalization pond with predetermined amount of flow and carries out acid-base neutralisation reaction, input the second reaction tank and lime and heavy metal complexing agent again and carry out chemical reaction, input the second flocculation basin again to flocculate, input settler again, obtain supernatant liquor, supernatant liquor exports clean water basin to, purpose ceramic-film filter is adopted by supernatant liquor to carry out the contaminant filter reaction of Large stone again, the particle diameter of described Large stone impurity is 0.001mm-0.5mm, adopt reverse osmosis membrane to filter the filtered liquid obtained, obtain industrial water purification.
2. sintering wet-type magnesium method desulfurization according to claim 1 is purified liquid waste treatment system, and it is characterized in that, described Large stone device for filtering impurities is porcelain filter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520779686.9U CN205170548U (en) | 2015-09-30 | 2015-09-30 | Sintering wet -type magnesium method desulfuration purification effluent disposal system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520779686.9U CN205170548U (en) | 2015-09-30 | 2015-09-30 | Sintering wet -type magnesium method desulfuration purification effluent disposal system |
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| CN205170548U true CN205170548U (en) | 2016-04-20 |
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| CN201520779686.9U Withdrawn - After Issue CN205170548U (en) | 2015-09-30 | 2015-09-30 | Sintering wet -type magnesium method desulfuration purification effluent disposal system |
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- 2015-09-30 CN CN201520779686.9U patent/CN205170548U/en not_active Withdrawn - After Issue
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Granted publication date: 20160420 Effective date of abandoning: 20170825 |