CN105152415B - Sinter wet-type magnesium method desulfurization purification Waste Water Treatment and technique - Google Patents
Sinter wet-type magnesium method desulfurization purification Waste Water Treatment and technique Download PDFInfo
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- CN105152415B CN105152415B CN201510649459.9A CN201510649459A CN105152415B CN 105152415 B CN105152415 B CN 105152415B CN 201510649459 A CN201510649459 A CN 201510649459A CN 105152415 B CN105152415 B CN 105152415B
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 52
- 230000023556 desulfurization Effects 0.000 title claims abstract description 52
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 34
- 238000000746 purification Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 25
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 17
- 239000011777 magnesium Substances 0.000 title claims abstract description 17
- 239000002351 wastewater Substances 0.000 claims abstract description 168
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 117
- 238000006243 chemical reaction Methods 0.000 claims abstract description 56
- 239000000428 dust Substances 0.000 claims abstract description 47
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- 230000016615 flocculation Effects 0.000 claims abstract description 41
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- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 36
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 32
- 239000012535 impurity Substances 0.000 claims abstract description 32
- 230000018044 dehydration Effects 0.000 claims abstract description 27
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 27
- 239000002245 particle Substances 0.000 claims abstract description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000012716 precipitator Substances 0.000 claims abstract description 25
- 238000005245 sintering Methods 0.000 claims abstract description 23
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- 235000011941 Tilia x europaea Nutrition 0.000 claims description 18
- 239000004571 lime Substances 0.000 claims description 18
- 239000002002 slurry Substances 0.000 claims description 18
- 239000008213 purified water Substances 0.000 claims description 17
- 239000000919 ceramic Substances 0.000 claims description 13
- 238000011084 recovery Methods 0.000 claims description 12
- 229910001385 heavy metal Inorganic materials 0.000 claims description 11
- 238000001223 reverse osmosis Methods 0.000 claims description 10
- 239000008139 complexing agent Substances 0.000 claims description 9
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- 239000000779 smoke Substances 0.000 claims description 3
- 241000370738 Chlorion Species 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 15
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
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- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The present invention disclose a kind of sintering wet-type magnesium method desulfurization purification Waste Water Treatment and technique, including wet electrical dust precipitator wastewater treatment subsystem to the flushing waste water processing of wet electrical dust precipitator, desulfurizing tower output flue gas is handled through mechanical dehydration after the obtained desulfurizing tower wastewater treatment subsystem of dehydration wastewater treatment；The wet electrical dust precipitator wastewater treatment subsystem, including the first wastewater equalization pond being sequentially communicated, first neutralization pond, first reaction tank, first flocculation basin, clarifier, first clear water reserviors, chlorine ion concentration detection means is provided with first clear water reserviors, first clear water reserviors are connected with the desulfurizing tower wastewater treatment subsystem, the desulfurizing tower wastewater treatment subsystem, including the second wastewater equalization pond being sequentially communicated, second neutralization pond, second reaction tank, second flocculation basin, clarifier, second clear water reserviors, and big particle diameter device for filtering impurities, small particle impurity and chlorion filter.
Description
Technical Field
The invention relates to the field of environmental engineering and sewage treatment, in particular to a system and a process for treating desulfurization and purification wastewater by a sintering wet magnesium method.
Background
Because of low operation cost and high desulfurization efficiency, the wet magnesium desulfurization is applied to a large number of projects of sintering or pelletizing of domestic iron and steel enterprises, and meanwhile, in order to reduce investment and operation cost, the existing desulfurization device does not have GGH (gas-gas heat exchanger), the flue gas temperature after desulfurization is only about 50 ℃, although the chimney is subjected to corrosion prevention, the corrosion prevention effect is poor, and the chimney is subjected to low-temperature SO3The corrosion was severe. The desulfurized flue gas contains a large amount of water mist, sulfuric acid mist and fine aerosol, and the substances fall near a chimney, so that dust rain or small snowflakes are easily formed at low temperature. The "landscape" is very polluted.
The high-efficiency wet electrostatic dust collector can effectively remove the phenomena and SO3Heavy metal, fine dust (PM2.5), fine liquid drops and the like, so that the opacity (turbidity) of the flue gas is greatly reduced, the emission concentration of the flue gas is also greatly reduced, and the higher environmental protection requirement is met; in addition, SO3And a large amount of water mist is removed, so that the corrosion prevention grade of the chimney corrosion prevention can be effectively reduced, and the social benefit and the economic benefit are remarkable.
The wet electric dust remover is developed on the basis of a dry electric dust remover. The wet type electric dust collector has high dust removal efficiency, is suitable for treating the smoke containing high specific resistance dust and can purify certain harmful gases, so the wet type electric dust collector has great development in recent years. The flue gas before entering the wet electric dust collector is generally humidified and saturated in a spray tower or an inlet diffusion section. After the saturated flue gas enters an electric field, dust particles or fog drops in the air flow quickly carry charges, the dust particles or the fog drops move to a dust collecting electrode under the action of the electric field force, the fog drops attached to a polar plate are connected into a sheet to form a liquid film, and the liquid film and the dust particles fall into a slurry tank at the lower part of a dust remover under the action of gravity.
The wet-method ash removal is one of the characteristics of a wet-type electric dust remover which is different from a dry-type electric dust remover. The wet electric dust collector utilizes liquid film water flow on the polar plate to remove dust without a rapping device, so that secondary flying of the dust is eliminated, and the dust removal efficiency is improved. Wet type electricityThe dust remover adopts liquid film water flow to remove dust on the pole plate, and the ash cleaning water is generally called flushing water. Because the flushing water contains SO trapped by the wet electric dust collector3Heavy metals, and fine dust (PM2.5), and therefore the flushing wastewater becomes sewage similar to the desulfurization wastewater.
The main pollution indexes of the sintering desulfurization water of domestic iron and steel enterprises are as follows: calcium ion 1000-4000(mg/l) which is liable to cause scaling and chloride ion 15000-20000(mg/l) which is liable to cause corrosion. Through measurement and calculation and on-site assay analysis, the main pollution indexes of the washing and drainage of the wet electric dust remover are as follows: 1000 (mg/l) of calcium ion which is easy to cause scaling and 500(mg/l) of chlorine ion which is easy to cause corrosion. The necessary washing of wet-type electrostatic precipitator has increased the sewage volume of wet flue gas desulfurization system, can carry out effectual purification, retrieval and utilization to this sparge water, will to a great extent influence the application and the popularization of wet-type electrostatic precipitator.
Disclosure of Invention
Aiming at the problems, the invention provides a sintering wet-type magnesium desulfurization purification wastewater treatment system and method for reasonably recovering, treating and utilizing wastewater generated by additionally arranging a wet-type electric precipitator after wet-type magnesium desulfurization.
In order to achieve the aim, the sintering wet-type magnesium desulfurization purification wastewater treatment system comprises a wet-type electric precipitator wastewater treatment subsystem for treating flushing wastewater of a wet-type electric precipitator, a wet-type electric precipitator wastewater recovery subsystem, a desulfurization tower wastewater treatment subsystem for treating dehydration wastewater obtained by mechanically dehydrating desulfurization tower output smoke, and a desulfurization tower wastewater recovery subsystem;
wherein,
the wet-type electric precipitator wastewater treatment subsystem comprises a first wastewater adjusting tank, a first neutralizing tank, a first reaction tank, a first flocculation tank, a clarifier and a first clean water tank which are sequentially communicated and used for storing washing wastewater, wherein a chloride ion concentration detection device is arranged in the first clean water tank, and the first clean water tank is communicated with the desulfurization tower wastewater treatment subsystem;
the wet-type electric precipitator wastewater recovery subsystem comprises a slurry supply pipeline communicated with a slurry supply system of the purification tower and a valve arranged on the slurry supply pipeline;
the desulfurization tower wastewater treatment subsystem comprises a second wastewater adjusting tank, a second neutralizing tank, a second reaction tank, a second flocculation tank, a clarifier, a second clean water tank, a large-particle-size impurity filtering device and a small-particle-size impurity and chloride ion filtering device which are sequentially communicated and used for storing washing wastewater;
the desulfurization tower waste water recovery subsystem comprises an industrial purified water conveying pipeline for communicating small-particle-size impurities and a chlorine ion filtering device with a water replenishing tank of a wet dust collector, and large-particle-size impurity filtering devices respectively arranged on the industrial purified water conveying pipeline;
the first clean water tank is communicated with the second wastewater adjusting tank;
the method comprises the steps that flushing wastewater is buffered by a first wastewater adjusting tank and then is input into a first neutralizing tank at a constant speed according to a preset flow rate to perform acid-base neutralization reaction, then is input into a first reaction tank to perform chemical reaction with lime, then is input into a first flocculation tank to perform flocculation, then is input into a clarifier to obtain supernatant, the supernatant is output into a first clear water tank, the chloride ion concentration of the flushing wastewater in the first clear water tank is detected, if the chloride ion concentration is higher than 20000mg/L, the supernatant is output into a second wastewater adjusting tank, and if the chloride ion concentration is lower than 20000mg/L, the supernatant is output into a slurry supply system of a purification tower;
and (2) inputting the dehydrated wastewater into a second neutralization tank at a constant speed by a second wastewater regulating tank at a preset flow rate for acid-base neutralization reaction, inputting the dehydrated wastewater into a second reaction tank for chemical reaction with lime and a heavy metal complexing agent, inputting the dehydrated wastewater into a second flocculation tank for flocculation, inputting the dehydrated wastewater into a clarifier to obtain supernatant, outputting the supernatant to a second clear water tank, filtering the supernatant by a ceramic membrane filter for impurity filtration reaction with large particle size, wherein the particle size of the large particle size impurities is 0.01-1 mu m, and filtering the obtained filtrate by a reverse osmosis membrane to obtain industrial purified water.
In order to achieve the aim, the process for treating the sintering wet-type magnesium desulfurization purification wastewater comprises the steps of treating the washing wastewater of a wet-type electric precipitator and treating the dehydration wastewater obtained after the mechanical dehydration treatment of the flue gas output by a desulfurization tower;
wherein, the treatment of the dehydration waste water obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower comprises the following steps:
s4.11, inputting the dehydrated wastewater obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower into a second wastewater adjusting tank for storage;
s4.12, outputting the wastewater from the wastewater adjusting tank to a second neutralization tank at a constant speed at a preset flow rate to neutralize the pH value of the dehydrated wastewater;
s4.13, outputting the dehydrated wastewater to a second reaction tank, adding lime and a heavy metal complexing agent into the second reaction tank, and carrying out chemical reaction on the dehydrated wastewater and the lime and heavy metal complexing agent;
s4.14, outputting the dehydrated wastewater to a flocculation tank, adding a flocculating agent into the flocculation tank, and performing flocculation reaction on the dehydrated wastewater;
s4.15, outputting the dehydrated wastewater to a clarifier, and outputting a supernatant to a second clean water tank by the clarifier;
s4.16, filtering the supernatant by using a ceramic filter to perform impurity filtering reaction of large particle size, wherein the particle size of the large particle size impurity is 0.01-1 mu m;
s4.17, filtering the filtrate obtained in the step S4.16 by adopting a reverse osmosis membrane to obtain industrial purified water;
the treatment of washing waste water to wet-type electrostatic precipitator include:
4.21, inputting the dehydrated wastewater obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower into a first wastewater adjusting tank for storage;
s4.22, outputting the wastewater from the wastewater adjusting tank to a first neutralization tank at a constant speed at a preset flow rate to neutralize the pH value of the dehydrated wastewater;
s4.23, outputting the dehydrated wastewater to a first reaction tank, adding lime into the first reaction tank, and carrying out chemical reaction on the dehydrated wastewater and the lime;
s4.24, outputting the dehydrated wastewater to a flocculation tank, adding a flocculating agent into the flocculation tank, and performing flocculation reaction on the dehydrated wastewater;
s4.25, outputting the dehydrated wastewater to a clarifier, and outputting a supernatant to a first clean water tank by the clarifier;
s4.26, detecting the concentration of chloride ions in the supernatant in the first clean water pool,
and if the concentration of the chloride ions in the supernatant is more than 20000mg/L, outputting the supernatant to a second wastewater adjusting tank, and performing steps S4.11 to S4.17.
And if the concentration of the chloride ions in the supernatant is less than or equal to 20000mg/L, outputting the supernatant to a desulfurizing tower for supplying water to the slurry of the desulfurizing tower.
Further, returning the industrial purified water to the wet electric dust collector for washing water of the wet electric dust collector;
and (4) filtering impurities with large particle sizes in the supernatant obtained in the step (S4.16) by using a ceramic filter, filtering the filtrate obtained in the step (S4.17) by using a reverse osmosis membrane, and using the obtained impurities for sintering and batching.
According to the system and the process for treating the sintering wet magnesium desulfurization purification wastewater, the washing water in the purification tower is purified and then returns to the desulfurization tower to be used as slurry supplementing water for desulfurization and recycling. And the waste water discharged according to the slurry concentration requirement in the desulfurizing tower is purified and returned to be used as washing make-up water in the purifying tower. The drainage in the desulfurizing tower is purified by a ceramic membrane filter, and the desulfurizing tower has the advantages of pollution resistance, long service life and the like. The strong brine removed by the membrane system is sent to the sintering ingredients to be used as water for uniformly mixing, and the water system of the whole desulfurization system is in closed cycle without generating harmful wastewater.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
The scheme of adding the wet electric dust collector to the wet desulphurization comprises the following steps: the wet-type electric dust collector tower and the discharge flue are newly added near the desulfurizing tower, the desulfurized saturated flue gas is introduced into the lower part of the wet-type electric dust collector from the middle part of the tower, and the desulfurized saturated flue gas is firstly dehydrated mechanically and then enters the wet-type electric dust collector for purification and then is discharged through a pipeline. The mechanical dewatering and wet electric dust collector washing water is newly added washing waste water outside the water balance of the original desulfurization system. The invention provides a sintering wet magnesium desulfurization purification wastewater treatment system and process for purifying and recycling part of wastewater and rebalancing the water quantity of the system.
Industrial purified water for washing the wet electric dust collector enters a water replenishing tank through a water replenishing pipeline and is connected to a purification tower (a purification demisting tower) through a water pump and an electric valve to be used for washing polar plates of the wet electric dust collector; waste water after washing gets into 1# waste water equalizing basin through electric valve, and waste water promotes to the neutralization pond through the pump in the equalizing basin and adds the acid-base, flows into reaction tank, flocculation tank after the abundant reaction, gets into the clarifier and clarifies, and upper portion clear water flows into the clean water basin, squeezes into the sparge water of handling into desulfurizing tower lower part thick liquid pond with the pump, and the corresponding new water yield that gets into the desulfurizing tower through the moisturizing that reduces.
Example 1
As shown in fig. 1, the system for treating wastewater from sintering wet-type magnesium desulfurization and purification in the present embodiment includes a wet-type electrostatic precipitator wastewater treatment subsystem for treating the rinse wastewater of the wet-type electrostatic precipitator, and a desulfurization tower wastewater treatment subsystem for treating the dehydration wastewater obtained by mechanically dehydrating the flue gas output from the desulfurization tower;
wherein,
the system comprises a wet electric precipitator wastewater treatment subsystem for treating flushing wastewater of a wet electric precipitator, a wet electric precipitator wastewater recovery subsystem, a desulfurizing tower wastewater treatment subsystem for treating dehydration wastewater obtained by mechanically dehydrating flue gas output by a desulfurizing tower, and a desulfurizing tower wastewater recovery subsystem;
wherein,
the wet-type electric precipitator wastewater treatment subsystem comprises a first wastewater adjusting tank, a first neutralizing tank, a first reaction tank, a first flocculation tank, a clarifier and a first clean water tank which are sequentially communicated and used for storing washing wastewater, wherein a chloride ion concentration detection device is arranged in the first clean water tank, and the first clean water tank is communicated with the desulfurization tower wastewater treatment subsystem;
the wet-type electric dust collector wastewater recovery subsystem comprises a slurry supply pipeline communicated with the slurry supply system of the vulcanizing tower and a valve arranged on the slurry supply pipeline;
the desulfurization tower wastewater treatment subsystem comprises a second wastewater adjusting tank, a second neutralizing tank, a second reaction tank, a second flocculation tank, a clarifier, a second clean water tank, a large-particle-size impurity filtering device and a small-particle-size impurity and chloride ion filtering device which are sequentially communicated and used for storing washing wastewater;
the desulfurization tower waste water recovery subsystem comprises an industrial water purification transport pipeline for communicating small-particle-size impurities and a chlorine ion filtering device with a water replenishing tank of a wet dust collector, and large-particle-size impurity filtering devices respectively arranged on the industrial water purification transport pipeline;
the first clean water tank is communicated with the second wastewater adjusting tank;
the method comprises the steps that flushing wastewater passes through a first wastewater adjusting tank and is input into a first neutralizing tank at a constant speed according to a preset flow rate to perform acid-base neutralization reaction, then is input into a first reaction tank to perform chemical reaction with lime, then is input into a first flocculation tank to perform flocculation, and then is input into a clarifier to obtain supernatant, the supernatant is output into a first clear water tank, the chloride ion concentration of the flushing wastewater in the first clear water tank is detected, if the chloride ion concentration is higher than 20000mg/L, the supernatant is output into a second wastewater adjusting tank, and if the chloride ion concentration is lower than 20000mg/L, the supernatant is output into a slurry replenishing system of a vulcanizing tower;
and (2) inputting the dehydrated wastewater into a second neutralization tank at a constant speed by a second wastewater regulating tank at a preset flow rate for acid-base neutralization reaction, inputting the dehydrated wastewater into a second reaction tank for chemical reaction with lime and a heavy metal complexing agent, inputting the dehydrated wastewater into a second flocculation tank for flocculation, inputting the dehydrated wastewater into a clarifier to obtain supernatant, outputting the supernatant to a second clean water tank, filtering the supernatant by using a ceramic filter for impurity filtration reaction with large particle size, wherein the particle size of the large particle size impurities is 0.01-1 mu m, and filtering the obtained filtrate by using a reverse osmosis membrane to obtain industrial purified water.
Example 2
As shown in fig. 1, the sintering wet magnesium desulfurization purification wastewater treatment process of the embodiment includes treatment of washing wastewater of a wet electric precipitator and treatment of dehydration wastewater obtained by mechanical dehydration of flue gas output from a desulfurization tower;
wherein, the treatment of the dehydration waste water obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower comprises the following steps:
s4.11, inputting the dehydrated wastewater obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower into a second wastewater adjusting tank for storage;
s4.12, outputting the wastewater from the wastewater adjusting tank to a second neutralization tank at a constant speed at a preset flow rate to neutralize the pH value of the dehydrated wastewater;
s4.13, outputting the dehydrated wastewater to a second reaction tank, adding lime and a heavy metal complexing agent into the second reaction tank, and carrying out chemical reaction on the dehydrated wastewater and the lime and heavy metal complexing agent;
s4.14, outputting the dehydrated wastewater to a flocculation tank, adding a flocculating agent into the flocculation tank, and performing flocculation reaction on the dehydrated wastewater;
s4.15, outputting the dehydrated wastewater to a clarifier, and outputting a supernatant to a second clean water tank by the clarifier;
s4.16, filtering the supernatant by using a ceramic filter to perform impurity filtering reaction of large particle size, wherein the particle size of the large particle size impurity is 0.01-1 mu m;
s4.17, filtering the filtrate obtained in the step S4.16 by adopting a reverse osmosis membrane to obtain industrial purified water;
the treatment of washing waste water to wet-type electrostatic precipitator include:
s4.21, inputting dehydrated wastewater obtained after mechanical dehydration treatment of the flue gas output by the desulfurizing tower into a first wastewater adjusting tank for storage;
s4.22, outputting the wastewater from the wastewater adjusting tank to a first neutralization tank at a constant speed at a preset flow rate to neutralize the pH value of the dehydrated wastewater;
s4.23, outputting the dehydrated wastewater to a first reaction tank, adding lime into the first reaction tank, and carrying out chemical reaction on the dehydrated wastewater and the lime;
s4.24, outputting the dehydrated wastewater to a flocculation tank, adding a flocculating agent into the flocculation tank, and performing flocculation reaction on the dehydrated wastewater;
s4.25, outputting the dehydrated wastewater to a clarifier, and outputting a supernatant to a first clean water tank by the clarifier;
s4.26, detecting the concentration of chloride ions in the supernatant in the first clean water pool,
and if the concentration of the chloride ions in the supernatant is more than 20000mg/L, outputting the supernatant to a second wastewater adjusting tank, and performing steps S4.11 to S4.18.
And if the concentration of the chloride ions in the supernatant is less than or equal to 20000mg/L, outputting the supernatant to a desulfurizing tower for supplying water to the slurry of the desulfurizing tower.
Returning the industrial purified water to the wet electric dust remover for washing water of the wet electric dust remover;
and (4) filtering impurities with large particle size in the supernatant obtained in the step (S4.16) by using a ceramic filter, filtering the filtrate obtained in the step (S4.18) by using a reverse osmosis membrane, and using the obtained impurities for sintering and batching.
Description of specific examples:
one 360m2 sintering machine of a certain iron and steel enterprise has standard flue gas condition air volume of 1305000Nm3The temperature is 120 ℃, the volume ratio of water vapor is 12%, the original design adopts a set of magnesium wet desulphurization system, a purification tower adopting mechanical dehydration and a wet electric precipitator is added beside the original desulphurization tower, and the washing water in the purification tower needs to be purified and utilized.
And (3) determining by calculation: the amount of mechanical demisting water and flushing water is 1350 and 800, 2150 ton/day
As shown in fig. 1, the novel treatment method for treating and recycling the rinsing wastewater generated by the wet type electric dust collector added for wet type desulfurization in the embodiment of the present invention comprises the following steps:
working mode of new water supply system of purification tower
Mode 1: the valve F1 is closed, the valve F2 is opened, and the new demisting water supply pump supplies water to the demisting tower;
mode 2: opening an F4 valve, opening a reflux pump, and discontinuously working to control the liquid level in the desulfurizing tower;
mode 3: the liquid level in the clear water tank is automatically controlled by a valve;
when the concentration of the chlorine ions in the absorption liquid in the desulfurizing tower reaches 15000-20000mg/L, opening a valve F5 to discharge liquid to the No. 2 wastewater regulating tank, and supplementing fresh absorption liquid after the liquid is finished;
when the absorption liquid in the desulfurizing tower begins to be discharged, the reflux pump stops refluxing;
when the concentration of the wastewater in the demisting tower reaches 20000mg/L, the valves F5, F6 and F7 are opened to discharge the wastewater from the No. 1 wastewater adjusting tank.
Before transformation, the operation of the desulfurizing tower needs to continuously supplement 1350 tons/day of water into the tower, the supplement of 800 tons/day of flushing water in the purifying demisting tower, and the total drainage of 2150 tons/day of flushing water, mechanical dehydration and dehydration of a wet electric precipitator. After the process is transformed according to the invention, 1350 tons of new water do not need to be supplemented to the desulfurizing tower per day, 800 tons of industrial purified water are supplemented to the purifying and demisting tower once a week, 120 tons of concentrated brine is discharged to a sintering and stock yard by the membrane filter at regular time every day for uniformly mixing and batching, the consumption of the new water is greatly reduced, and new discharged sewage is not generated.
Industrial purified water for washing the wet electric dust collector enters the water replenishing tank through a water replenishing pipeline and is connected to the purification demisting tower through a water pump and an electric valve to be used for washing polar plates of the wet electric dust collector; waste water after washing gets into 1# waste water equalizing basin through electric valve, and waste water promotes to the neutralization pond through the pump in the equalizing basin and adds the acid-base, flows into reaction tank, flocculation tank after the abundant reaction, gets into the clarifier and clarifies, and upper portion clear water flows into the clean water basin, squeezes into the sparge water of handling into desulfurizing tower lower part thick liquid pond with the pump, and the corresponding new water yield that gets into the desulfurizing tower through the moisturizing that reduces.
According to the requirement of the desulfurization process, when the concentration of the chloride ions in the absorption liquid in the desulfurization tower reaches 15000-; and pumping the waste water which does not meet the recycling requirement at the lower parts of the clean water tank and the clarifier into a No. 2 waste water adjusting tank for discharging water of the desulfurizing tower by using a pump. Waste water in the regulating reservoir is lifted to a neutralization tank by a pump and added with acid and alkali, flows into a reaction tank and a flocculation tank for full reaction, enters a clarifier for clarification, upper clear water flows into a clear water tank, the concentration of chloride ions in the clear water is higher than 20000(mg/l), and the clear water can be recycled by adopting membrane system desalination.
The common PVDF ultrafiltration membrane cannot be suitable for desulfurization wastewater with high pollution index SDI, the ultrafiltration membrane is easy to block, short in service life, high in pretreatment requirement and the like, the high-anti-fouling ultrafiltration membrane formed by sintering the ceramic membrane can be suitable for desulfurization wastewater treatment, but the equipment cost is higher than that of the PVDF membrane component, the desulfurization wastewater discharge capacity is small, the technical feasible operation reliability is the most important factor, the ceramic membrane filtration service life can reach more than 5 years, and the comprehensive cost performance is higher. And (3) adding a high-pressure reverse osmosis treatment process to the ceramic membrane, taking the purified water subjected to membrane filtration treatment as washing water for supplementing water, and pumping concentrated brine and clarifier removed by the membrane and wastewater in a clean water tank to a sintering ingredient by using a pump to serve as mixing water.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are also included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope defined by the claims.
Claims (3)
1. A sintering wet-type magnesium desulfurization purification wastewater treatment system is characterized by comprising a wet-type electric precipitator wastewater treatment subsystem for treating flushing wastewater of a wet-type electric precipitator, a wet-type electric precipitator wastewater recovery subsystem, a desulfurization tower wastewater treatment subsystem for treating dehydration wastewater obtained by mechanically dehydrating desulfurization tower output smoke, and a desulfurization tower wastewater recovery subsystem;
wherein,
the wet-type electric precipitator wastewater treatment subsystem comprises a first wastewater adjusting tank, a first neutralizing tank, a first reaction tank, a first flocculation tank, a clarifier and a first clean water tank which are sequentially communicated and used for storing washing wastewater, wherein a chloride ion concentration detection device is arranged in the first clean water tank, and the first clean water tank is communicated with the desulfurization tower wastewater treatment subsystem;
the wet-type electric precipitator wastewater recovery subsystem comprises a slurry supply pipeline communicated with a slurry supply system of the purification tower and a valve arranged on the slurry supply pipeline;
the desulfurization tower wastewater treatment subsystem comprises a second wastewater adjusting tank, a second neutralizing tank, a second reaction tank, a second flocculation tank, a clarifier, a second clean water tank, a large-particle-size impurity filtering device and a small-particle-size impurity and chloride ion filtering device which are sequentially communicated and used for storing washing wastewater;
the desulfurization tower waste water recovery subsystem comprises an industrial purified water conveying pipeline for communicating small-particle-size impurities and a chlorine ion filtering device with a water replenishing tank of a wet dust collector, and large-particle-size impurity filtering devices respectively arranged on the industrial purified water conveying pipeline;
the first clean water tank is communicated with the second wastewater adjusting tank;
the method comprises the steps that flushing wastewater is buffered by a first wastewater adjusting tank and then is input into a first neutralizing tank at a constant speed according to a preset flow rate to perform acid-base neutralization reaction, then is input into a first reaction tank to perform chemical reaction with lime, then is input into a first flocculation tank to perform flocculation, then is input into a clarifier to obtain supernatant, the supernatant is output into a first clear water tank, the chloride ion concentration of the flushing wastewater in the first clear water tank is detected, if the chloride ion concentration is higher than 20000mg/L, the supernatant is output into a second wastewater adjusting tank, and if the chloride ion concentration is lower than 20000mg/L, the supernatant is output into a slurry supply system of a purification tower;
and (2) inputting the dehydrated wastewater into a second neutralization tank at a constant speed by a second wastewater regulating tank at a preset flow rate for acid-base neutralization reaction, inputting the dehydrated wastewater into a second reaction tank for chemical reaction with lime and a heavy metal complexing agent, inputting the dehydrated wastewater into a second flocculation tank for flocculation, inputting the dehydrated wastewater into a clarifier to obtain supernatant, outputting the supernatant to a second clear water tank, filtering the supernatant by a ceramic membrane filter for impurity filtration reaction with large particle size, wherein the particle size of the large particle size impurities is 0.01-1 mu m, and filtering the obtained filtrate by a reverse osmosis membrane to obtain industrial purified water.
2. A sintering wet magnesium method desulfurization purification wastewater treatment process is characterized by comprising the steps of treating washing wastewater of a wet electric precipitator and treating dehydration wastewater obtained after mechanical dehydration treatment of flue gas output by a desulfurization tower;
wherein, the treatment of the dehydration waste water obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower comprises the following steps:
s4.11, inputting the dehydrated wastewater obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower into a second wastewater adjusting tank for storage;
s4.12, outputting the wastewater from the wastewater adjusting tank to a second neutralization tank at a constant speed at a preset flow rate to neutralize the pH value of the dehydrated wastewater;
s4.13, outputting the dehydrated wastewater to a second reaction tank, adding lime and a heavy metal complexing agent into the second reaction tank, and carrying out chemical reaction on the dehydrated wastewater and the lime and heavy metal complexing agent;
s4.14, outputting the dehydrated wastewater to a flocculation tank, adding a flocculating agent into the flocculation tank, and performing flocculation reaction on the dehydrated wastewater;
s4.15, outputting the dehydrated wastewater to a clarifier, and outputting a supernatant to a second clean water tank by the clarifier;
s4.16, filtering the supernatant by using a ceramic filter to perform impurity filtering reaction of large particle size, wherein the particle size of the large particle size impurity is 0.01-1 mu m;
s4.17, filtering the filtrate obtained in the step S4.16 by adopting a reverse osmosis membrane to obtain industrial purified water;
the treatment of washing waste water to wet-type electrostatic precipitator include:
4.21, inputting the dehydrated wastewater obtained after the mechanical dehydration treatment of the flue gas output by the desulfurizing tower into a first wastewater adjusting tank for storage;
s4.22, outputting the wastewater from the wastewater adjusting tank to a first neutralization tank at a constant speed at a preset flow rate to neutralize the pH value of the dehydrated wastewater;
s4.23, outputting the dehydrated wastewater to a first reaction tank, adding lime into the first reaction tank, and carrying out chemical reaction on the dehydrated wastewater and the lime;
s4.24, outputting the dehydrated wastewater to a flocculation tank, adding a flocculating agent into the flocculation tank, and performing flocculation reaction on the dehydrated wastewater;
s4.25, outputting the dehydrated wastewater to a clarifier, and outputting a supernatant to a first clean water tank by the clarifier;
s4.26, detecting the concentration of chloride ions in the supernatant in the first clean water pool,
if the concentration of the chloride ions in the supernatant is more than 20000mg/L, outputting the supernatant to a second wastewater adjusting tank, and performing steps S4.11 to S4.17;
and if the concentration of the chloride ions in the supernatant is less than or equal to 20000mg/L, outputting the supernatant to a desulfurizing tower for supplying water to the slurry of the desulfurizing tower.
3. The sintering wet magnesium desulfurization purification wastewater treatment process according to claim 2, wherein the industrial purified water is returned to the wet electric precipitator for washing water of the wet electric precipitator;
and (4) filtering impurities with large particle sizes in the supernatant obtained in the step (S4.16) by using a ceramic filter, filtering the filtrate obtained in the step (S4.17) by using a reverse osmosis membrane, and using the obtained impurities for sintering and batching.
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