CN210764730U - Zero-emission treatment system for sintering wet-type desulfurization wastewater - Google Patents
Zero-emission treatment system for sintering wet-type desulfurization wastewater Download PDFInfo
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Abstract
The utility model relates to a zero release processing system of sintering wet-type desulfurization waste water belongs to the sewage treatment field. The system of the utility model removes Mg including the pretreatment and the adjusting device for the pretreatment and the mud-water separation2+First-stage reaction with ammonia nitrogen, precipitation device, separation and removal of precipitated magnesium hardness and PO4 3‑、SO4 2‑、F‑A secondary reaction and precipitation device for partial heavy metal ions, a tertiary reaction and precipitation device for separating and removing the rest heavy metal ions in the wastewater, a sewage post-treatment device for separating and removing the rest ammonia nitrogen and reducing COD, a sludge treatment device for carrying out concentration and dehydration treatment on the discharged sludge to treat the sintering wet-type desulfurization wastewater to obtain a water solution containing a large amount of chloride ions and a sludge cake capable of being transported outside, wherein the treated water solution contains a large amount of chloride ions and can be used for preparing a spraying liquid (CaCl) for sintering finished ore2Solution), to achieve zero-emission treatment of sintering wet desulfurization wastewater.
Description
Technical Field
The utility model belongs to the sewage treatment field, concretely relates to zero release processing system of sintering wet-type desulfurization waste water.
Background
With the stricter national environmental protection policy, the treatment and recycling of sintering desulfurization waste water become more and more urgent. At present, the wet sintering desulfurization devices established by iron and steel enterprises in China mostly use wet desulfurization devices of coal-fired power plants for reference, and the wastewater treatment also correspondingly uses a desulfurization wastewater treatment method of the coal-fired power plants for reference. However, the water quality of the wet desulphurization wastewater of the coal-fired power plant is similar to that of the sintering wet flue gas desulphurization wastewater, but the water quality of the wet desulphurization wastewater of the coal-fired power plant is also fundamentally different, and the biggest difference between the water quality of the wet desulphurization wastewater of the coal-fired power plant and the water quality of the sintering wet flue gas desulphurization wastewater is that the sintering desulphurization wastewater contains a large amount of ammonia nitrogen (usually 500-700 mg/L), and the power. In addition, because the components of the sintering raw material ore are different, the contents of magnesium ions and heavy metals are far higher than those of the desulfurization wastewater of a power plant. Therefore, the existing wet desulphurization wastewater treatment process of the coal-fired power plant is not completely suitable for the sintering wet desulphurization wastewater treatment process.
At present, most of sintering desulfurization waste water of iron and steel enterprises is used for blast furnace water slag flushing or steel making slag treatment after being treated, but because the desulfurization waste water contains a large amount of Cl-(12000 mg/L-22000 mg/L), not only causes serious corrosion to slag treatment pipelines and equipment, but also influences the quality and utilization of slag, and limits the recycling of the desulfurization waste water. Therefore, part of the desulfurization wastewater of the iron and steel enterprises is directly discharged after being treated, but the discharged water quality is difficult to reach the standard; therefore, individual enterprises have started to implement zero discharge of desulfurization wastewater by adopting an evaporative crystallization process, but the investment and the operating cost of evaporative crystallization are extremely high, and the popularization and the application of the technology are limited.
Therefore, an economical and feasible treatment system capable of realizing zero discharge of sintering desulfurization wastewater needs to be researched and researched.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a zero release processing system of sintering wet flue gas desulfurization waste water.
In order to achieve the above purpose, the utility model provides a following technical scheme:
the utility model provides a sintering wet desulfurization waste water's zero release processing system, the system is including the preliminary treatment and adjusting device, one-level reaction and precipitation device, second grade reaction and precipitation device, tertiary reaction and precipitation device and the sewage aftertreatment device that set up in order, the system still includes the sludge treatment equipment who links to each other respectively with preliminary treatment and adjusting device, one-level reaction and precipitation device, second grade reaction and precipitation device and tertiary reaction and precipitation device.
Preferably, the pretreatment and regulation device comprises a regulation tank 1, a mud scraper 2 and a wastewater lift pump 3.
Preferably, the first-stage reaction and sedimentation device comprises a reaction tank I4, a front pH adjusting tank 5 and a MAP clarifying tank 6 which are arranged in sequence.
More preferably, the reaction tank I and the front pH adjusting tank are both mechanical reaction tanks.
More preferably, the front pH adjusting tank comprises a primary adjusting tank and a secondary adjusting tank.
More preferably, the MAP clarifier is a mechanical accelerated clarifier, and the surface load of the MAP clarifier is 0.5m3/m2And h, adding a PAM polymer coagulant aid at the inlet bottom plate of the second reaction chamber of the MAP clarifier, and performing sludge-water separation in the separation chamber of the MAP clarifier to remove generated sediment and floccule.
Preferably, the secondary reaction and sedimentation device comprises an aeration tank 7, a reaction tank II 8 and a secondary clarification tank 9 which are arranged in sequence.
More preferably, the aeration tank performs forced aeration in a perforated pipe manner.
More preferably, the reaction tank II is a mechanical reaction tank.
More preferably, the reaction tank II comprises a first-stage reaction tank and a second-stage reaction tank, NaOH is added at the inlet end of the first-stage reaction tank, and slaked lime milk is added at the outlet end of the first-stage reaction tank.
More preferably, the secondary clarifier is a mechanical accelerated clarifier, and the surface load of the secondary clarifier is 0.5m3/m2And h, adding a PAM (polyacrylamide) high-molecular coagulant aid at the bottom plate of the inlet of the second reaction chamber of the secondary clarification tank, and performing sludge-water separation in the separation chamber of the secondary clarification tank to remove generated precipitates.
Preferably, the third-stage reaction and precipitation device comprises an intermediate water tank 10, a second-stage lift pump 11, a reaction tank III 12, a reaction tank IV 13 and a third-stage clarification tank 14 which are sequentially arranged.
More preferably, the reaction tank III and the reaction tank IV are both mechanical reaction tanks.
More preferably, the tertiary clarifier is a mechanical accelerated clarifier, and the surface load of the tertiary clarifier is 0.5m3/m2And h, adding a PAM (polyacrylamide) high-molecular coagulant aid at the bottom plate of the inlet of the second reaction chamber of the three-stage clarification tank, and performing sludge-water separation in the separation chamber of the three-stage clarification tank to remove generated sediments and floccules.
Preferably, the sewage post-treatment device comprises a post-pH adjusting tank 15, a reaction tank V16, a water producing tank 17 and a pressurizing pump 18 which are arranged in sequence.
More preferably, the post-pH adjusting tank comprises a primary adjusting tank and a secondary adjusting tank.
Preferably, the sludge treatment device comprises a sludge concentration tank 19, a sludge adjusting tank 20, a sludge pump 21 and a sludge dewatering machine 22 which are arranged in sequence.
More preferably, the sludge concentration tank is a gravity type sludge concentration tank, and the surface load of the sludge concentration tank is 0.4-0.5 m3/m2.h。
More preferably, the sludge dewatering machine is a plate-and-frame filter press.
The beneficial effects of the utility model reside in that:
1. the utility model discloses a zero discharge treatment method of sintering wet desulfurization waste water, in the treatment process, firstly use Na after mud-water separation2HPO4NaOH makes Mg in waste water2+MgNH is generated with ammonia nitrogen4PO4Precipitating to remove partial Mg in wastewater2+The reaction with ammonia nitrogen and the components contained in the wastewater are utilized to react with each other, so that the input of other reagents is reduced, and the treatment cost is reduced;
2. the water solution containing chloride ions and the mud cakes which can be transported outside are obtained after the treatment by the method, so that zero discharge of waste water is really realized, and meanwhile, the water solution containing chloride ions obtained after the treatment can be completely used for preparing the spraying liquid of the sintering finished ore, so that the chloride ions in the waste water are recycled, the cost of the medicament prepared by the spraying liquid of the sintering finished ore is saved, and the resource recovery and reutilization are realized;
3. the utility model discloses a processing compares with current preliminary treatment + membrane concentration + evaporative crystallization's zero row technology, greatly reduced investment and working costs, the investment is about the latter 1/10, and the working costs is about the latter 1/5 ~ 1/8, has saved occupation of land and operation maintenance cost greatly, and the occupation of land is about the latter 1/3, and maintenance cost is about the latter 1/8 ~ 1/10.
Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention. The objectives and other advantages of the invention may be realized and attained by the means of the instrumentalities and/or combinations particularly pointed out in the appended claims.
Drawings
For the purposes of promoting a better understanding of the objects, features and advantages of the invention, reference will now be made to the following detailed description taken in conjunction with the accompanying drawings in which:
FIG. 1 is a process flow diagram of a zero-emission treatment system for sintering wet desulfurization wastewater;
FIG. 2 is a diagram of a zero-emission treatment system for sintering wet desulfurization wastewater;
wherein: 1-a regulating reservoir; 2-a mud scraper; 3-a wastewater lift pump; 4-reaction tank I; 5-front pH adjusting tank; 6-MAP clarification tank; 7-an aeration tank; 8-a reaction tank; 9-a secondary clarification tank; 10-an intermediate pool; 11-a secondary lift pump; 12-reaction tank iii; 13-reaction tank IV; 14-a third-stage clarification tank; 15-pH adjusting tank; 16-reaction tank V; 17-a water producing pond; 18-a pressure pump; 19-sludge concentration tank; 20-a slurry adjusting tank; 21-a slurry pump; 22-sludge dewatering machine.
Detailed Description
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein. The present invention can also be implemented or applied through other different specific embodiments, and various details in the present specification can be modified or changed based on different viewpoints and applications without departing from the spirit of the present invention.
A zero-emission treatment system of sintering wet desulfurization wastewater is characterized in that a process flow diagram of the treatment system is shown in figure 1, and used devices are shown in figure 2, wherein the system comprises a pretreatment and regulation device (comprising a regulation tank 1, a mud scraper 2 and a wastewater lift pump 3) which are sequentially arranged, a first-stage reaction and precipitation device (comprising a reaction tank I4, a front pH regulation tank 5 and an MAP clarification tank 6 which are sequentially arranged), a second-stage reaction and precipitation device (comprising an aeration tank 7, a reaction tank II 8 and a second-stage clarification tank 9 which are sequentially arranged), a third-stage reaction and precipitation device (comprising a middle water tank 10, a second-stage lift pump 11, a reaction tank III 12, a reaction tank IV 13 and a third-stage clarification tank 14 which are sequentially arranged) and a sewage post-treatment device (comprising a rear pH regulation tank 15, a reaction tank 16, a water production tank 17 and a pressure pump 18 which are sequentially arranged), and the system further comprises a pretreatment and regulation device, a sludge scraper 2, the sludge treatment device (comprising a sludge concentration tank 19, a sludge adjusting tank 20, a sludge pump 21 and a sludge dewatering machine 22 which are sequentially arranged) is respectively connected with the first-stage reaction and precipitation device, the second-stage reaction and precipitation device and the third-stage reaction and precipitation device, and the concrete treatment steps are as follows:
1. carrying out pretreatment and sludge-water separation in a pretreatment and regulation device: sending the sintering wet-type desulfurization wastewater to be treated into a pretreatment and regulation device, carrying out mud-water separation and homogeneous uniform treatment in a regulation tank 1 to obtain wastewater I and sludge discharge I, wherein a sludge scraper 2 and a wastewater lifting pump 3 are arranged in the pretreatment and regulation device, and the sludge scraper 2 is used for scraping accumulated sludge deposited at the bottom of the regulation tank.
2. Mg is separated and removed in a first-stage reaction and precipitation device2+And ammonia nitrogen:
performing an experiment on the wastewater I to determine the ammonia nitrogen content in the wastewater I;
pressurizing the wastewater I by using a wastewater lifting pump 3, uniformly sending the wastewater I into a first-stage reaction and precipitation device for next treatment, namely uniformly lifting the wastewater I by using the wastewater lifting pump 3, sending the wastewater I into a reaction tank I, and adding Na according to the N to P ratio of 1: 1.2-1.52HPO4Reacting for 15-20 min, wherein the reaction tank I is a mechanical reaction tank;
after the reaction is finished, the mixture enters a front pH adjusting tank (for two-stage adjustment, the front pH adjusting tank comprises a first-stage adjusting tank and a second-stage adjusting tank respectively, and the reaction is carried out in each stage of adjusting tank for more than 15 min), NaOH is added to adjust the pH of the solution to be 8.5-9.5, so that Mg contained in the wastewater is enabled to be in a range of 8.5-9.52+And NH4 +Reaction of NH4 ++Mg2++PO4 3-＝MgNH4PO4↓, generating MgNH4PO4(MAP) precipitate;
then enters a surface load of0.5m3/m2H, in the MAP clarification tank 6, wherein the MAP clarification tank 6 is a mechanical accelerated clarification tank, PAM (polyacrylamide) polymer coagulant aid (the mass-to-volume ratio of the PAM polymer coagulant aid to the solution is 1-2: 1, Mg: L) is added at the bottom plate of the inlet of a second reaction chamber of the MAP clarification tank 6 for accelerated sedimentation for more than 2h, then sludge-water separation is carried out in a separation chamber of the MAP clarification tank 6 to remove generated sediment and floccule, and part of Mg contained in the wastewater is removed2+And more than 90% of ammonia nitrogen, and separating to obtain wastewater II and sludge II.
3. Separating and removing part of heavy metal ions in a secondary reaction and precipitation device:
placing the wastewater II in an aeration tank for 30-40 min, and performing forced aeration in a perforated pipe mode to remove reducing substances (such as SO) in the wastewater II3 2-、S2O3 2-Etc.) to facilitate the subsequent operations of precipitation and reducing COD in the wastewater;
then taking the wastewater after aeration treatment to perform a beaker experiment to determine the magnesium hardness and PO in the precipitated wastewater II4 3-、SO4 2-、F-And the amount of slaked lime milk required by part of heavy metal ions, thereby determining the amount of standard slaked lime milk required to be added into the wastewater II;
introducing the wastewater into a reaction tank II 8 after the aeration treatment is finished, wherein the reaction tank II is a mechanical reaction tank and comprises a first-stage reaction tank and a second-stage reaction tank, adding NaOH at the inlet end of the first-stage reaction tank, adding slaked lime milk (added according to the amount which is 1.2 times of the standard slaked lime milk amount) at the outlet end of the first-stage reaction tank, then introducing the slaked lime milk into the second-stage reaction tank, and reacting in each stage of reaction tank for more than 30min to ensure that Mg in the wastewater is contained2+、PO4 3-、SO4 2-、F-、Mn2+And Cr3+The heavy metal ions react to generate Mg (OH)2、Ca3(PO4)2、CaSO4、CaF2、Mn(OH)2And Cr (OH)3And (d) precipitating, wherein the reaction occurs as follows: MgCl2+Ca(OH)2＝Mg(OH)2↓+CaCl2，3Ca2++2PO4 3-＝Ca3(PO4 3-)2↓，Ca2++SO4 2-＝CaSO4↓，Ca2++2F-＝CaF2↓，Cu2++2OH-＝Cu(OH)2↓，Mn2++2OH-＝Mn(OH)2↓，Cr3++3OH-＝Cr(OH)3↓。
The wastewater from the second-stage reaction tank of the reaction tank II continuously enters the surface load of 0.5m3/m2H, a secondary clarification tank 9, wherein the secondary clarification tank 9 is a mechanical accelerated clarification tank, PAM high-molecular coagulant aid is added at the bottom plate of the inlet of a second reaction chamber of the secondary clarification tank 9 so as to form larger flocs, the precipitation is accelerated for more than 2h, then the generated precipitate and the flocs are removed in a separation chamber of the secondary clarification tank 9, and wastewater III and sludge III are obtained by separation.
4. And (3) separating and removing the rest heavy metal ions in the wastewater in a three-stage reaction and precipitation device:
performing a beaker experiment on the wastewater III to determine heavy metal ions (Pb) in the wastewater III2+、Cd2+And Hg2+Etc.) the amount of standard metal capture required to be added for the reaction;
the wastewater III enters an intermediate water tank 10 to stay for more than 30min, and is pressurized by a secondary lift pump 11 and sent into a reaction tank III 12, wherein the reaction tank III is a mechanical reaction tank, and an organic sulfide heavy metal trapping agent is added according to 1.2-1.3 times of the standard metal trapping agent, so that the residual Pb in the wastewater2+、Cd2+And Hg2+S in heavy metal ion and metal scavenger2-Reacting for more than 30min to form stable heavy metal organic sulfide precipitate;
after the precipitation reaction is finished, the reaction product enters a reaction tank IV 13, wherein the reaction tank IV is a mechanical reaction tank, and polyaluminium chloride (PAC), polyferric sulfate (PFS) or ferric trichloride are added as a coagulant to react for more than 2min so as to destabilize the colloid;
then the wastewater enters the surface with the load of 0.5m3/m2H three stage clarifierAnd 14, the three-stage clarification tank is a mechanical accelerated clarification tank, PAM (polyacrylamide) high-molecular coagulant aid is added at the bottom plate of the inlet of the second reaction chamber of the three-stage clarification tank to form larger flocs, the larger flocs are precipitated for more than 2 hours in an accelerated manner, finally, the generated precipitates and the flocs are removed from a separation chamber of the three-stage clarification tank, and water is separated to obtain wastewater IV and sludge IV.
5. Separating and removing residual ammonia nitrogen and reducing COD in a sewage post-treatment device:
adding HCl to adjust the pH value of the solution to be 6.0-7.0 in a pH adjusting tank (for two-stage adjustment, including a first-stage adjusting tank and a second-stage adjusting tank respectively, and reacting for more than 15min in each stage of adjusting tank) after the wastewater IV enters;
and (2) continuously feeding the wastewater after the pH is adjusted into a reaction tank V16, wherein the reaction tank V is a mechanical reaction tank, adding NaClO for reaction for more than 30min to remove a small amount of residual ammonia nitrogen in the wastewater, further reducing the COD of the wastewater and enabling the content of the ammonia nitrogen in the wastewater to be less than or equal to 5mg/L, and the generated reaction comprises the following steps: NaClO + H2O＝HClO+NaOH，NH4 ++HClO→NH2Cl+H++H2O，NH2Cl+HClO→NHCl2+H2O，2NH2Cl+HClO→N2↑+3H++3Cl-+H2O，2NaClO+SO3 2-═Na2SO4↓+2Cl-；
And (3) enabling water from the reaction tank V to enter a water generating tank to obtain an aqueous solution containing chloride ions, wherein the mass volume concentration of the chloride ions is 12000-22000 mg/L.
Because the water solution in the water generating tank contains a large amount of chloride ions, the water solution can be sent to a spraying system of sintering finished ore through a pressure pump and used as a solvent for preparing a calcium chloride solution, so that resource recycling and real zero emission are realized.
6. Carrying out concentration and dehydration treatment on the discharged sludge in a sludge treatment device:
pumping the sludge I, the sludge II, the sludge III and the sludge IV obtained after the treatment in the previous steps to a surface load of 0.4-0.5 m3/m2H, concentrating the sludge in a sludge concentration tank 19 for more than 4h, wherein the sludge concentration tankIs a gravity type sludge concentration tank;
the concentrated sludge is firstly passed through a sludge regulating tank 20, then is pressurized by a slurry pump 21 and then is sent into a sludge dewatering machine 22 for dewatering treatment, and then sludge cakes capable of being transported outside are obtained;
wherein the effective volume of the slurry adjusting tank 20 is set to be larger than the sludge inlet amount of the sludge dewatering machine 22 for the convenience of operation.
The utility model discloses the ammonia nitrogen content in sintering wet desulfurization waste water after handling is less than or equal to 5mg/L, and surplus a large amount of chloride ions in aqueous can be regarded as preparing sintering finished ore and spray liquid (CaCl)2Solution), it is thus seen that the utility model discloses a processing method has not only realized the zero release of sintering desulfurization waste water, has also practiced thrift the quantity of solid calcium chloride when preparing sintering finished ore spraying liquid greatly, has good application prospect.
Finally, the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions may be made to the technical solutions of the present invention without departing from the spirit and scope of the technical solutions, and all of them should be covered by the scope of the claims of the present invention.
Claims (10)
1. The system is characterized by comprising a pretreatment and regulation device, a primary reaction and precipitation device, a secondary reaction and precipitation device, a tertiary reaction and precipitation device and a sewage post-treatment device which are sequentially arranged, and further comprising a sludge treatment device respectively connected with the pretreatment and regulation device, the primary reaction and precipitation device, the secondary reaction and precipitation device and the tertiary reaction and precipitation device.
2. The zero discharge treatment system of sintering wet desulphurization waste water according to claim 1, characterized in that the pretreatment and conditioning device comprises a conditioning tank (1), a mud scraper (2) and a waste water lift pump (3).
3. The zero emission treatment system of sintering wet desulfurization waste water according to claim 1, characterized in that said primary reaction and precipitation device comprises a reaction tank I (4), a front pH adjusting tank (5) and a MAP clarification tank (6) arranged in sequence.
4. The zero emission treatment system of sintering wet desulphurization waste water according to claim 3, characterized in that the reaction tank I and the front pH adjusting tank (5) are both mechanical reaction tanks, and the MAP clarifier (6) is a mechanical accelerated clarifier.
5. The zero discharge treatment system of sintering wet desulfurization waste water according to claim 1, characterized in that said secondary reaction and precipitation device comprises an aeration tank (7), a reaction tank II (8) and a secondary clarification tank (9) arranged in sequence.
6. The zero emission treatment system of sintering wet desulfurization waste water according to claim 5, characterized in that the aeration tank (7) is forcibly aerated by means of perforated pipes; the reaction tank II (8) is a mechanical reaction tank, the reaction tank II (8) comprises a first-stage reaction tank and a second-stage reaction tank, NaOH is added at the inlet end of the first-stage reaction tank, and slaked lime milk is added at the outlet end of the first-stage reaction tank; the secondary clarification tank (9) is a mechanical accelerated clarification tank.
7. The zero discharge treatment system of sintering wet desulfurization waste water according to claim 1, characterized in that said three-stage reaction and precipitation device comprises an intermediate water tank (10), a secondary lift pump (11), a reaction tank III (12), a reaction tank IV (13) and a three-stage clarification tank (14) arranged in sequence.
8. The zero emission treatment system of sintering wet desulphurization wastewater according to claim 7, characterized in that the reaction tank III (12) and the reaction tank IV (13) are both mechanical reaction tanks, and the tertiary clarifier (14) is a mechanical accelerated clarifier.
9. The zero emission treatment system of sintering wet desulfurization waste water according to claim 1, characterized in that the sewage post-treatment device comprises a post-pH adjusting tank (15), a reaction tank V (16), a water production tank (17) and a pressurizing pump (18) which are arranged in sequence.
10. The zero emission treatment system of sintering wet desulfurization waste water according to claim 1, characterized in that the sludge treatment device comprises a sludge concentration tank (19), a sludge adjustment tank (20), a mud pump (21) and a sludge dewatering machine (22) which are arranged in sequence.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110436671A (en) * | 2019-08-30 | 2019-11-12 | 中冶赛迪工程技术股份有限公司 | A kind of Zero discharge treatment method and system being sintered wet type desulfurizing waste water |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110436671A (en) * | 2019-08-30 | 2019-11-12 | 中冶赛迪工程技术股份有限公司 | A kind of Zero discharge treatment method and system being sintered wet type desulfurizing waste water |
| CN110436671B (en) * | 2019-08-30 | 2024-05-14 | 中冶赛迪工程技术股份有限公司 | Zero discharge treatment method and system for sintering wet desulfurization wastewater |
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