CN209537201U - High chlorine low-sulfur acid group waste water treatment system - Google Patents
High chlorine low-sulfur acid group waste water treatment system Download PDFInfo
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- CN209537201U CN209537201U CN201920188052.4U CN201920188052U CN209537201U CN 209537201 U CN209537201 U CN 209537201U CN 201920188052 U CN201920188052 U CN 201920188052U CN 209537201 U CN209537201 U CN 209537201U
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Abstract
The utility model discloses a kind of high chlorine low-sulfur acid group waste water treatment systems comprising conditioning tank, the first reaction tank, the first clarifying basin, the second reaction tank, the second clarifying basin, sludge concentrating pot, sand filter, evaporative crystallization unit, ozone reaction tank and dosing unit；The utility model structure simple device is few, and cost of investment is low, can effectively remove the SO in waste water4 2‑、Ca2+, COD and suspended matter etc., and the salinity contained in waste water is recycled；The utility model, which overcomes, only not only adjusts pH by addition lime, but also removes sulfate radical, so that lime consumption is big, the pH of waste water is caused constantly to increase, and subsequent and needs readjust pH by addition acid solution, causes acid solution dosage big, the high disadvantage of processing cost；The CO that decarbonizing tower is generated2It rationally and efficiently uses, reduces the dosage of sodium carbonate, saved cost, while reducing CO2Outer discharge capacity, be conducive to environmental protection.
Description
Technical field:
The utility model relates to field of waste water treatment more particularly to a kind of high chlorine low-sulfur acid group waste water treatment systems.
Background technique:
Coal chemical industry enterprises can generate a large amount of high chlorine low-sulfur acid group waste water in the process of running, due to current China's coal chemical industry
For the most centralized layout of project in the west area of ecological environment frailty, sewage body is not received on periphery, and it is direct not have such waste water
The condition of outlet, such waste water could be discharged externally after having to pass through processing, this gives such discharge of wastewater band of coal chemical industry enterprises
Many problems are carried out.
Currently, for such waste water processing mode mainly in such a way that nanofiltration divides salt；But using nanofiltration to such useless
When water is separated, concentrated water side still remains a large amount of chloride ions, divides salt ineffective, causes the waste of chloride ion.Meanwhile useless
In water treatment technology, decarbonizing tower can generate a large amount of CO2, due to there is no reasonable utilization mode, CO2Direct outlet processing, it is right
Environment causes great pollution.
Utility model content:
A kind of the purpose of this utility model is to provide structures simple, stable high chlorine low-sulfur acid group wastewater treatment system
System.
The utility model is implemented by following technical solution:
High chlorine low-sulfur acid group waste water treatment system comprising conditioning tank, the first reaction tank, the first clarifying basin, the second reaction
Pond, the second clarifying basin, sludge concentrating pot, sand filter, evaporative crystallization unit, ozone reaction tank and dosing unit；
The water inlet connection of the water outlet of the conditioning tank and first reaction tank, the water outlet of first reaction tank
It is connected to the water inlet of first clarifying basin, the water inlet of the water outlet of first clarifying basin and second reaction tank connects
Logical, the water outlet of second reaction tank is connected to the water inlet of second clarifying basin, the water outlet of second reaction tank
Be connected to the water inlet of the sand filter, the evaporation former pond of the water outlet of the sand filter and the evaporative crystallization unit into
Mouth of a river connection, the mother liquor outlet of the single effect evaporator of the evaporative crystallization unit are connected to the water inlet of the ozone reaction tank,
The water outlet of the ozone reaction tank is connected to the water inlet of the conditioning tank；The mud mouth of first clarifying basin and described
The mud mouth of two clarifying basins with the import connection of the sludge concentrating pot；
The feeding opening of the lime storage tank of the dosing unit and the medicine outlet end of calcium chloride storage tank with first reaction tank
Connection, the medicine outlet end of the coagulant storage tank of the dosing unit divide two-way respectively with the feeding opening of first clarifying basin and described
The feeding opening of second clarifying basin is connected to, and the medicine outlet end of the flocculant storage tank of the dosing unit divides two-way clear with described first respectively
The feeding opening in clear pond is connected to the feeding opening of second clarifying basin, the CO of the dosing unit2The aeration tube of storage tank is placed in institute
It states in the second reaction tank.
Further, the dosing unit include lime storage tank, calcium chloride storage tank, flocculant storage tank, coagulant storage tank with
And CO2Storage tank；
In the drug of the lime storage tank, the calcium chloride storage tank, the flocculant storage tank and the coagulant storage tank
End is equipped with valve；
In the CO2Blower is equipped in storage tank, the air outlet of the blower by pipeline and is placed in second reaction tank
Interior the aeration tube connection.
Further, the dosing unit further includes sodium carbonate storage tank, the medicine outlet end of the sodium carbonate storage tank and described the
The feeding opening of two reaction tanks is connected to.
Further, the evaporative crystallization unit includes evaporation former pond, single effect evaporator, thickener, centrifuge, drying
Bed and packing machine；
The water outlet of the evaporation former pond is connected to the water inlet of the single effect evaporator, the crystalline substance of the single effect evaporator
The magma outlet of the inlet communication of slurry outlet and the thickener, the thickener is connected to the entrance of the centrifuge, described
The inlet communication of the crystal salt outlet and the drying bed of centrifuge, the outlet of the drying bed connect with the import of the packing machine
It is logical.
It further, further include decarbonizing tower, the CO of the decarbonizing tower2Gas outlet and the CO2The air inlet of storage tank connects
It is logical.
The advantages of the utility model:
1, Tthe utility model system structure simple device is few, and cost of investment is low, first by the first reaction tank simultaneously
Lime and calcium chloride are added, to adjust the pH of waste water and remove the SO in waste water4 2-；In the first clarifying basin, in coagulant and wadding
Under the action of solidifying agent, calcium sulfate is settled, into sludge concentrating pot；It is added by way of aeration in the second reaction tank
CO2, to remove Ca2+；Work as CO2Amount it is inadequate when, then add sodium carbonate, equally reach removal Ca2+Effect；Second clarifying basin
Interior, under the action of coagulant and flocculant, calcium carbonate is settled, into sludge concentrating pot；Remove Ca2+Waste water afterwards is through sand
Filter enters evaporation former pond homogeneous average after removing the suspended matter in water removal, enters single effect evaporator later and is evaporated crystallization,
Sodium chloride crystal salt can be obtained；And the COD being enriched in evaporation mother liquor is removed by ozone reaction tank.Tthe utility model system
The SO in waste water can be effectively removed4 2-、Ca2+, COD and suspended matter etc., and the salinity contained in waste water is recycled.
2, Tthe utility model system, which overcomes, only not only adjusts pH by addition lime, but also removes sulfate radical, so that lime
Dosage is big, and the pH of waste water is caused constantly to increase, and subsequent and needs readjust pH by addition acid solution, leads to acid solution dosage
Greatly, the high disadvantage of processing cost.
3, the CO that Tthe utility model system generates decarbonizing tower2It rationally and efficiently uses, reduces the dosage of sodium carbonate, save
Cost, while reducing CO2Outer discharge capacity, be conducive to environmental protection.
4, the utility model is a kind of for chloride ion content is more and the disposition side for the haline water that sulfate radical content is less
Method is designed by the system in combination that two-stage reaction and two-stage settle, it is ensured that the long-period stable operation of subsequent evaporation crystalline element,
Crystal salt quality reaches the utilization of technical grade standard resourceization, while realizing the utmostly resource utilization of crystal salt, has one
Fixed economic benefit and social benefit.
Detailed description of the invention:
In order to illustrate the embodiment of the utility model or the technical proposal in the existing technology more clearly, below will be to embodiment
Or attached drawing needed to be used in the description of the prior art is briefly described, it should be apparent that, the accompanying drawings in the following description is only
It is some embodiments of the utility model, for those of ordinary skill in the art, in the premise not made the creative labor
Under, it is also possible to obtain other drawings based on these drawings.
Fig. 1 is the system structure diagram of embodiment 1；
In figure: conditioning tank 1, the first reaction tank 2, the first clarifying basin 3, the second reaction tank 4, the second clarifying basin 5, sludge condensation
Tank 6, evaporative crystallization unit 8, evaporation former pond 8-1, single effect evaporator 8-2, thickener 8-3, centrifuge 8-4, is done sand filter 7
Dry bed 8-5, packing machine 8-6, ozone reaction tank 9, dosing unit 10, lime storage tank 10-1, calcium chloride storage tank 10-2, flocculant storage
Tank 10-3, coagulant storage tank 10-4, CO2Storage tank 10-5, sodium carbonate storage tank 10-6, blower 10-7, aeration tube 10-8, decarbonizing tower
11。
Specific embodiment:
The following will be combined with the drawings in the embodiments of the present invention, carries out the technical scheme in the embodiment of the utility model
Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art are without making creative work
Every other embodiment obtained, fall within the protection scope of the utility model.
Embodiment 1:
High chlorine low-sulfur acid group waste water treatment system as shown in Figure 1 comprising conditioning tank 1, the first reaction tank 2, first are clear
Clear pond 3, the second reaction tank 4, the second clarifying basin 5, sludge concentrating pot 6, sand filter 7, evaporative crystallization unit 8, ozone reaction tank 9 with
And dosing unit 10；
The water inlet connection of the water outlet of conditioning tank 1 and the first reaction tank 2, the water outlet of the first reaction tank 2 and first clear
The water inlet connection in clear pond 3, the water outlet of the first clarifying basin 3 are connected to the water inlet of the second reaction tank 4, the second reaction tank 4
Water outlet is connected to the water inlet of the second clarifying basin 5, and the water outlet of the second reaction tank 4 is connected to the water inlet of sand filter 7, sand filtration
The water outlet of device 7 is connected to the water inlet of the evaporation former pond 8-1 of evaporative crystallization unit 8, the single effect evaporation of evaporative crystallization unit 8
The mother liquor outlet of device 8-2 is connected to the water inlet of ozone reaction tank 9, the water outlet of ozone reaction tank 9 and the water inlet of conditioning tank 1
Connection；Import connection of the mud mouth of the mud mouth of first clarifying basin 3 and the second clarifying basin 5 with sludge concentrating pot 6；
The medicine outlet end of the lime storage tank 10-1 and calcium chloride storage tank 10-2 of dosing unit 10 is with the first reaction tank 2 into medicine
Mouthful connection, the medicine outlet end of the coagulant storage tank 10-4 of dosing unit 10 divide two-way respectively with the feeding opening of the first clarifying basin 3 and the
The feeding opening of two clarifying basins 5 is connected to, and the medicine outlet end of the flocculant storage tank 10-3 of dosing unit 10 divides two-way to clarify respectively with first
The connection of the feeding opening of the feeding opening in pond 3 and the second clarifying basin 5, the CO of dosing unit 102The aeration tube 10-8 of storage tank 10-5 is placed in
In second reaction tank 4.
Dosing unit 10 includes lime storage tank 10-1, calcium chloride storage tank 10-2, flocculant storage tank 10-3, coagulant storage tank
10-4 and CO2Storage tank 10-5；
In the drug of lime storage tank 10-1, calcium chloride storage tank 10-2, flocculant storage tank 10-3 and coagulant storage tank 10-4
End is equipped with valve；
In CO2Blower 10-7 is equipped in storage tank 10-5, the air outlet of blower 10-7 by pipeline and is placed in the second reaction tank 4
Interior aeration tube 10-8 connection.
Dosing unit 10 further includes sodium carbonate storage tank 10-6, the medicine outlet end of sodium carbonate storage tank 10-6 and the second reaction tank 4
Feeding opening connection.
Evaporative crystallization unit 8 includes evaporation former pond 8-1, single effect evaporator 8-2, thickener 8-3, centrifuge 8-4, drying
Bed 8-5 and packing machine 8-6；
The water outlet of evaporation former pond 8-1 is connected to the water inlet of single effect evaporator 8-2, the magma of single effect evaporator 8-2
The magma outlet of the inlet communication of outlet and thickener 8-3, thickener 8-3 is connected to the entrance of centrifuge 8-4, centrifuge 8-4
Crystal salt outlet and the inlet communication of drying bed 8-5, the outlet of drying bed 8-5 and the inlet communication of packing machine 8-6.
The present embodiment further includes decarbonizing tower 11, the CO of decarbonizing tower 112Gas outlet and CO2The air inlet of storage tank 10-5 is connected to.
In the present embodiment, lime and calcium chloride are added simultaneously in the first reaction tank 2, the pH of waste water is adjusted in lime, and
Calcium chloride can remove the sulfate radical in waste water；It overcomes and pH is not only only adjusted by addition lime, but also remove sulfate radical, so that
Lime consumption is big, and the pH of waste water is caused constantly to increase, and subsequent and needs readjust pH by addition acid solution, and acid solution is caused to be used
Amount is big, and processing cost is high.
In the first clarifying basin 3, under the action of coagulant and flocculant, calcium sulfate is settled, into sludge condensation
Tank 6；In the second reaction tank 4, CO that on-site decarbonizing tower 11 is generated2It is added by way of aeration in the second reaction tank 4,
With residue Ca in waste water2+It reacts, generates precipitation of calcium carbonate；As the CO that decarbonizing tower 11 generates2Amount it is inadequate when, by carbonic acid
Sodium storage tank 10-6 adds sodium carbonate into the second reaction tank 4, and sodium carbonate equally can be with residue Ca in waste water2+It reacts, generates
Precipitation of calcium carbonate；The CO that the present embodiment generates decarbonizing tower 112It rationally and efficiently uses, reduces the dosage of sodium carbonate, save
Cost.
In the second clarifying basin 5, under the action of coagulant and flocculant, calcium carbonate is settled, into sludge condensation
Tank 6；Remove Ca2+Waste water afterwards enters evaporation former pond 8-1 homogeneous average after sand filter 7 removes the suspended matter in water removal, later
It is evaporated crystallization into single effect evaporator 8-2, sodium chloride crystal salt can be obtained；It is generated again because of single effect evaporator 8-2
COD enrichment in mother liquor is evaporated, therefore is additionally arranged ozone reaction tank 9 again to remove part COD, is guaranteed in the water being back in system
COD is in reduced levels, and then guarantees the water quality for going out salt quality and evaporation condensate of sodium chloride crystal salt.Sludge concentrating pot 6
It is outer again after sludge being concentrated to drain into sludge treating system, the sludge quantity of outlet can be reduced.
The industrial chlorinations sodium that this system generates reaches the dry salt one of highly industry in GB/T 5462-2015 " Nacl " standard
Grade standard can directly pack outer sell.
This system is a kind of for chloride ion content is more and the method for disposal for the haline water that sulfate radical content is less, is passed through
The system in combination design of two-stage reaction and two-stage sedimentation, it is ensured that the long-period stable operation of subsequent evaporation crystalline element 8, crystal salt
Quality reaches the utilization of technical grade standard resourceization, while realizing the utmostly resource utilization of crystal salt, has certain warp
Benefit of helping and social benefit.
Embodiment 2:
It using the technique of high chlorine low-sulfur acid group waste water treatment system described in embodiment 1, comprises the following steps: one acid of process
Alkali is adjusted；Two preliminary sedimentation of process；Process three is except hard；Four secondary settlement of process；Process five filters；Six evaporative crystallization of process；Work
Seven ozone oxidation of sequence；Eight sludge condensation of process；Wherein:
One acid-base accommodation of process: being 50000ppm by TDS in conditioning tank 1；Hardness is 5000ppm, Ca2+Concentration is
2000ppm；SO4 2-Concentration is 6000ppm；Cl-Concentration is 15000ppm；The waste water that pH is 7 is sent at supreme chlorine low-sulfur acid group waste water
In first reaction tank 2 of reason system, acid-base accommodation is carried out by addition lime, and by addition calcium chloride, make the portion in waste water
Divide calcium ion to precipitate in the form of calcium sulfate, remove sulfate radical, obtaining pH is 10.5, SO4 2-The adjusting that concentration is 2000ppm is useless
Water；
Two preliminary sedimentation of process: adjusting waste water obtained in one acid-base accommodation of process is sent at supreme chlorine low-sulfur acid group waste water
In first clarifying basin 3 of reason system, by addition coagulant and flocculant, and a supernatant and primary sludge are obtained；
Process three is except hard: sending a supernatant obtained in two preliminary sedimentation of process to supreme chlorine low-sulfur acid group wastewater treatment
In second reaction tank 4 of system, by exposing CO into the second reaction tank 42, make the remaining calcium ion in waste water with calcium carbonate
Form precipitating, can remove remaining calcium ion, obtains Ca2+Concentration is 15ppm except hard waste water；
Four secondary settlement of process: by process three except obtained in hard except hard waste water send supreme chlorine low-sulfur acid group wastewater treatment system
In second clarifying basin 5 of system, by addition coagulant and flocculant, and secondary supernatant and secondary sludge are obtained；
Process five filters: sending secondary supernatant obtained in four secondary settlement of process to supreme chlorine low-sulfur acid group wastewater treatment
Suspended matter in the sand filter 7 of system in removal waste water obtains the filtering that concentration of suspension is 0.8ppm and produces water；
Six evaporative crystallization of process: filtering obtained in the filtering of process five is produced into water and send supreme chlorine low-sulfur acid group wastewater treatment system
The single effect evaporator 8-2 of system is evaporated crystallization treatment, obtains sodium chloride crystal salt and evaporation mother liquor；
Seven ozone oxidation of process: evaporation mother liquor obtained in six evaporative crystallization of process is sent at supreme chlorine low-sulfur acid group waste water
Ozone Oxidation Treatment is carried out in the ozone reaction tank 9 of reason system, and the removal rate of COD is 50%, is obtained through ozone Oxidation Treatment
Production water be re-fed into conditioning tank 1 progress homogeneous average processing；
Eight sludge condensation of process；It will be obtained in four secondary settlement of primary sludge obtained in two preliminary sedimentation of process and process
Secondary sludge send supreme chlorine low-sulfur acid group waste water treatment system sludge concentrating pot 6 carry out sludge condensation processing, finally obtain
Thickened sludge be sent into sludge treating system handled.
In the present embodiment, process three is removed in hard, can also be made in waste water by adding sodium carbonate into the second reaction tank 4
Remaining calcium ion precipitates as calcium carbonate, can remove remaining calcium ion, obtains except hard waste water.
Embodiment 3:
It using the technique of high chlorine low-sulfur acid group waste water treatment system described in embodiment 1, comprises the following steps: one acid of process
Alkali is adjusted；Two preliminary sedimentation of process；Process three is except hard；Four secondary settlement of process；Process five filters；Six evaporative crystallization of process；Work
Seven ozone oxidation of sequence；Eight sludge condensation of process；Wherein:
One acid-base accommodation of process: being 55000ppm by TDS in conditioning tank 1；Hardness is 5500ppm, Ca2+Concentration is
2500ppm；SO4 2-Concentration is 8000ppm；Cl-Concentration is 17000ppm；The waste water that pH is 7.5 send supreme chlorine low-sulfur acid group waste water
In first reaction tank 2 of processing system, acid-base accommodation is carried out by addition lime, and by addition calcium chloride, make in waste water
Part calcium ion is precipitated in the form of calcium sulfate, removes sulfate radical, and obtaining pH is 11, SO4 2-The adjusting that concentration is 2500ppm is useless
Water；
Two preliminary sedimentation of process: adjusting waste water obtained in one acid-base accommodation of process is sent at supreme chlorine low-sulfur acid group waste water
In first clarifying basin 3 of reason system, by addition coagulant and flocculant, and a supernatant and primary sludge are obtained；
Process three is except hard: sending a supernatant obtained in two preliminary sedimentation of process to supreme chlorine low-sulfur acid group wastewater treatment
In second reaction tank 4 of system, by exposing CO into the second reaction tank 42, make the remaining calcium ion in waste water with calcium carbonate
Form precipitating, can remove remaining calcium ion, obtains Ca2+Concentration is 17ppm except hard waste water；
Four secondary settlement of process: by process three except obtained in hard except hard waste water send supreme chlorine low-sulfur acid group wastewater treatment system
In second clarifying basin 5 of system, by addition coagulant and flocculant, and secondary supernatant and secondary sludge are obtained；
Process five filters: sending secondary supernatant obtained in four secondary settlement of process to supreme chlorine low-sulfur acid group wastewater treatment
Suspended matter in the sand filter 7 of system in removal waste water obtains the filtering that concentration of suspension is 0.9ppm and produces water；
Six evaporative crystallization of process: filtering obtained in the filtering of process five is produced into water and send supreme chlorine low-sulfur acid group wastewater treatment system
The single effect evaporator 8-2 of system is evaporated crystallization treatment, obtains sodium chloride crystal salt and evaporation mother liquor；
Seven ozone oxidation of process: evaporation mother liquor obtained in six evaporative crystallization of process is sent at supreme chlorine low-sulfur acid group waste water
Ozone Oxidation Treatment is carried out in the ozone reaction tank 9 of reason system, and the removal rate of COD is 50%, is obtained through ozone Oxidation Treatment
Production water be re-fed into conditioning tank 1 progress homogeneous average processing；
Eight sludge condensation of process；It will be obtained in four secondary settlement of primary sludge obtained in two preliminary sedimentation of process and process
Secondary sludge send supreme chlorine low-sulfur acid group waste water treatment system sludge concentrating pot 6 carry out sludge condensation processing, finally obtain
Thickened sludge be sent into sludge treating system handled.
In the present embodiment, process three is removed in hard, can also be made in waste water by adding sodium carbonate into the second reaction tank 4
Remaining calcium ion precipitates as calcium carbonate, can remove remaining calcium ion, obtains except hard waste water.
Embodiment 4:
It using the technique of high chlorine low-sulfur acid group waste water treatment system described in embodiment 1, comprises the following steps: one acid of process
Alkali is adjusted；Two preliminary sedimentation of process；Process three is except hard；Four secondary settlement of process；Process five filters；Six evaporative crystallization of process；Work
Seven ozone oxidation of sequence；Eight sludge condensation of process；Wherein:
One acid-base accommodation of process: being 60000ppm by TDS in conditioning tank 1；Hardness is 6000ppm, Ca2+Concentration is
3000ppm；SO4 2-Concentration is 9000；Cl-Concentration is 20000ppm；The waste water that pH is 8 send supreme chlorine low-sulfur acid group wastewater treatment
In first reaction tank 2 of system, acid-base accommodation is carried out by addition lime, and by addition calcium chloride, make the part in waste water
Calcium ion is precipitated in the form of calcium sulfate, removes sulfate radical, and obtaining pH is 11.5, SO4 2-Concentration is the adjusting waste water of 3000ppm；
Two preliminary sedimentation of process: adjusting waste water obtained in one acid-base accommodation of process is sent at supreme chlorine low-sulfur acid group waste water
In first clarifying basin 3 of reason system, by addition coagulant and flocculant, and a supernatant and primary sludge are obtained；
Process three is except hard: sending a supernatant obtained in two preliminary sedimentation of process to supreme chlorine low-sulfur acid group wastewater treatment
In second reaction tank 4 of system, by exposing CO into the second reaction tank 42, make the remaining calcium ion in waste water with calcium carbonate
Form precipitating, can remove remaining calcium ion, obtains Ca2+Concentration is 20ppm except hard waste water；
Four secondary settlement of process: by process three except obtained in hard except hard waste water send supreme chlorine low-sulfur acid group wastewater treatment system
In second clarifying basin 5 of system, by addition coagulant and flocculant, and secondary supernatant and secondary sludge are obtained；
Process five filters: sending secondary supernatant obtained in four secondary settlement of process to supreme chlorine low-sulfur acid group wastewater treatment
Suspended matter in the sand filter 7 of system in removal waste water obtains the filtering that concentration of suspension is 1ppm and produces water；
Six evaporative crystallization of process: filtering obtained in the filtering of process five is produced into water and send supreme chlorine low-sulfur acid group wastewater treatment system
The single effect evaporator 8-2 of system is evaporated crystallization treatment, obtains sodium chloride crystal salt and evaporation mother liquor；
Seven ozone oxidation of process: evaporation mother liquor obtained in six evaporative crystallization of process is sent at supreme chlorine low-sulfur acid group waste water
Ozone Oxidation Treatment is carried out in the ozone reaction tank 9 of reason system, and the removal rate of COD is 50%, is obtained through ozone Oxidation Treatment
Production water be re-fed into conditioning tank 1 progress homogeneous average processing；
Eight sludge condensation of process；It will be obtained in four secondary settlement of primary sludge obtained in two preliminary sedimentation of process and process
Secondary sludge send supreme chlorine low-sulfur acid group waste water treatment system sludge concentrating pot 6 carry out sludge condensation processing, finally obtain
Thickened sludge be sent into sludge treating system handled.
In the present embodiment, process three is removed in hard, can also be made in waste water by adding sodium carbonate into the second reaction tank 4
Remaining calcium ion precipitates as calcium carbonate, can remove remaining calcium ion, obtains except hard waste water.
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Within the spirit and principle of utility model, any modification, equivalent replacement, improvement and so on should be included in the utility model
Protection scope within.
Claims (5)
1. high chlorine low-sulfur acid group waste water treatment system, which is characterized in that it include conditioning tank, the first reaction tank, the first clarifying basin,
Second reaction tank, the second clarifying basin, sludge concentrating pot, sand filter, evaporative crystallization unit, ozone reaction tank and dosing unit；
The water inlet connection of the water outlet of the conditioning tank and first reaction tank, the water outlet of first reaction tank and institute
The water inlet connection of the first clarifying basin is stated, the water outlet of first clarifying basin is connected to the water inlet of second reaction tank,
The water outlet of second reaction tank is connected to the water inlet of second clarifying basin, the water outlet of second reaction tank and institute
State the water inlet connection of sand filter, the water inlet of the water outlet of the sand filter and the evaporation former pond of the evaporative crystallization unit
Connection, the mother liquor outlet of the single effect evaporator of the evaporative crystallization unit is connected to the water inlet of the ozone reaction tank, described
The water outlet of ozone reaction tank is connected to the water inlet of the conditioning tank；The mud mouth of first clarifying basin and described second clear
The mud mouth in clear pond with the import connection of the sludge concentrating pot；
The lime storage tank of the dosing unit and the medicine outlet end of calcium chloride storage tank are connected to the feeding opening of first reaction tank,
The medicine outlet end of the coagulant storage tank of the dosing unit divide two-way respectively with the feeding opening of first clarifying basin and described second
The feeding opening of clarifying basin is connected to, the medicine outlet end of the flocculant storage tank of the dosing unit divide two-way respectively with first clarifying basin
Feeding opening be connected to the feeding opening of second clarifying basin, the CO of the dosing unit2The aeration tube of storage tank is placed in described
In two reaction tanks.
2. high chlorine low-sulfur acid group waste water treatment system according to claim 1, which is characterized in that the dosing unit includes
Lime storage tank, calcium chloride storage tank, flocculant storage tank, coagulant storage tank and CO2Storage tank；
It is equal in the medicine outlet end of the lime storage tank, the calcium chloride storage tank, the flocculant storage tank and the coagulant storage tank
Equipped with valve；
In the CO2Blower is equipped in storage tank, the air outlet of the blower passes through pipeline and the institute being placed in second reaction tank
State aeration tube connection.
3. high chlorine low-sulfur acid group waste water treatment system according to claim 2, which is characterized in that the dosing unit also wraps
Sodium carbonate storage tank is included, the medicine outlet end of the sodium carbonate storage tank is connected to the feeding opening of second reaction tank.
4. high chlorine low-sulfur acid group waste water treatment system according to claim 1, which is characterized in that the evaporative crystallization unit
Including evaporation former pond, single effect evaporator, thickener, centrifuge, drying bed and packing machine；
The water outlet of the evaporation former pond is connected to the water inlet of the single effect evaporator, and the magma of the single effect evaporator goes out
The magma outlet of the inlet communication of mouth and the thickener, the thickener is connected to the entrance of the centrifuge, the centrifugation
The inlet communication of the crystal salt outlet and the drying bed of machine, the outlet of the drying bed and the inlet communication of the packing machine.
5. high chlorine low-sulfur acid group waste water treatment system according to claim 1, which is characterized in that it further includes decarbonizing tower,
The CO of the decarbonizing tower2Gas outlet and the CO2The air inlet of storage tank is connected to.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920188052.4U CN209537201U (en) | 2019-02-01 | 2019-02-01 | High chlorine low-sulfur acid group waste water treatment system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920188052.4U CN209537201U (en) | 2019-02-01 | 2019-02-01 | High chlorine low-sulfur acid group waste water treatment system |
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| Publication Number | Publication Date |
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| CN209537201U true CN209537201U (en) | 2019-10-25 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113185037A (en) * | 2021-06-08 | 2021-07-30 | 金川集团股份有限公司 | System and method for removing calcium in non-ferrous metal smelting wastewater |
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2019
- 2019-02-01 CN CN201920188052.4U patent/CN209537201U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113185037A (en) * | 2021-06-08 | 2021-07-30 | 金川集团股份有限公司 | System and method for removing calcium in non-ferrous metal smelting wastewater |
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