CN110342710A - High chlorine low-sulfur acid group waste water treatment system and its technique - Google Patents
High chlorine low-sulfur acid group waste water treatment system and its technique Download PDFInfo
- Publication number
- CN110342710A CN110342710A CN201910107810.XA CN201910107810A CN110342710A CN 110342710 A CN110342710 A CN 110342710A CN 201910107810 A CN201910107810 A CN 201910107810A CN 110342710 A CN110342710 A CN 110342710A
- Authority
- CN
- China
- Prior art keywords
- waste water
- reaction tank
- acid group
- storage tank
- sulfur acid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention 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；Present system 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 invention also discloses a kind of high chlorine low-sulfur acid group waste water treatment process, comprise the following steps: one acid-base accommodation of process；Two preliminary sedimentation of process；Process three is except hard；Four secondary settlement of process；Process five filters；Six evaporative crystallization of process；Seven ozone oxidation of process；Eight sludge condensation of process；This system technique be it 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, it can be achieved that crystal salt utmostly resource utilization, have certain economic benefit and social benefit.
Description
Technical field:
The present invention relates to field of waste water treatment more particularly to a kind of high chlorine low-sulfur acid group waste water treatment system and its techniques.
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.
Summary of the invention:
The first purpose of this invention is to provide the high chlorine low-sulfur acid group wastewater treatment that a kind of structure is simple, stable
System；
Second object of the present invention is that providing the high chlorine low-sulfur acid group that a kind of technique is simplified, salinity recovering effect is good gives up
Water treatment technology；
The first purpose of this invention 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.
Second object of the present invention is implemented by following technical solution:
High chlorine low-sulfur acid group waste water treatment process, comprises the following steps: one acid-base accommodation of process；Two preliminary sedimentation of process；
Process three is except hard；Four secondary settlement of process；Process five filters；Six evaporative crystallization of process；Seven ozone oxidation of process；Eight sludge of process
Concentration；Wherein:
One acid-base accommodation of process: by TDS >=50000ppm in conditioning tank；Water inlet hardness >=5000ppm, Ca2+≥
2000ppm；SO4 2-Concentration is in 6000~10000ppm；Cl-Waste water of the concentration between 15000~20000ppm send supreme chlorine low
In first reaction tank of sulfate radical waste water treatment system, acid-base accommodation is carried out by addition lime, and by addition calcium chloride, make
Part calcium ion in waste water is precipitated in the form of calcium sulfate, removes sulfate radical, obtains adjusting waste water；
Two preliminary sedimentation of process: adjusting waste water obtained in one acid-base accommodation of process is sent to supreme chlorine low-sulfur acid
In first clarifying basin of root waste water treatment system, by addition coagulant and flocculant, and a supernatant and primary dirt are obtained
Mud；
The process three is except hard: sending a supernatant obtained in two preliminary sedimentation of process to supreme chlorine low-sulfur acid group
In second reaction tank of waste water treatment system, by exposing CO into second reaction tank2, make the remaining calcium ion in waste water
It precipitates as calcium carbonate, can remove remaining calcium ion, obtain except hard waste water；
Four secondary settlement of process: by the process three except obtained in hard except hard waste water send supreme chlorine low-sulfur acid group to give up
In second clarifying basin of water treatment system, by addition coagulant and flocculant, and secondary supernatant and secondary sludge are obtained；
The process five filters: sending secondary supernatant obtained in four secondary settlement of process to supreme chlorine low-sulfur acid group
Suspended matter in the sand filter of waste water treatment system in removal waste water obtains filtering and produces water；
Six evaporative crystallization of process: filtering obtained in the process five filtering is produced into water, supreme chlorine low-sulfur acid group is sent to give up
The single effect evaporator of water treatment 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 to supreme chlorine low-sulfur acid
Ozone Oxidation Treatment is carried out in the ozone reaction tank of root waste water treatment system, the production water obtained through ozone Oxidation Treatment is re-fed into institute
State progress homogeneous average processing in conditioning tank；
Eight sludge condensation of process；By primary sludge and the process four or two obtained in two preliminary sedimentation of process
Secondary sludge obtained in secondary sedimentation send the sludge concentrating pot of supreme chlorine low-sulfur acid group waste water treatment system to carry out at sludge condensation
Reason, finally obtained thickened sludge are sent into sludge treating system and are handled.
Further, the process three is removed in hard, by adding sodium carbonate into second reaction tank, is made in waste water
Remaining calcium ion precipitates as calcium carbonate, can remove remaining calcium ion, obtains except hard waste water.
Advantages of the present invention:
1, present system structure simple device is few, and cost of investment is low, first by adding simultaneously in the first reaction tank
Lime and calcium chloride, to adjust the pH of waste water and remove the SO in waste water4 2-；In the first clarifying basin, in coagulant and flocculant
Under the action of, calcium sulfate settles, into sludge concentrating pot；CO is added by way of aeration in the second reaction tank2, come
Remove Ca2+；Work as CO2Amount it is inadequate when, then add sodium carbonate, equally reach removal Ca2+Effect；In second clarifying basin, mixed
Under the action of solidifying agent and flocculant, calcium carbonate is settled, into sludge concentrating pot；Remove Ca2+Waste water afterwards is gone through sand filter
Enter evaporation former pond homogeneous average after suspended matter in water removal, enters single effect evaporator later and be evaporated crystallization, can obtain
To sodium chloride crystal salt；And the COD being enriched in evaporation mother liquor is removed by ozone reaction tank.Present system can effectively remove
SO in waste water4 2-、Ca2+, COD and suspended matter etc., and the salinity contained in waste water is recycled.
2, present system, which overcomes, only not only adjusts pH by addition lime, but also removes sulfate radical, so that lime consumption
Greatly, the pH of waste water is caused constantly to increase, subsequent and needs readjust pH by addition acid solution, cause acid solution dosage big, locate
Manage costly disadvantage.
3, the CO that present system generates decarbonizing tower2Rationally and efficiently use, reduce the dosage of sodium carbonate, saved at
This, while reducing CO2Outer discharge capacity, be conducive to environmental protection.
4, this system technique 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 more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
Some embodiments of invention for those of ordinary skill in the art without creative efforts, can be with
It obtains 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:
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
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 foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (7)
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.
6. handling high chlorine low-sulfur acid group waste water using any high chlorine low-sulfur acid group waste water treatment system of claim 1-5
Technique, which is characterized in that comprise the following steps: one acid-base accommodation of process；Two preliminary sedimentation of process；Process three is except hard；Process four
Secondary settlement；Process five filters；Six evaporative crystallization of process；Seven ozone oxidation of process；Eight sludge condensation of process；Wherein:
One acid-base accommodation of process: by TDS >=50000ppm in conditioning tank；Water inlet hardness >=5000ppm, Ca2+≥
2000ppm；SO4 2-Concentration is in 6000~10000ppm；Cl-Waste water of the concentration between 15000~20000ppm send supreme chlorine low
In first reaction tank of sulfate radical waste water treatment system, acid-base accommodation is carried out by addition lime, and by addition calcium chloride, make
Part calcium ion in waste water is precipitated in the form of calcium sulfate, removes sulfate radical, obtains adjusting waste water；
Two preliminary sedimentation of process: supreme chlorine low-sulfur acid group is sent to give up adjusting waste water obtained in one acid-base accommodation of process
In first clarifying basin of water treatment system, by addition coagulant and flocculant, and a supernatant and primary sludge are obtained；
The process three is except hard: sending a supernatant obtained in two preliminary sedimentation of process to supreme chlorine low-sulfur acid group waste water
In second reaction tank of processing system, by exposing CO into second reaction tank2, make the remaining calcium ion in waste water with carbon
The form of sour calcium precipitates, and can remove remaining calcium ion, obtains except hard waste water；
Four secondary settlement of process: by the process three except obtained in hard except hard waste water is sent at supreme chlorine low-sulfur acid group waste water
In second clarifying basin of reason system, by addition coagulant and flocculant, and secondary supernatant and secondary sludge are obtained；
The process five filters: sending secondary supernatant obtained in four secondary settlement of process to supreme chlorine low-sulfur acid group waste water
Suspended matter in the sand filter of processing system in removal waste water obtains filtering and produces water；
Six evaporative crystallization of process: filtering obtained in the process five filtering is produced into water and is sent at supreme chlorine low-sulfur acid group waste water
The single effect evaporator of reason system is evaporated crystallization treatment, obtains sodium chloride crystal salt and evaporation mother liquor；
Seven ozone oxidation of process: supreme chlorine low-sulfur acid group is sent to give up in evaporation mother liquor obtained in six evaporative crystallization of process
Ozone Oxidation Treatment is carried out in the ozone reaction tank of water treatment system, the production water obtained through ozone Oxidation Treatment is re-fed into the tune
It saves and carries out homogeneous average processing in pond；
Eight sludge condensation of process；Primary sludge obtained in two preliminary sedimentation of process and the process four or two times is heavy
Secondary sludge obtained in drop send the sludge concentrating pot of supreme chlorine low-sulfur acid group waste water treatment system to carry out sludge condensation processing, most
The thickened sludge obtained eventually is sent into sludge treating system and is handled.
7. high chlorine low-sulfur acid group waste water treatment system treatment process according to claim 6, which is characterized in that the process
Three remove in hard, by adding sodium carbonate into second reaction tank, make the remaining calcium ion in waste water with the shape of calcium carbonate
Formula precipitating, can remove remaining calcium ion, obtain except hard waste water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910107810.XA CN110342710A (en) | 2019-02-01 | 2019-02-01 | High chlorine low-sulfur acid group waste water treatment system and its technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910107810.XA CN110342710A (en) | 2019-02-01 | 2019-02-01 | High chlorine low-sulfur acid group waste water treatment system and its technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110342710A true CN110342710A (en) | 2019-10-18 |
Family
ID=68173834
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910107810.XA Withdrawn CN110342710A (en) | 2019-02-01 | 2019-02-01 | High chlorine low-sulfur acid group waste water treatment system and its technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110342710A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110697983A (en) * | 2019-10-23 | 2020-01-17 | 绍兴市上虞众联环保有限公司 | Leachate treatment process |
| CN113024080A (en) * | 2021-03-05 | 2021-06-25 | 北京科技大学 | Full-tailing slurry two-section type continuous, rapid and deep dewatering system |
-
2019
- 2019-02-01 CN CN201910107810.XA patent/CN110342710A/en not_active Withdrawn
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110697983A (en) * | 2019-10-23 | 2020-01-17 | 绍兴市上虞众联环保有限公司 | Leachate treatment process |
| CN113024080A (en) * | 2021-03-05 | 2021-06-25 | 北京科技大学 | Full-tailing slurry two-section type continuous, rapid and deep dewatering system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101746874B (en) | Processing method of wastewater desulfurized by fume wet method | |
| CN110040878B (en) | Advanced treatment method for fluorine-containing wastewater | |
| CN105384316B (en) | A kind of processing method of the fluorine-containing nitrogen-containing wastewater of electronics industry | |
| CN204824453U (en) | Desulfurization pretreatment of water device that gives up | |
| CN104418445A (en) | Treatment method of heavy metal sewage | |
| CN106630343B (en) | A kind of method for treating desulfurized wastewater and system | |
| CN105800846A (en) | Method used for reverse osmosis concentrated water treatment and zero discharge, and apparatus thereof | |
| CN113003846A (en) | Zero-emission treatment process and system for sewage with high salt content and high COD (chemical oxygen demand) | |
| CN107176726A (en) | Desulphurization for Coal-fired Power Plant waste water integrates defluorination method | |
| CN111217484A (en) | Desulfurization wastewater recycling treatment method | |
| JP4693128B2 (en) | Phosphorus recovery method and phosphorus recovery system | |
| CN110316897A (en) | A kind of system and method for the full factory waste water zero discharge of power plant and resource utilization | |
| CN107055885B (en) | Desulfurization wastewater recycling system of coal-fired power plant and working method | |
| CN113003845B (en) | Zero-emission treatment process and system for sewage with high sulfate content and high COD (chemical oxygen demand) | |
| CN106746108A (en) | A kind of desulfurization wastewater recycling treatment system and method | |
| CN110342710A (en) | High chlorine low-sulfur acid group waste water treatment system and its technique | |
| CN107935255A (en) | A kind of processing method of the desulfurization wastewater of near-zero release | |
| CN209537201U (en) | High chlorine low-sulfur acid group waste water treatment system | |
| CN107055886B (en) | A kind of depth graded divides salt technique | |
| CN111099773A (en) | Desulfurization wastewater treatment method and system | |
| CN112573720A (en) | Thermal power plant desulfurization wastewater zero-discharge system and method | |
| CN108529788A (en) | A kind of purification method and device of waste liquid from bromine extraction | |
| CN209259867U (en) | Water treatment system with high salt | |
| JP2002205077A (en) | Method and apparatus for treating organic sewage | |
| CN207451807U (en) | Desulphurization for Coal-fired Power Plant waste water integrates fluoride-removing equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: Room 803, Gaoxin building, Ordos hi tech Industrial Park, Inner Mongolia Autonomous Region Applicant after: Inner Mongolia Jingtai environmental science and Technology Co., Ltd. Address before: Room 1008, Headquarters Base of Cloud Computing Big Data Enterprises, Ordos High-tech Industrial Park, Inner Mongolia Autonomous Region Applicant before: Inner Mongolia Jingtai environmental science and Technology Co., Ltd. |
|
| CB02 | Change of applicant information | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20191018 |
|
| WW01 | Invention patent application withdrawn after publication |