CN204779206U - High COD evaporation of water crystallization zero release processing system that gives up - Google Patents
High COD evaporation of water crystallization zero release processing system that gives up Download PDFInfo
- Publication number
- CN204779206U CN204779206U CN201520438025.XU CN201520438025U CN204779206U CN 204779206 U CN204779206 U CN 204779206U CN 201520438025 U CN201520438025 U CN 201520438025U CN 204779206 U CN204779206 U CN 204779206U
- Authority
- CN
- China
- Prior art keywords
- crystallizer
- treatment system
- water
- mother liquor
- vaporizer
- 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.)
- Expired - Fee Related
Links
Abstract
The utility model discloses a high COD evaporation of water crystallization zero release processing system that gives up, it includes pre -heater, evaporimeter, crystallizer, centrifuge and mother liquor tank, wherein: the water inlet of pre -heater and delivery port link to each other with the water inlet of waste water raw water and evaporimeter respectively, and the concentrate that the evaporimeter evaporation produced enters into the crystallizer, and the magma that the crystallizer produced enters into centrifuge, and the mother liquor that centrifuge centrifugation produced returns to the crystallizer through mother liquor tank, and crystallization salt that the separation produced is outer to be arranged or retrieve, processing system includes still that one gets rid of COD's in the waste water quenching and tempering unit through electric catalytic oxidation, the quenching and tempering unit locate between the water inlet of delivery port and the evaporimeter of pre -heater or the water inlet of the concentrate delivery port of locating the evaporimeter and crystallizer between perhaps locate between the water inlet of mother liquor tank's delivery port and crystallizer. The utility model provides a processing system can really realize the zero release under the prerequisite of long -term, steady operation.
Description
Technical field
The utility model relates to a kind of Waste Water Treatment, be specifically related to a kind of can the waste water evaporative crystallization zero-discharge treatment system of resistance to high COD, belong to environment-protective water process field.
Background technology
Along with the proposition of wastewater treatment " zero release " concept, evaporative crystallization technique is widely applied to brine waste process field.At present, brine waste mainly adopts the technique of pre-treatment+membrane concentration+evaporative crystallization to process.As the end step of wastewater treatment, evaporative crystallization steps mainly adopts mechanical vapor recompression technology and multiple-effect evaporation technology.
Apply to some extent in above-mentioned technology waste-water treatment project at home, and also have a certain amount of engineering achievement for the process of high-COD waste water, but mostly there is following problem when running in it: 1, there is a certain amount of high dense mother liquor and arrange outward, can not accomplish real zero release; 2, in gained crystal salt, organic content is high, can not reclaim and utilize; 3, outer row's mother liquor, high COD crystal salt are that solid waste or danger are useless, and need do further process, intractability is large, costly; 4, existing evaporative crystallizer is made up of a large amount of heat-exchange equipments, and in waste water, organic existence and accumulation cause the heat exchange efficiency of heat-exchange equipment to reduce, and energy consumption increases; 5, in waste water, organic existence and accumulation also add the difficulty of salt cleaning in crystallizer.Therefore, waste water evaporative crystallization zero-discharge treatment system and the method for developing a kind of resistance to high COD are very necessary.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art, provides a kind of evaporative crystallization treatment system of high-COD waste water, under the prerequisite of long-term, steady running, really can realize zero release.
For achieving the above object, the utility model is by the following technical solutions:
A kind of evaporative crystallization zero-discharge treatment system of high-COD waste water, it comprises preheater, vaporizer, crystallizer, separating centrifuge and mother liquor tank, wherein: the water-in of the water inlet of described preheater and water outlet water former in waste water and vaporizer is respectively connected, the concentrated solution that evaporator evaporation produces enters into crystallizer, the magma that crystallizer crystallization produces enters into separating centrifuge, the mother liquor that separating centrifuge centrifugation produces is back in crystallizer through mother liquor tank, be separated the crystal salt produced arrange outward or reclaim, described treatment system also comprises one to remove COD in waste water modified unit by catalytic oxidation.
Preferably: according to the difference of waste water quality, as the TDS > 10000mg/L in waste water, COD > 1000mg/L, described modified unit is located between the water outlet of preheater and the water-in of vaporizer.
Preferably: as the TDS > 5000mg/L in waste water, 1000mg/L > COD > 100mg/L, described modified unit is located between the concentrated solution water outlet of vaporizer and the water inlet of crystallizer.
Preferably: as the TDS > 5000mg/L in waste water, COD < 100mg/L, described modified unit is located between the water outlet of mother liquor tank and the water inlet of crystallizer.
Preferably: described modified unit comprises modified tank and one or more groups modified electrode group be arranged in parallel, and often organizes modified electrode group and comprises one or more modified electrode be arranged in series.
Preferably: described modified electrode is diamond alloy electrode.
Preferably: described treatment system comprises condensate drum, the phlegma that vaporizer and crystallizer produce is back in preheater with after the former water heat exchange in preheater through condensate drum to be arranged outward.
Preferably: described preheater is any one in tube and shell heat exchanger, double-pipe exchanger, plate-type heat exchanger.
Preferably: described separating centrifuge is horizontal centrifugal separating machine; Described vaporizer and crystallizer are multiple-effect evaporator or mechanically compress evaporating vaporizer again.
Preferably: described treatment system can use in multiple series connection.
The beneficial effects of the utility model are, compared with existing evaporative crystallization technique, the evaporative crystallization treatment system of the application can reduce or even organics removal on the impact of evaporation crystallization equipment itself and product, and, 1) treatment system of the present utility model is adopted, arrange outward without mother liquor, " near zero release " is promoted to real zero release; 2) be separated organic content in the crystal salt obtained, lower than 0.1%, can directly reclaim and utilize; 3) in whole treating processes, do not produce any waste gas, waste liquid, give up admittedly, non-secondary pollution; 4) equipment is without organism attachment and accumulation, and pre-thermo-efficiency is high; 5) cleanliness efficiency of crystallizer is high; 6) whole evaporation and crystallization system can for a long time, steady running.
Accompanying drawing explanation
Fig. 1 shows the structural representation for the treatment of system described in the utility model;
Fig. 2 shows the structural representation under the another kind of embodiment for the treatment of system described in the utility model;
Fig. 3 shows the structural representation under another embodiment for the treatment of system described in the utility model;
Fig. 4 shows the structural representation of modulator described in the utility model.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described further.
As shown in Figure 1, treatment system described in the utility model, comprise preheater 1, vaporizer 3, crystallizer 4, separating centrifuge 5 and condensate drum 2 and mother liquor tank 6, wherein: the water inlet of described preheater 1 and former aqueous phase connect, its water outlet is entered in vaporizer 3 by pipeline carries out heat exchange evaporation, the phlegma that evaporation is formed enters into condensate drum 2, and the concentrated solution that evaporation produces enters into crystallizer 4 through concentrated solution outlet and carries out circulation crystallization, the phlegma that described crystallizer 4 circulation crystallization produces also is collected in condensate drum 2 by pipeline, in the utility model, the phlegma coming flash-pot 3 and crystallizer 4 collected in condensate drum 2 can enter in preheater 1 with after the former water heat exchange in preheater 1 and arrange outward under the castering action of pump, the magma that crystallizer 4 circulation crystallization produces enters into separating centrifuge 5 carry out centrifugation through the magma outlet of crystallizer 4, the mother liquor that centrifugation produces enters into mother liquor tank 6, and can be back in crystallizer 4 under the effect of pump and carry out circulation crystallization, the crystal salt that separating centrifuge 5 centrifugation produces can arrange outward or reclaim.Further, as the TDS > 10000mg/L in waste water, COD > 1000mg/L, treatment system described in the utility model also can comprise to be located between preheater 1 and vaporizer 3, for removing the modified unit 7 of COD in waste water, and the waste water after preheater 1 pre-heating temperature elevation is introduced in modified 7 removal waste water to enter in vaporizer 3 after COD again and carries out evaporating and subsequent disposal.
Or, according to another kind of embodiment of the present utility model, as the TDS > 5000mg/L in waste water, 1000mg/L > COD > 100mg/L, as shown in Figure 2, described modified unit 7 also can be located between the concentrated solution water outlet of vaporizer 3 and the water inlet of crystallizer 4, and vaporizer 3 enters crystallizer 4 again after evaporating the first COD removed through modified unit 7 in concentrated solution of the concentrated solution produced and carries out circulation crystallization.
Again or, according to another embodiment of the present utility model, as the TDS > 5000mg/L in waste water, COD < 100mg/L, as shown in Figure 3, described modified unit 7 also can be located between the water outlet of mother liquor tank 6 and the water inlet of crystallizer 5, and the mother liquor in mother liquor tank 6 is back in crystallizer 4 first remove the COD in magma through modified unit 7 after again and carries out circulation crystallization.
As shown in Figure 4, described modified unit 7 comprises modified tank 71 and is arranged at a group or two groups and the modified electrode group 72 be arranged in parallel more than two of modified tank 71 outside, often organize modified electrode group 72 and comprise one or more modified electrode be arranged in series, in the utility model, described modified electrode preferably can various organic diamond alloy electrode (BDD electrode) in the oxidized waste water of non-selectivity, the water inlet of waste water bottom modified tank 71 enters in modified tank 71, modified electrode produces hydroxyl radical free radical under electric field action, organism in waste water and ammonia nitrogen pollutant are oxidized to carbonic acid gas by hydroxyl radical free radical, nitrogen G&W, thus the effect of the COD reached in degrading waste water and ammonia nitrogen pollutant, its essence is a kind of catalytic oxidation process, and meeting release of heat in modified electrode operation, the modified electrode of separate unit can make wastewater temperature raise 3-4 DEG C, waste water is continuous circular treatment in modified unit 7, until after waste water COD < 100mg/l in modified tank 71, the water outlet of waste water after modified anodizing through modified tank 71 top is discharged modified tank 71 and is entered next treatment process.
As preferred embodiment, in the utility model, described preheater 1 can adopt tube and shell heat exchanger, double-pipe exchanger or plate-type heat exchanger, described separating centrifuge 5 can adopt horizontal centrifugal separating machine, described vaporizer 3 and crystallizer 4 can adopt identical structure, as multiple-effect evaporator, mechanically compress is evaporating vaporizer (MVR vaporizer) etc. again, preferred MVR vaporizer, it utilizes the import fans in series of two same sizes or the domestic compressor compresses secondary steam of separate unit to reach the evaporation temperature difference of needs, vaporizer falling liquid film unit is divided into two effects to reduce the energy consumption of blower fan, the thermal source that the secondary steam that falling liquid film one imitates generation is imitated as falling liquid film two, the secondary steam that film two is imitated is entered first step blower fan/compressor, the secondary steam liquid of crystallizer enters first step blower fan/compressor.In addition, treatment system described in the utility model also comprises connecting pipe for connecting each equipment and recycle pump.Further, treatment system of the present utility model can use, with lifting waste water processing efficiency in multiple series connection.
Adopt the utility model treatment system as above to process high-COD waste water, its treatment step comprises:
1) brine waste of 20-30 DEG C enters vaporizer 3 and evaporates after preheater 1 pre-heating temperature elevation is to 80-100 DEG C;
2) concentrated solution that vaporizer 3 evaporation produces enters crystallizer 4 and carries out circulation crystallization;
3) magma that crystallizer 4 circulation crystallization produces enters separating centrifuge 5 and carries out centrifugation, and the mother liquor that centrifugation produces returns in crystallizer 4 and carries out circulation crystallization, and the crystal salt that centrifugation produces is arranged outward or reuse.
Further, the phlegma that vaporizer 3 and crystallizer 4 produce is outer after being back to and carrying out heat exchange with brine waste in preheater 1 to be arranged.
Preferably, described step 1) in, the waste water after preheater 1 pre-heating temperature elevation first enters vaporizer 3 again and evaporates after the COD that modified unit 7 catalytic oxidation is removed in waste water.
Or, preferably, described step 2) in, the concentrated solution that vaporizer 3 evaporation produces first enters crystallizer 4 again and carries out circulation crystallization after the COD that modified unit 7 catalytic oxidation is removed in waste water.
Again or, preferably, described step 3) in, the mother liquor that separating centrifuge 5 centrifugation produces first is back in crystallizer 4 again and carries out circulation crystallization after the COD that modified unit 7 catalytic oxidation is removed in waste water.
Embodiment 1
The utility model treatment system as above and treatment process is adopted to process the ethene alkali residue waste liquid that certain enterprise produces, waste liquid amount 25m
3/ h, its water quality situation is as shown in table 1:
Certain enterprise's ethene alkali residue waste liquid water quality of table 1
Note: contained salt is divided into sodium sulfate.
As can be seen from Table 1, this waste water have that organic content is high, complicated component, difficult degradation feature.According to the feature of waste water, the utility model adopts treatment process as shown in Figure 1, that is: modified unit 7 is located between preheater 1 and vaporizer 3.Its treating processes comprises:
1) inflow temperature is that the waste lye of 30 DEG C promotes through fresh feed pump and enters after preheater 1 is preheated to 80 DEG C, and enter modified unit 7, remove the pollutent in waste water under the electro-oxidizing-catalyzing effect of electrode, in the present embodiment, the volume of modified tank 71 is 600m
3, be of a size of Φ 9.2m × 10.5m, carbon steel is anticorrosion; Modified electrode establishes two groups altogether, and often organize 4, totally 8, modified pump 3,2 is standby with 1, and circular flow is 160m
3/ h, lift 15m;
2) the waste lye temperature after the modified oxidation of modified unit 7 rises to 100 DEG C, and is promoted to vaporizer 3 top through quality-adjusting device discharging pump, is evenly distributed to heat transfer tube and evaporates;
3) concentrated solution that vaporizer 3 evaporation produces enters crystallizer 4 and carries out circulation crystallization,
4) magma that crystallizer 4 circulation crystallization produces enters separating centrifuge and carries out being separated of crystal and mother liquor, and crystalline salt 1.33t/h sends outside, and mother liquor enters mother liquor tank 6; Mother liquor tank 6 mother liquor is saturated salt solution, and weigh through mother liquor pump and be back in crystallizer 4, mother liquor pumping capacity is 0.13m
3/ h, lift is 15m;
5) phlegma that vaporizer 3 and crystallizer 4 produce enters in condensate drum 2, and is weighed to be promoted in preheater 1 with after water heat exchange by condensate pump and to arrange outward, and condensate pump flow is 23.67m
3/ h, lift is 15m.
Alkali residue waste liquid is after processing as mentioned above, and its water outlet COD does not detect, and TDS is less than 50mg/l, NH
3-N does not detect, and arranges outward without mother liquor, can obtain technical grade sodium sulfate salt (GB6009-2014II class acceptable end product), whole treatment system can continuously, steady running.
Embodiment 2
The utility model treatment system as above and treatment process is adopted to process the high-salt wastewater that certain chemical enterprise obtains after being separated through pre-treatment, membrane concentration, salt, salt water yield 150m
3/ h, its water quality situation is as shown in table 2:
Certain chemical enterprise salt solution water quality of table 2
Note: contained salt is divided into sodium sulfate.
According to the water quality characteristics of the salt solution of table 2, the present embodiment adopts treatment process as shown in Figure 2, that is: modified unit 7 is located between the concentrated solution water outlet of vaporizer 3 and the water inlet of crystallizer 4, and the present embodiment adopts the mode of series connection 3 treatment system as shown in Figure 2 to process waste water, and the treating processes of single treatment system comprises:
1) inflow temperature is that the waste lye of 30 DEG C promotes through fresh feed pump and enters after preheater 1 is preheated to 100 DEG C, is promoted to vaporizer 3 top, is evenly distributed to heat transfer tube and evaporates through pump;
2) concentrated solution that vaporizer 3 evaporation produces enters modified unit 7, and under the electro-oxidizing-catalyzing effect of electrode, remove the pollutent in waste water, in the present embodiment, the volume of modified tank 71 is 720m
3, be of a size of Φ 9.9m × 10.6m, carbon steel is anticorrosion; Modified electrode establishes one group altogether, and often organize 4, modified pump 2,1 is standby with 1, and circular flow is 160m
3/ h, lift 15m;
3) waste water after the modified oxidation of modified unit 7 enters crystallizer 4 and carries out circulation crystallization, and the magma that crystallizer 4 circulation crystallization produces enters separating centrifuge and carries out being separated of crystal and mother liquor, and crystalline salt 3.6t/h sends outside, and mother liquor enters mother liquor tank 6; Mother liquor tank 6 mother liquor is saturated salt solution, and weigh through mother liquor pump and be back in crystallizer 4, mother liquor pumping capacity is 0.35m
3/ h, lift is 15m;
4) phlegma that vaporizer 3 and crystallizer 4 produce enters in condensate drum 2, and is weighed to be promoted in preheater 1 with after water heat exchange by condensate pump and to arrange outward, and condensate pump flow is 49.65m
3/ h, lift is 15m.
Alkali residue waste liquid is after processing as mentioned above, its water outlet COD does not detect, and TDS < 50mg/l, arranges outward without mother liquor, technical grade sodium sulfate salt (GB6009-2014II class acceptable end product) can be obtained, whole treatment system can continuously, steady running.
Embodiment 3
The utility model treatment system as above and treatment process is adopted to process the high slat-containing wastewater that certain enterprise's ion exchange regenerant waste liquid obtains after pre-treatment, membrane concentration, salt water yield 16m
3/ h, its water quality situation is as shown in table 3:
Certain enterprise's salt solution water quality of table 3
Note: contained salinity is mainly sulphur calcium chloride, magnesium chloride, sodium-chlor.
According to the water quality characteristics of the salt solution of table 3, the present embodiment adopts treatment process as shown in Figure 3, that is: modified unit 7 is located between the water outlet of mother liquor tank 6 and the water inlet of crystallizer 5, and the treating processes of described treatment system comprises:
1) inflow temperature is that the waste lye of 30 DEG C promotes through fresh feed pump and enters after preheater 1 is preheated to 100 DEG C, is promoted to vaporizer 3 top, is evenly distributed to heat transfer tube and evaporates through pump;
2) vaporizer 3 evaporates the concentrated solution produced and enters crystallizer 4 and carry out circulation crystallization, and the magma that crystallizer 4 circulation crystallization produces enters separating centrifuge and carries out being separated of crystal and mother liquor, and crystalline salt 1.2t/h sends outside, and mother liquor enters mother liquor tank 6;
3) mother liquor in mother liquor tank 6 promotes through pump and enters modified unit 7, and under the electro-oxidizing-catalyzing effect of electrode, remove the pollutent in waste water, in the present embodiment, the volume of modified tank 71 is 1m
3, be of a size of 1m × 1m × 1m, PE material; Modified electrode establishes one group altogether, and often organize 1, modified pump 2,1 is standby with 1, and circular flow is 40m
3/ h, lift 15m;
4) waste water after the modified oxidation of modified unit 7 enters crystallizer 4 and carries out circulation crystallization, the phlegma that vaporizer 3 and crystallizer 4 produce enters in condensate drum 2, and weighed to be promoted in preheater 1 with after water heat exchange by condensate pump and outer to arrange, condensate pump flow is 14.8m
3/ h, lift is 15m.
Alkali residue waste liquid is after described above process, and its water outlet COD does not detect, and TDS < 50mg/l, arranges outward without mother liquor, can obtain the mixing salt that organic content is less than 0.1%, whole treatment system can continuously, steady running.
The utility model is by preferred embodiment having carried out detailed explanation.But, by studying carefully above, to the change of each embodiment with to increase also be that one of ordinary skill in the art institute is apparent.Being intended that all these changes and increasing of applicant has dropped in the protection domain of the utility model claim.Term used herein is only and is illustrated specific embodiment, and it is also not intended to limit utility model.Unless otherwise defined, all terms used herein (comprising technical term and scientific terminology) are all identical with the understanding of the utility model one of ordinary skill in the art.Known function or structure are for briefly and clearly consider or repeat no more.
Claims (10)
1. the evaporative crystallization zero-discharge treatment system of a high-COD waste water, it is characterized in that: comprise preheater, vaporizer, crystallizer, separating centrifuge and mother liquor tank, wherein: the water-in of the water inlet of described preheater and water outlet water former in waste water and vaporizer is respectively connected, the concentrated solution that evaporator evaporation produces enters into crystallizer, the magma that crystallizer crystallization produces enters into separating centrifuge, the mother liquor that separating centrifuge centrifugation produces is back in crystallizer through mother liquor tank, be separated the crystal salt produced arrange outward or reclaim, described treatment system also comprises one for removing the modified unit of COD in waste water.
2. treatment system according to claim 1, is characterized in that: described modified unit is located between the water outlet of preheater and the water-in of vaporizer.
3. treatment system according to claim 1, is characterized in that: described modified unit is located between the concentrated solution water outlet of vaporizer and the water inlet of crystallizer.
4. treatment system according to claim 1, is characterized in that: described modified unit is located between the water outlet of mother liquor tank and the water inlet of crystallizer.
5. according to the treatment system in claim 1-4 described in any one, it is characterized in that: described modified unit comprises modified tank and one or more groups modified electrode group be arranged in parallel, and often organizes modified electrode group and comprises one or more modified electrode be arranged in series.
6. treatment system according to claim 5, is characterized in that: described modified electrode is diamond alloy electrode.
7. according to the treatment system in claim 1-4 described in any one, it is characterized in that: described treatment system comprises condensate drum, the phlegma that vaporizer and crystallizer produce is back in preheater with after the former water heat exchange in preheater through condensate drum and arranges outward.
8. according to the treatment system in claim 1-4 described in any one, it is characterized in that: described preheater is any one in tube and shell heat exchanger, double-pipe exchanger, plate-type heat exchanger.
9. according to the treatment system in claim 1-4 described in any one, it is characterized in that: described separating centrifuge is horizontal centrifugal separating machine; Described vaporizer and crystallizer are multiple-effect evaporator or mechanically compress evaporating vaporizer again.
10. according to the treatment system in claim 1-4 described in any one, it is characterized in that: described treatment system can use in multiple series connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520438025.XU CN204779206U (en) | 2015-06-24 | 2015-06-24 | High COD evaporation of water crystallization zero release processing system that gives up |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520438025.XU CN204779206U (en) | 2015-06-24 | 2015-06-24 | High COD evaporation of water crystallization zero release processing system that gives up |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204779206U true CN204779206U (en) | 2015-11-18 |
Family
ID=54519298
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520438025.XU Expired - Fee Related CN204779206U (en) | 2015-06-24 | 2015-06-24 | High COD evaporation of water crystallization zero release processing system that gives up |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204779206U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926011A (en) * | 2015-06-24 | 2015-09-23 | 北京纬纶华业环保科技股份有限公司 | Evaporating and crystallizing zero-discharge treatment system and method for high-COD waste water |
| CN107651804A (en) * | 2017-11-15 | 2018-02-02 | 昌邑市瑞海生物科技有限公司 | A kind of highly concentrated high salt wastewater from chemical industry prepares the recycling processing method and device of Nacl |
| CN111470692A (en) * | 2020-02-27 | 2020-07-31 | 中国恩菲工程技术有限公司 | Method for treating waste water |
| CN113277665A (en) * | 2021-06-12 | 2021-08-20 | 富莱特(北京)科技有限公司 | Method and device for treating high-concentration high-salinity wastewater through electrolytic evaporation |
-
2015
- 2015-06-24 CN CN201520438025.XU patent/CN204779206U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926011A (en) * | 2015-06-24 | 2015-09-23 | 北京纬纶华业环保科技股份有限公司 | Evaporating and crystallizing zero-discharge treatment system and method for high-COD waste water |
| CN107651804A (en) * | 2017-11-15 | 2018-02-02 | 昌邑市瑞海生物科技有限公司 | A kind of highly concentrated high salt wastewater from chemical industry prepares the recycling processing method and device of Nacl |
| CN111470692A (en) * | 2020-02-27 | 2020-07-31 | 中国恩菲工程技术有限公司 | Method for treating waste water |
| CN113277665A (en) * | 2021-06-12 | 2021-08-20 | 富莱特(北京)科技有限公司 | Method and device for treating high-concentration high-salinity wastewater through electrolytic evaporation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104926011A (en) | Evaporating and crystallizing zero-discharge treatment system and method for high-COD waste water | |
| CN204779206U (en) | High COD evaporation of water crystallization zero release processing system that gives up | |
| CN101786754A (en) | Zero-emission treatment process for salt-containing wastewater | |
| CN104692575A (en) | Crystallization treatment method and device of high salt wastewater | |
| CN204417272U (en) | A kind of crystallization treatment device of high slat-containing wastewater | |
| CN107352726A (en) | A kind of MVR ammonia still processs recovery ammonium sulfate processing high ammonia-nitrogen wastewater technology | |
| CN203768159U (en) | Small seawater desalination device | |
| CN106746110A (en) | A kind of device and processing method for processing high ammonia nitrogen and high salt waste water | |
| CN105254096B (en) | A kind of gas making is containing ammonia containing circulation water pretreatment process and device of the cyanogen containing phenol | |
| CN204417276U (en) | A kind of Coal Chemical Industry strong brine evaporative crystallization divides salt device | |
| CN110981065A (en) | Treatment method of lithium battery industrial wastewater | |
| CN111362492A (en) | Double-effect MVR evaporation treatment method | |
| CN105236627A (en) | Papermaking tail water/recycled water reusing zero-discharge processing method | |
| CN104355431A (en) | Device capable of efficiently treating and recycling reverse osmosis concentrated water and high-salt wastewater | |
| CN203295308U (en) | Organic salt-containing waste water treating system | |
| CN113277665A (en) | Method and device for treating high-concentration high-salinity wastewater through electrolytic evaporation | |
| CN105174587B (en) | A kind of slurrying vacuum in draft tube Zero discharge treatment method | |
| CN204939142U (en) | A kind for the treatment of facility of desulfurization wastewater of flue gas desulphurization system discharge | |
| CN115259518A (en) | System and method for treating percolate concentrated solution | |
| CN206886879U (en) | Membrane separation process concentrates the processing unit of brackish water | |
| CN206156979U (en) | High processing apparatus who contains salt difficult degradation saccharin industrial waste water waste gas | |
| CN210278297U (en) | Sodium nitrate triple-effect countercurrent evaporation crystallization system | |
| CN210261447U (en) | Ultrasonic evaporative crystallization salt separation system for sodium chloride and sodium sulfate | |
| CN211366982U (en) | Sodium chloride and sodium sulfate evaporation and separation device | |
| CN105036444A (en) | Reduction and reclamation recycled water reuse zero emission treating technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151118 |