CN212800002U - High salt waste water zero release resourceful treatment equipment - Google Patents
High salt waste water zero release resourceful treatment equipment Download PDFInfo
- Publication number
- CN212800002U CN212800002U CN202020975665.5U CN202020975665U CN212800002U CN 212800002 U CN212800002 U CN 212800002U CN 202020975665 U CN202020975665 U CN 202020975665U CN 212800002 U CN212800002 U CN 212800002U
- Authority
- CN
- China
- Prior art keywords
- treatment
- unit
- evaporation
- wastewater
- dosing
- 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.)
- Active
Links
Images
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model discloses a high salt waste water zero release resourceful treatment equipment, equipment includes: the evaporation unit is used for carrying out multi-effect forced circulation evaporation concentration treatment on the mixed raw water of the high-salinity wastewater and the desulfurization wastewater; the dosing treatment unit is used for dosing and precipitating the concentrated water output by the evaporation unit; the filtering unit is used for performing pre-filtering treatment on the wastewater after the dosing precipitation treatment; and the post-treatment unit is used for processing the wastewater after the pre-filtration treatment to obtain a resource product. The utility model discloses to high salt waste water treatment, provide a high salt waste water zero release resourceful treatment equipment of optimization, really realize high salt waste water zero release, realized recycling of wastes material, the running cost is low, and product economy is good, and the running cost of whole resourceful zero release is at 20 ~ 50 yuan/ton water, and investment cost also will reduce 20 ~ 40% simultaneously.
Description
Technical Field
The utility model relates to a technical field of high salt waste water treatment, more specifically say, relate to a high salt waste water zero release resourceful treatment equipment.
Background
High salinity wastewater generally refers to wastewater with TDS greater than 1%. The production route of the high-salinity wastewater is wide, and the water quantity is increased year by year. At present, many components in high-salinity wastewater are pollutants which must be strictly controlled in the environmental protection standard of China, and common high-salinity wastewater zero-discharge treatment technical routes are a salt separation treatment technical route and a mixed salt treatment technical route.
The salt separation treatment route mainly adopts membrane method salt separation and thermal method salt separation. The technical route adopted by the membrane method technology is as follows: softening by pretreatment>NF partial salt>Membrane concentration>And (4) performing mass separation and crystallization. The technical route has long flow, high investment and operation cost (the investment cost is more than 200 ten thousand per ton of water according to the water amount per hour, the operation cost per ton of water is more than 100 yuan), especially a large amount of medicament needs to be added in the pretreatment softening stage to reduce the hardness of the desulfurization wastewater, the whole economy is poor, the later maintenance of the membrane is difficult, and finally NaCl and Na produced by quality-divided crystallization2SO4The salt economy is poor. In addition, there is also a small amount of miscellaneous salts that ultimately need to be handled separately in this route. At present, part of the miscellaneous salt is judged as dangerous waste, and the treatment cost is high. The salt separation by a thermal method also needs deep softening pretreatment according to NaCl and Na2SO4The solubility difference realizes the salt separation crystallization at different temperatures, and the overall investment and operation cost are also very high.
The miscellaneous salt treatment route mainly adopts a thermal method technology, and is low-temperature multi-effect evaporation and flue gas evaporation. The low-temperature multi-effect evaporation technology is to adopt steam as a heat source to concentrate or evaporate the high-salinity wastewater into mixed salt after the high-salinity wastewater is softened. To avoid CaSO during evaporation4Scale formation needs to be carried out by perfect softening pretreatment and system integrationThe operating cost of the body is higher than 60 yuan/ton water. Multiple-effect evaporation to obtain miscellaneous salt, difficult subsequent treatment and CaSO4The heat exchange tube is easy to be blocked due to scaling in the evaporation process, and generally needs to be cleaned once in 2-3 months.
Another hot method process route is to treat high-salinity wastewater by high-temperature flue gas bypass evaporation. For a power plant, extracting the flue gas with the temperature of more than 300 ℃ in front of the air preheater, directly drying the high-salinity wastewater into mixed salt, and finally mixing the mixed salt into the fly ash to realize zero discharge of the high-salinity wastewater. However, the high-temperature flue gas bypass evaporation has certain influence on the efficiency of the air preheater and the boiler. Meanwhile, after the concentrated water is evaporated by the bypass flue, salt in the concentrated water is captured by the dust remover along with dust in the flue gas and finally enters the fly ash, so that the resource utilization rate of the fly ash is influenced, and finally the concentrated water enters the natural environment in an uncontrollable way. Typically, the operating cost of high temperature bypass flue gas evaporation is around 40 yuan per ton of water.
SUMMERY OF THE UTILITY MODEL
To the ubiquitous two big problems of high and final product utilization ratio of pretreatment cost of prior art high salt waste water zero release processing technology, the utility model provides an optimization high salt waste water zero release resource processing technology can not only realize the zero release of high salt waste water, has optimized pretreatment process and running cost low moreover, and the final product is chemical industry raw materials such as acid, alkali simultaneously, and utilization ratio is high as a resource.
The utility model provides a high salt waste water zero release resourceful treatment equipment, equipment includes:
the evaporation unit is used for carrying out multi-effect forced circulation evaporation concentration treatment on the mixed raw water of the high-salinity wastewater and the desulfurization wastewater;
the dosing treatment unit is used for dosing and precipitating the concentrated water output by the evaporation unit;
the filtering unit is used for performing pre-filtering treatment on the wastewater after the dosing precipitation treatment;
and the post-treatment unit is used for processing the wastewater after the pre-filtration treatment to obtain a resource product.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment equipment, equipment is still including setting up the preprocessing unit in the evaporation unit upper reaches, preprocessing unit includes pretreatment tank and the pipeline that surpasss that sets up with pretreatment tank is parallelly connected.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment facility, the evaporation unit is multiple-effect forced circulation evaporation concentration device and including two to four-effect circulation evaporimeter of series connection, the dense water export of evaporation unit links to each other with the dense water case that adds the medicine processing unit.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment facility, circulation evaporator is imitated to each among the multiple-effect forced circulation evaporative concentration device and is included seed crystal jar, heater, separator and condensation water pitcher, the upper portion steam outlet of heater links to each other with the separator and the lower part circulating water export of separator links to each other with the lower part circulating water entry of heater through circulating line and the circulating pump that sets up on circulating line, the seed crystal jar pass through the seed crystal pump with the circulating line links to each other, the lower part comdenstion water export of heater still links to each other with the condensation water pitcher, and the dense water export of separator links to each other with the dense water tank who adds the medicine processing unit.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment facility, add the medicine processing unit and include the thick water tank and with the continuous sub-unit that adds of thick water tank's medicine mouth, it has the medicament and is provided with the measurement charging means to store in the medicine sub-unit.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment equipment, the thick water tank includes water inlet, delivery port, adds medicine mouth and sludge outlet, the sludge outlet of thick water tank links to each other with sludge treatment system.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment equipment, the aftertreatment unit is the evaporation crystallization system, waste water after the preliminary filtration treatment gets into evaporation crystallization system aftertreatment obtains NaCl crystal salt.
According to the utility model discloses an embodiment of high salt waste water zero release resourceful treatment equipment, aftertreatment unit is including the ultrafiltration system and the ED bipolar membrane electrodialysis system that establish ties and set up, waste water after the preliminary filtration treatment gets into ultrafiltration system and ED bipolar membrane electrodialysis system aftertreatment in proper order and obtains HCL solution and NaOH solution.
Compared with the conventional scheme, the utility model discloses to high salt waste water treatment, provide a high salt waste water zero release resourceful treatment equipment of optimization, really realize high salt waste water zero release, realized the recycle of wastes material, running cost is low, and product economy is good, and the running cost of whole resourceful zero release is at 20 ~ 50 yuan/ton water, and investment cost also will reduce 20 ~ 40% simultaneously.
Drawings
Fig. 1 shows a schematic structural diagram of a high-salinity wastewater zero-emission recycling treatment device according to an exemplary embodiment of the present invention.
Fig. 2 shows a schematic structural diagram of a high-salinity wastewater zero-emission recycling treatment device according to another exemplary embodiment of the present invention.
Description of reference numerals:
1-desulfurization wastewater, 2-high-salinity wastewater, 3-pretreatment tank, 31-transcendental pipeline, 4-evaporation unit, 41-separation chamber, 42-heater, 43-circulating pump, 44-condensate water tank, 45-seed tank, 5-concentrated water tank, 51-dosing subunit, 52-sludge treatment system, 6-filtration unit, 7-ultrafiltration system, 8-ED bipolar membrane electrodialysis system, 81-HCL and NaOH solution, 9-evaporative crystallization system and 91-NaCL crystallized salt.
Detailed Description
All of the features disclosed in this specification, or all of the steps in any method or process so disclosed, may be combined in any combination, except combinations of features and/or steps that are mutually exclusive.
Any feature disclosed in this specification may be replaced by alternative features serving equivalent or similar purposes, unless expressly stated otherwise. That is, unless expressly stated otherwise, each feature is only an example of a generic series of equivalent or similar features.
The design idea of the high-salinity wastewater zero-discharge recycling treatment equipment is explained in detail below.
The utility model discloses an integral process flow is behind simple preliminary treatment control suspended solid for high salt waste water as required, gets into seed crystal method multi-effect evaporation system and concentrates, and concentrated water after the concentration becomes to use NaCl mixed salt solution as leading after precipitation softening and medicament processing, later adopts the evaporation crystal system to produce NaCl crystallization salt or adopts ED bipolar membrane system to turn into HCL solution and NaOH solution, based on this process flow the utility model provides a corresponding resourceful treatment equipment.
Fig. 1 shows the structure schematic diagram of the high-salinity wastewater zero-emission recycling treatment equipment according to an exemplary embodiment of the present invention, and fig. 2 shows the structure schematic diagram of the high-salinity wastewater zero-emission recycling treatment equipment according to another exemplary embodiment of the present invention.
As shown in fig. 1 and fig. 2, according to the exemplary embodiment of the present invention, the high-salinity wastewater zero-discharge recycling treatment apparatus includes an evaporation unit 4, a chemical-adding treatment unit, a filtering unit 6 and a post-treatment unit, and sequentially performs corresponding treatment on the wastewater.
Specifically, the evaporation unit 4 performs multi-effect forced circulation evaporation concentration treatment on the mixed raw water of the high-salinity wastewater and the desulfurization wastewater. Preferably, the plant also comprises a pre-treatment unit arranged upstream of the evaporation unit 4, the pre-treatment unit comprising a pre-treatment tank 3 and an override line 31 arranged in parallel with the pre-treatment tank 3.
Wherein, the desulfurization waste water 1 is converged with other high-salinity waste water 2, and then enters the evaporation unit 4 for evaporation concentration after passing through the pretreatment unit. The utility model discloses a pretreatment unit can adopt simple coagulating sedimentation's method to carry out the preliminary treatment in order to get rid of most suspended solid to waste water, when the mixed raw water suspended solid content after mixing is lower, also can not carry out the processing of preliminary treatment case and directly get into in the evaporation unit 4 via surmounting pipeline 31.
The utility model discloses an evaporation unit 4 is multiple-effect forced circulation evaporation concentration device and including two to four-effect circulation evaporimeter of series connection, evaporation unit 4's dense water export links to each other with the dense water tank 5 that adds the medicine processing unit. Specifically, the utility model discloses an evaporation unit adopts the evaporation of crystal seed method, prevents the system scale deposit through the crystal seed in the evaporation process, and its effect number can be confirmed according to concrete water yield and quality of water.
Each effect circulating evaporator in the multi-effect forced circulation evaporation and concentration device comprises a seed crystal tank 45, a heater 42, a separation chamber 41 and a condensed water tank 44, wherein an upper steam outlet of the heater 42 is connected with the separation chamber 41, a lower circulating water outlet of the separation chamber 41 is connected with a lower circulating water inlet of the heater 42 through a circulating pipeline and a circulating pump 43 arranged on the circulating pipeline, the seed crystal tank 45 is connected with the circulating pipeline through a seed crystal pump, a lower condensed water outlet of the heater 42 is also connected with the condensed water tank 44, and a concentrated water outlet of the separation chamber 41 is connected with a concentrated water tank 5 of a dosing treatment unit.
The evaporation unit 4 is in a forced circulation evaporation mode, mixed raw water is heated by a heater 42 in the circulation process and then enters a separation chamber 41 for flash evaporation, secondary steam obtained by flash evaporation enters a next effect heater to continuously heat wastewater, and therefore the heat of the secondary steam is recycled. The steam in the heater enters a condensed water tank 44 after being condensed, the concentrated water after being flashed continues to be circularly evaporated through a circulating pump 43, and the concentrated water in the separation chamber is conveyed to a concentrated water tank 5 through a discharge pump after the concentration of the concentrated water reaches a set value. When the system is started, the seed crystals in the seed crystal tank 45 are pumped to the circulating pipeline through the seed crystal pump, and the secondary steam discharged from the final-effect separation chamber is condensed into distilled water through the condenser. The whole evaporation unit is preferably operated in a slightly negative pressure state, and the system vacuum degree is maintained through a vacuum pump.
The dosing processing unit is used for dosing and precipitating the concentrated water output by the evaporation unit. Specifically, add medicine processing unit and include thick water tank 5 and the medicine subunit that links to each other with the medicine mouth of thick water tank 5, add and store the medicament in the medicine subunit and be provided with the measurement charging means. Wherein, the thick water tank 5 also comprises a water inlet, a water outlet, a chemical adding port and a sludge outlet, the sludge outlet of the thick water tank 5 is connected with the sludge treatment system 52, and the sludge generated by the thick water tank 5 can be treated by the sludge treatment system 52.
After the concentrated water generated by multi-effect evaporation enters the concentrated water tank 5, impurities such as hardness, suspended matters, sulfate radicals and the like in the concentrated water are removed through the dosing subunit 51.The dosing subunit 51 sequentially adds lime and Na into the concentrated water in the concentrated water tank 52CO3The raw water is concentrated by times after multi-effect evaporation, the content of calcium sulfate in the raw water is increased by times, and calcium sulfate crystals are separated out after the saturated solubility of the calcium sulfate is exceeded. Because the solubility of calcium sulfate is low, most of calcium sulfate will be separated out into crystals in the concentration process, and only the soluble part of calcium ions and sulfate radicals are left in the concentrated water. Because the concentrated water quantity is reduced by times relative to the original water quantity, the consumption of the medicament required by treating calcium ions and sulfate radicals in the concentrated water is reduced by times compared with the original water treatment, the integral softening and precipitation dosage is reduced by times, and the dosing cost of the system is greatly reduced.
The utility model discloses a filtration unit carries out prefiltration to adding the waste water after the medicine sedimentation treatment, and the follow-up treatment of being convenient for after the prefiltration is handled obtains the resourceful product.
Specifically, the wastewater after the pre-filtration treatment is processed by a post-treatment unit to obtain a resource product. As shown in FIG. 2, the post-treatment unit may be an evaporative crystallization system 9, and the wastewater after the pre-filtration treatment enters the evaporative crystallization system 9 for post-treatment to obtain NaCl crystallized salt 91. As shown in fig. 1, the post-treatment unit may further include an ultrafiltration system 7 and an ED bipolar membrane electrodialysis system 8, which are connected in series, and the wastewater after the pre-filtration treatment sequentially enters the ultrafiltration system 7 to be filtered to remove impurities such as suspended matters and colloids, and then is treated in the ED bipolar membrane electrodialysis system 8 to obtain a HCL solution and a NaOH solution 81. The filtering unit, the ultrafiltration system 7, the ED bipolar membrane electrodialysis system 8 and the like can adopt corresponding products with structures in the prior art.
The utility model discloses a this technical route for the power plant reduced traditional triplex box system, reduced extensive chemical softening system to other high salt waste water. The whole system is simple, solves the problems of high operation cost, incapability of treating miscellaneous salt, easy scaling of the system and the like commonly existing in other high-salt wastewater treatment technologies at present, and has the following main characteristics:
1) the traditional triple box of the power plant can be saved, the rear end of the evaporation concentration system is precipitated and then is softened with concentrated water, the investment cost is saved, and the operation cost is greatly reduced.
2) The method has the advantages that the wastewater concentration is realized by using a seed crystal evaporation technology, the system scaling is avoided, a raw water chemical softening system is avoided, and the system investment and the operation cost are reduced.
3) The treatment mode of firstly concentrating and then adding medicine for softening is adopted, the water quantity after concentration is reduced by times, and therefore the investment cost and the operating cost of a medicine adding system are saved to a great extent.
4) The wastewater is purified by the medicament, and aiming at the characteristics of high chloride ion content and low sulfate radical content commonly existing in the high-salt wastewater at present, barium chloride is adopted to remove sulfate radicals, so that the wastewater is converted into a NaCl solution with higher purity.
5) By adopting the bipolar membrane electrodialysis technology, the concentrated high-concentration NaCl solution is converted into the HCL and NaOH solutions, so that the problem of treatment of waste water mixed salt is solved, the prepared HCL solution and NaOH solution are chemical raw materials, the system can be used for chemical adding treatment, and the economy of resource utilization and sale is better.
The present invention will be further described with reference to the following specific embodiments.
In the embodiment, the total water inlet amount of the mixed raw water after the desulfurization wastewater 1 is converged with other high-salinity wastewater 2 is 30t/h, the hardness is 3000mg/l, suspended matters pretreated by the pretreatment unit are controlled below 500mg/l, and then the mixed raw water enters the evaporation unit 4 (if the content of the suspended matters in the raw water is low, the mixed raw water can directly enter the evaporation unit 4 through the surpassing pipeline 31 for evaporation and concentration). Wherein, the pretreatment is simple coagulating sedimentation to remove most suspended matters, the evaporation unit 4 adopts a forced circulation evaporation form and adopts a crystal seed method for evaporation, and the crystal seed is used for preventing the system from scaling in the evaporation process. The effect of the evaporation unit 4 is determined according to the specific water quantity and water quality, and is determined as three effects in this embodiment.
The evaporation unit 4 is in a forced circulation evaporation mode, the wastewater is heated by the heater 42 in the circulation process and then enters the separation chamber 41 for flash evaporation, and the secondary steam obtained by flash evaporation enters the next effect heater to heat the wastewater continuously, so that the heat of the secondary steam is recycled. The steam in the heater is condensed and then enters the steam condensate tank 44. Flash evaporationThe concentrated water after passing through the circulating pump 43 is continuously evaporated circularly, and after the concentration of the concentrated water in the separation chamber reaches a set value, the concentrated water is sent to the concentrated water tank 5 through the discharging pump. When the system is started, the seed crystals in the seed crystal tank 45 are pumped to the circulating pipeline through the seed crystal pump and maintain the proper seed crystal amount of the system, and CaSO generated by evaporation and crystallization in the wastewater4Preferentially grows on the seed crystal, avoids scaling of the heat exchange tube and a system, and reduces the hardness of the concentrated water supernatant. Meanwhile, the flow velocity of the pipeline of the forced circulation system is controlled to be 2-3 m/s, and the scaling of the wall surface of the heat exchange tube is further avoided. The raw water is concentrated by 5-10 times in a multi-effect evaporation system. The secondary steam discharged from the last effect separation chamber is condensed into distilled water by a condenser. The evaporation system runs under the state of micro negative pressure, and the vacuum degree of the system is maintained through a vacuum pump.
After the concentrated water generated by multi-effect evaporation enters the concentrated water tank 5, the medicament is added through the medicament adding subunit 51 to remove impurities such as hardness, suspended matters, sulfate radicals and the like in the concentrated water. Lime and Na are adopted in the dosing subunit 51 in sequence2CO3And the barium chloride, PAM and other medicaments are subjected to multi-effect evaporation, and then raw water is concentrated by 5-10 times, so that the content of calcium sulfate in the raw water is increased by times and calcium sulfate crystals are precipitated after the saturated solubility of the calcium sulfate is exceeded. Because the solubility of calcium sulfate is low, most of calcium sulfate will be separated out into crystals in the concentration process, and only the soluble part of calcium ions and sulfate radicals are left in the concentrated water. Because the concentrated water amount is only 0.2-0.1 time of the original water amount, the consumption of the medicament for treating calcium ions and sulfate radicals in the concentrated water is reduced by times compared with the original water treatment, the integral softening and precipitation dosage is reduced by times, and the system dosing cost is greatly reduced. The supernatant is mixed salt solution with NaCl as main component and has NaCl purity over 90%. Sludge produced by the concentrate tank 5 is treated by a sludge treatment system 52.
The main component of the solution after the wastewater is treated by the concentrated water tank 5 is NaCl, the wastewater is filtered by the filtering unit 6 and then enters the ultrafiltration system 7 to be filtered to remove impurities such as suspended matters and colloids, the effluent enters the ED bipolar membrane electrodialysis system 8, the wastewater is finally converted into a product 81, and the product 81 is an acid-base solution with the concentration of 5-20%. Or the product salt 91 is crystallized in the evaporation crystallization system 9 after passing through the filtering unit 6, wherein the product 91 is NaCl crystallized salt, and the purity can reach the standard of industrial secondary salt.
The present invention is not limited to the foregoing embodiments. The invention extends to any novel feature or any novel combination of features disclosed in this specification, and to any novel method or process steps or any novel combination of features disclosed.
Claims (8)
1. The utility model provides a high salt waste water zero release resourceful treatment equipment which characterized in that, equipment includes:
the evaporation unit is used for carrying out multi-effect forced circulation evaporation concentration treatment on the mixed raw water of the high-salinity wastewater and the desulfurization wastewater;
the dosing treatment unit is used for dosing and precipitating the concentrated water output by the evaporation unit;
the filtering unit is used for performing pre-filtering treatment on the wastewater after the dosing precipitation treatment;
and the post-treatment unit is used for processing the wastewater after the pre-filtration treatment to obtain a resource product.
2. The high-salinity wastewater zero-emission recycling treatment facility according to claim 1, further comprising a pretreatment unit arranged upstream of the evaporation unit, wherein the pretreatment unit comprises a pretreatment tank and an override pipeline arranged in parallel with the pretreatment tank.
3. The high-salinity wastewater zero-emission recycling treatment equipment according to claim 1, wherein the evaporation unit is a multi-effect forced circulation evaporation concentration device and comprises two to four-effect circulation evaporators connected in series, and a concentrated water outlet of the evaporation unit is connected with a concentrated water tank of the dosing treatment unit.
4. The high-salinity wastewater zero-emission resource treatment equipment according to claim 3, wherein each effect circulation evaporator in the multi-effect forced circulation evaporation and concentration device comprises a seed crystal tank, a heater, a separation chamber and a condensate water tank, an upper steam outlet of the heater is connected with the separation chamber, a lower circulating water outlet of the separation chamber is connected with a lower circulating water inlet of the heater through a circulating pipeline and a circulating pump arranged on the circulating pipeline, the seed crystal tank is connected with the circulating pipeline through a seed crystal pump, a lower condensate water outlet of the heater is further connected with the condensate water tank, and a concentrated water outlet of the separation chamber is connected with a concentrated water tank of the chemical feeding treatment unit.
5. The high-salinity wastewater zero-emission recycling treatment equipment according to claim 1, wherein the dosing treatment unit comprises a concentrated water tank and a dosing subunit connected with a dosing port of the concentrated water tank, and the dosing subunit is stored with a medicament and provided with a metering feeder.
6. The high-salinity wastewater zero-emission resource treatment equipment according to claim 5, wherein the concentrated water tank comprises a water inlet, a water outlet, a chemical adding port and a sludge outlet, and the sludge outlet of the concentrated water tank is connected with a sludge treatment system.
7. The high-salinity wastewater zero-emission recycling treatment equipment according to claim 1, wherein the post-treatment unit is an evaporative crystallization system, and the wastewater after the pre-filtration treatment enters the evaporative crystallization system for post-treatment to obtain NaCl crystallized salt.
8. The high-salinity wastewater zero-emission recycling treatment equipment according to claim 1, wherein the post-treatment unit comprises an ultrafiltration system and an ED bipolar membrane electrodialysis system which are arranged in series, and the wastewater after the pre-filtration treatment sequentially enters the ultrafiltration system and the ED bipolar membrane electrodialysis system for post-treatment to obtain HCL solution and NaOH solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020975665.5U CN212800002U (en) | 2020-06-01 | 2020-06-01 | High salt waste water zero release resourceful treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020975665.5U CN212800002U (en) | 2020-06-01 | 2020-06-01 | High salt waste water zero release resourceful treatment equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212800002U true CN212800002U (en) | 2021-03-26 |
Family
ID=75095553
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020975665.5U Active CN212800002U (en) | 2020-06-01 | 2020-06-01 | High salt waste water zero release resourceful treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212800002U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112960839A (en) * | 2021-04-16 | 2021-06-15 | 宝武水务科技有限公司 | Zero-discharge treatment system and treatment method for acid-making wastewater from purification of active coke flue gas |
| CN113200633A (en) * | 2021-05-28 | 2021-08-03 | 东方电气集团东方锅炉股份有限公司 | Method and system for producing hydrogen by using landfill leachate |
-
2020
- 2020-06-01 CN CN202020975665.5U patent/CN212800002U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112960839A (en) * | 2021-04-16 | 2021-06-15 | 宝武水务科技有限公司 | Zero-discharge treatment system and treatment method for acid-making wastewater from purification of active coke flue gas |
| CN113200633A (en) * | 2021-05-28 | 2021-08-03 | 东方电气集团东方锅炉股份有限公司 | Method and system for producing hydrogen by using landfill leachate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10633271B2 (en) | Zero-discharge technique for separating sludge and salt from desulfurization wastewater | |
| WO2017133512A1 (en) | Treatment apparatus and method for zero liquid discharge of desulfurization wastewater | |
| CN109928560A (en) | A kind of zero emission treatment of desulfured waste water and processing unit | |
| CN212800002U (en) | High salt waste water zero release resourceful treatment equipment | |
| CN208120896U (en) | Can resource recycling power plant desulfurization wastewater zero discharge treatment device | |
| CN102030441A (en) | Method for treating wastewater in production of sebacic acid | |
| CN108178408A (en) | A kind of device and method of desulfurization wastewater processing | |
| CN109851139B (en) | High-salt wastewater softening and concentrating device and method | |
| CN115010309A (en) | Iron phosphate wastewater zero-discharge treatment system and treatment process | |
| CN108275823A (en) | A kind of compound Zero discharging system of dense salt waste water and technique | |
| CN111039492A (en) | Low-cost zero-discharge desulfurization wastewater treatment system and method | |
| CN111439882A (en) | Desulfurization wastewater zero discharge system utilizing flue gas waste heat of power plant | |
| CN104671572A (en) | Electrodialysis softening and concentrating treatment system and method for desulfurization wastewater from thermal power plant | |
| CN204434415U (en) | Concentrating and treating system is softened in a kind of heat-engine plant desulfurized Wastewater by Electric dialysis | |
| CN210620491U (en) | System for zero release of flue gas desulfurization waste water | |
| CN111484180B (en) | Waste heat method recrystallization purification mode and system for zero-emission associated crystallization salt of sewage | |
| CN108609775A (en) | A kind of method of efficient process waste incineration leachate reverse osmosis concentrated water | |
| CN205347092U (en) | Desulfurization waste water zero release processing system | |
| CN109607582B (en) | Method and system for recovering magnesium salt from desulfurization wastewater | |
| CN108483710B (en) | Comprehensive seawater utilization method and system | |
| CN109574366B (en) | High-salinity waste water salt concentration treatment system and process | |
| CN112194298B (en) | System and method for recycling wastewater of whole power plant | |
| CN207726913U (en) | A kind of device of desulfurization wastewater processing | |
| CN111661886A (en) | MVR evaporation salt separation system | |
| CN106430771B (en) | salt separation system and salt separation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |