CN104591458A - Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process - Google Patents
Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process Download PDFInfo
- Publication number
- CN104591458A CN104591458A CN201410059954.XA CN201410059954A CN104591458A CN 104591458 A CN104591458 A CN 104591458A CN 201410059954 A CN201410059954 A CN 201410059954A CN 104591458 A CN104591458 A CN 104591458A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- waste water
- water
- titanium dioxide
- passes
- 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.)
- Pending
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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to a titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process, which comprises: introducing ammonia-containing wastewater into an adjusting tank, introducing the wastewater passing through the adjusting tank into a coagulation sedimentation tank, introducing the wastewater passing through the coagulation sedimentation tank into a pipeline mixer while adding sodium hydroxide into the pipeline mixer, introducing the wastewater passing through the pipeline mixer into a pre-heater, introducing the wastewater passing through the pre-heater into an ammonia evaporation tower, introducing the wastewater passing through the ammonia evaporation tower into a condenser, introducing the condensed liquid into a gas-liquid separation tank, introducing the condensed gas into an ammonia washing tower, and carrying out circulating spraying absorption on the gas introduced into the ammonia washing tower by adding process water or purified water. According to the present invention, the effective treatment on the organic matter in the wastewater is ensured, such that the high-concentration ammonia nitrogen pollutants contained in the wastewater are effectively treated, and the pollution of the titanium dioxide industrial wastewater on the ecology environment is avoided.
Description
Technical field
The present invention relates to a kind of ammonia-containing water treatment process, be specifically related to a kind of titanium dioxide Ammonia-nitrogen wastewater treatment technology.
Background technology
Water is the widest and very important natural resources that the earth distributes, it is the resource that the mankind and all tellurians are depended on for existence, but along with the development of human society, the quantity of wastewater effluent that mankind's activity produces increases year by year, amount of pollutant is more and more, component is more complicated, beyond the water environment capacity of water body, break the ring quality of water body, even jeopardize the ecosystem.Discharge the having the greatest impact to water surrounding of trade effluent, the industrial water drainage such as chemical industry, metallurgy, pharmacy, coal washing, ore dressing, papermaking can cause water body feculence, variable color, and the pollution factors such as Suspended Matter in Water, colourity, turbidity, COD, oil, heavy metal, phenol, cyanogen are exceeded standard.In numerous industry, the acidic high-strength ammonia nitrogen waste water that titanium dioxide industry produces is subject to extensive concern because of features such as its quantity discharged are large, pollution factor is many, pollution load is large.
High-concentration ammonia nitrogenous wastewater process is considered to a global problem always, and because the titanium dioxide acid ammonia nitrogen waste water ammonia nitrogen concentration high water yield is large, change in concentration frequent, make treating processes more complicated, processing cost is higher, is difficult to realize wastewater to reach standard.The ammonia nitrogen processing method of domestic at present conventional titanium dioxide industry waste water mainly contains: in limestone vegetation method, carbide slag neutralisation and speed change up-flow and filter tower method etc., but adopts these methods in process waste water process because running cost is higher, treatment effect is not obvious and cause the reasons such as secondary pollution not to be widely used to environment.
Summary of the invention
Goal of the invention: the object of the invention is to overcome deficiency of the prior art, there is provided a kind of and ensure that useless Organic substance in water is effectively addressed, the high strength ammonia nitrogen pollutant wherein contained effectively is processed, avoids the treatment process that titanium dioxide industry Wastewater on Ecological Environmental pollutes.
Technical scheme: in order to solve the problems of the technologies described above, a kind of titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater of the present invention, it comprises the following steps,
(1) ammonia-containing water is passed into equalizing tank, ammonia-containing water passes into 10t-13t/h, and its water temperature is between 35-50 DEG C, and its pH value is between 6-7, and in waste water, the content of ammonia is between 18000mg/L-20000mg/L;
(2) waste water through equalizing tank is passed into coagulative precipitation tank;
(3) pass in line mixer by the waste water through coagulative precipitation tank, in line mixer, add sodium hydroxide, the amount added is drop into 150-200kg in waste water per ton, makes pH value >=12 of waste water simultaneously;
(4) waste water through line mixer is passed into preheater, make the temperature of waste water reach between 70-90 DEG C;
(5) waste water through preheater is passed into ammonia still, waste water passes into from the water-in of ammonia still middle and upper part with 10t-13t/h, wherein the pressure of ammonia still is 0.1Mpa, and high-temperature steam passes into bottom ammonia still simultaneously, and the intake of high-temperature steam is pass into 0.6m in waste water per ton
3, the pressure of the high-temperature steam passed into is 0.06Mpa, and the temperature of high-temperature steam is between 100-105 DEG C;
(6) waste water through ammonia still is passed into condenser, condensed liquid passes into knockout drum, and condensed gas passes into Ammonic washing tower;
(7) gas passing into Ammonic washing tower is by adding process water or pure water carries out circulated sprinkling absorption, and the liquid obtained passes into ammoniacal liquor relay tank after overcooling, and the gas after circulated sprinkling reaches requirement and directly discharges, and in emission gases, the content of ammonia is at 5-15mg/L.
Described sodium hydroxide adds in line mixer, or adds in coagulative precipitation tank and line mixer simultaneously, and add fashionable in coagulative precipitation tank and line mixer, the total amount that adds of described sodium hydroxide is also for dropping into 150-200kg in waste water per ton simultaneously.
In described ammonia still, be provided with throngh flowing type tray, throngh flowing type tray is provided with panel-type air separatory membrane, waste water carries out ammonia with high-temperature steam by the throngh flowing type tray being provided with panel-type air separatory membrane and is separated with waste water.
Waste water in described knockout drum is back to ammonia still by reflux pump.
After waste water after ammonia still is separated passes into preheater, pass into outlet sump.
Liquid after Ammonic washing tower circulated sprinkling passes into water cooler by pump, passes into Ammonic washing tower again through cooled liquid, finally passes into ammoniacal liquor relay tank.
Described in the present invention, ammonia still comprises tower reactor, described tower reactor is divided into rectifying section from top to bottom, wastewater feed section, profit reduction and reserving segregation section and raffinate segregation section, water inlet pipe is provided with in described tower reactor exterior lateral sides, three water-ins are provided with on described water inlet pipe top, ammoniacal liquor return line is separately provided with in described tower reactor exterior lateral sides, throngh flowing type tray is provided with in described tower reactor inside, described throngh flowing type tray is provided with panel-type air separatory membrane, described throngh flowing type tray is made up of S type column plate matrix, described S type column plate matrix is provided with mass transfer hole, ammonia outlet is provided with at described tower reactor top, wastewater outlet is provided with bottom described tower reactor, below described tower reactor outside, side is provided with high-temperature steam entrance.
Thermometer and tensimeter is provided with in described tower reactor upper outside.
The first liquidometer and the second liquidometer is provided with at described tower reactor lower outside.
Be provided with top visor on described tower reactor top, be provided with bottom visor in described tower reactor bottom.
Be provided with preheater on described tower reactor side, described preheater is connected with described steam stripping ammonia-removing tower by pipeline.
The membranous wall aperture of described panel-type air separatory membrane is 0.1nm-0.5nm.
The present invention is divided into two sections: one section to be pretreatment section, this pretreatment system by equalizing tank, coagulative precipitation tank, add alkali system and form, major function is that the pH value of waste water is adjusted to alkalescence by acidity; Two sections is deamination section, this segment process adopts steam stripped to reclaim ammoniacal liquor technology, it is a kind of method utilizing steam the free ammonia in waste water to be changed into ammonia effusion, namely when high ph-values, make waste water and gas close contact, thus ammonia density in reduction waste water, the impellent of mass transfer process is the difference between equilibrium partial pressure that in the dividing potential drop of ammonia in gas and waste water, the concentration of ammonia is suitable.
The present invention is by realizing by the following technical solutions:
Waste water enters equalizing tank after pipeline is collected, promoted by pump after adopting line mixer to add alkali adjust ph >=12 after modified tune amount and enter preheater, in preheater, at the bottom of waste water and ammonia still tower, high-temperature water outlet heat exchange enters ammonia still after heating up, in tower, the ammonia-containing water sent in tower flows downward, with the high-temperature steam counter current contact directly passed at the bottom of tower, under alkalescence, hot conditions and dynamic action, ammonia content in water is reduced gradually, bottom ammonia still, obtain the deamination water of ammonia content lower than 15mg/L.Enter condenser from the ammonia-containing gas of ammonia still top effusion, after part ammonia-containing gas is condensed, enter knockout drum, then send into ammonia still backflow by reflux pump.The ammonia-containing gas of condenser effusion enters Ammonic washing tower, adopts process water or pure water to carry out circulated sprinkling absorption and obtains the ammoniacal liquor that concentration is 15-20%.The non-condensable gas high altitude discharge up to standard of Ammonic washing tower tower top effusion, the ammoniacal liquor obtained is unified sends into ammoniacal liquor relay tank.The water outlet of ammonia still tower reactor and water inlet heat exchange enter outlet sump after lowering the temperature, and now ammonia nitrogen concentration is at 5-15mg/L, reaches emission standard.
The operation principles of patent deamination section of the present invention: in order to raise the efficiency reduction energy consumption, tower reactor high-temperature water and raw material are carried out heat exchange by this system, waste water enters stripping tower by interchanger, because the relative volatility of ammonia is greater than water, therefore under the effect of steam, more ammonia enters gas phase, and set up new vapor liquid equilibrium with the liquid that last layer S type column plate flows down, after repeatedly gas-liquid phase equilibrium, ammonia density in gas phase is raised to design requirements, then condenser is entered by tower top, liquefied completely, this liquid portion again from trim the top of column to tower in, remainder is transported to product storage tank as product, along with ammonia constantly volatilizees, in liquid, ammonia density is more and more lower, during to tower reactor, ammonia density in water has been reduced to the requirement of qualified discharge.
During the invention process, the waste water containing impurity such as ammonia nitrogens enters equalizing tank by the discharge of titanium white production workshop, is promoted enter preheater after modified tune amount after adopting line mixer to add alkali adjust ph >=12 by pump; In preheater, at the bottom of waste water and ammonia still tower, high-temperature water outlet heat exchange enters ammonia still after heating up; In tower, the ammonia-containing water sent in tower flows downward, and with the high-temperature steam counter current contact directly passed at the bottom of tower, under alkalescence, hot conditions and dynamic action, ammonia content in water is reduced gradually, obtains the deamination water of ammonia content lower than 15mg/L bottom ammonia still; Enter condenser from the ammonia-containing gas of ammonia still top effusion, after part ammonia-containing gas is condensed, enter knockout drum, then send into ammonia still backflow by reflux pump; The ammonia-containing gas of condenser effusion enters Ammonic washing tower, adopts process water or pure water to carry out circulated sprinkling absorption and obtains the ammoniacal liquor that concentration is 15-20%; The non-condensable gas high altitude discharge up to standard of Ammonic washing tower tower top effusion, the ammoniacal liquor obtained is unified sends into ammoniacal liquor relay tank; The water outlet of ammonia still tower reactor and water inlet heat exchange enter outlet sump after lowering the temperature, and now ammonia nitrogen concentration is at 5-15mg/L, reaches " integrated wastewater discharge standard " GB8978-1996 first discharge standard.
Beneficial effect: compared with prior art, its remarkable advantage is in the present invention: the present invention is reached the recovery ammonia in waste water by distillation condensation method, thus realizes the object of environmental protection and refuse renewable resources; Effectively realize the efficient removal of ammonia nitrogen pollutant, water outlet ammonia nitrogen concentration can reach 5-15ppm, and the resource utilization achieving ammonia nitrogen pollutant reclaims, and the ammonia and nitrogen pollution substrate concentration in processed waste water is lower than national grade one discharge standard (≤15ppm) requirement; Treatment effect is good, and cost is low, and level of automation is high, has very high environmental benefit and ecological benefits.
Accompanying drawing explanation
Fig. 1 is schematic flow sheet of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the present invention is further illustrated.
As shown in Figure 1, a kind of titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater of the present invention, it comprises the following steps, ammonia-containing water is passed into equalizing tank, ammonia-containing water passes into 10t-13t/h, its water temperature is between 35-50 DEG C, and its pH value is between 6-7, and in waste water, the content of ammonia is between 18000mg/L-20000mg/L; Waste water through equalizing tank is passed into coagulative precipitation tank; Pass in line mixer by the waste water through coagulative precipitation tank, in line mixer, add sodium hydroxide, the amount added is drop into 150-200kg in waste water per ton, makes pH value>=12 of waste water simultaneously; Waste water through line mixer is passed into preheater, makes the temperature of waste water reach between 70-90 DEG C; Waste water through preheater is passed into ammonia still, waste water passes into from the water-in of ammonia still middle and upper part with 10t-13t/h, wherein the pressure of ammonia still is 0.1Mpa, and high-temperature steam passes into bottom ammonia still simultaneously, and the intake of high-temperature steam is pass into 0.6m in waste water per ton
3, the pressure of the high-temperature steam passed into is 0.06Mpa, and the temperature of high-temperature steam is between 100-105 DEG C; Waste water through ammonia still is passed into condenser, and condensed liquid passes into knockout drum, and condensed gas passes into Ammonic washing tower; The gas passing into Ammonic washing tower is by adding process water or pure water carries out circulated sprinkling absorption, and the liquid obtained passes into ammoniacal liquor relay tank after overcooling, and the gas after circulated sprinkling reaches requirement and directly discharges, and in emission gases, the content of ammonia is at 5-15mg/L.Described sodium hydroxide adds in line mixer, or adds in coagulative precipitation tank and line mixer simultaneously, and add fashionable in coagulative precipitation tank and line mixer, the total amount that adds of described sodium hydroxide is also for dropping into 150-200kg in waste water per ton simultaneously.In described ammonia still, be provided with throngh flowing type tray, throngh flowing type tray is provided with panel-type air separatory membrane, waste water carries out ammonia with high-temperature steam by the throngh flowing type tray being provided with panel-type air separatory membrane and is separated with waste water.Waste water in described knockout drum is back to ammonia still by reflux pump.After waste water after ammonia still is separated passes into preheater, pass into outlet sump.Liquid after Ammonic washing tower circulated sprinkling passes into water cooler by pump, passes into Ammonic washing tower again through cooled liquid, finally passes into ammoniacal liquor relay tank.The present invention is reached the recovery ammonia in waste water by distillation condensation method, thus realizes the object of environmental protection and refuse renewable resources; Effectively realize the efficient removal of ammonia nitrogen pollutant, water outlet ammonia nitrogen concentration can reach 5-15ppm, and the resource utilization achieving ammonia nitrogen pollutant reclaims, and the ammonia and nitrogen pollution substrate concentration in processed waste water is lower than national grade one discharge standard (≤15ppm) requirement; Treatment effect is good, and cost is low, and level of automation is high, has very high environmental benefit and ecological benefits.
The invention provides a kind of thinking and method; the method and access of this technical scheme of specific implementation is a lot; the above is only the preferred embodiment of the present invention; should be understood that; for those skilled in the art, under the premise without departing from the principles of the invention, some improvements and modifications can also be made; these improvements and modifications also should be considered as protection scope of the present invention, and all available prior art of each integral part not clear and definite in the present embodiment is realized.
Claims (6)
1. a titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater, is characterized in that: it comprises the following steps,
(1) ammonia-containing water is passed into equalizing tank, ammonia-containing water passes into 10t-13t/h, and its water temperature is between 35-50 DEG C, and its pH value is between 6-7, and in waste water, the content of ammonia is between 18000mg/L-20000mg/L;
(2) waste water through equalizing tank is passed into coagulative precipitation tank;
(3) pass in line mixer by the waste water through coagulative precipitation tank, in line mixer, add sodium hydroxide, the amount added is drop into 150-200kg in waste water per ton, makes pH value >=12 of waste water simultaneously;
(4) waste water through line mixer is passed into preheater, make the temperature of waste water reach between 70-90 DEG C;
(5) waste water through preheater is passed into ammonia still, waste water passes into from the water-in of ammonia still middle and upper part with 10t-13t/h, wherein the pressure of ammonia still is 0.1Mpa, and high-temperature steam passes into bottom ammonia still simultaneously, and the intake of high-temperature steam is pass into 0.6m in waste water per ton
3, the pressure of the high-temperature steam passed into is 0.06Mpa, and the temperature of high-temperature steam is between 100-105 DEG C;
(6) waste water through ammonia still is passed into condenser, condensed liquid passes into knockout drum, and condensed gas passes into Ammonic washing tower;
(7) gas passing into Ammonic washing tower is by adding process water or pure water carries out circulated sprinkling absorption, and the liquid obtained passes into ammoniacal liquor relay tank after overcooling, and the gas after circulated sprinkling reaches requirement and directly discharges, and in emission gases, the content of ammonia is at 5-15mg/L.
2. titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater according to claim 1, it is characterized in that: described sodium hydroxide adds in line mixer, or add in coagulative precipitation tank and line mixer simultaneously, add fashionable in coagulative precipitation tank and line mixer, the total amount that adds of described sodium hydroxide is also for dropping into 150-200kg in waste water per ton simultaneously.
3. titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater according to claim 1, it is characterized in that: in described ammonia still, be provided with throngh flowing type tray, throngh flowing type tray is provided with panel-type air separatory membrane, and waste water carries out ammonia with high-temperature steam by the throngh flowing type tray being provided with panel-type air separatory membrane and is separated with waste water.
4. titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater according to claim 1, is characterized in that: the waste water in described knockout drum is back to ammonia still by reflux pump.
5. titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater according to claim 1, is characterized in that: after the waste water after ammonia still is separated passes into preheater, pass into outlet sump.
6. titanium dioxide ammonia nitrogen in high density technique for treating industrial wastewater according to claim 1, it is characterized in that: the liquid after Ammonic washing tower circulated sprinkling passes into water cooler by pump, pass into Ammonic washing tower again through cooled liquid, finally pass into ammoniacal liquor relay tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410059954.XA CN104591458A (en) | 2014-02-21 | 2014-02-21 | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410059954.XA CN104591458A (en) | 2014-02-21 | 2014-02-21 | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104591458A true CN104591458A (en) | 2015-05-06 |
Family
ID=53117574
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410059954.XA Pending CN104591458A (en) | 2014-02-21 | 2014-02-21 | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104591458A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830146A (en) * | 2017-02-15 | 2017-06-13 | 晨光生物科技集团股份有限公司 | Chilli extract produces the processing method and processing system of waste liquid |
| CN111115933A (en) * | 2019-12-05 | 2020-05-08 | 江苏中圣高科技产业有限公司 | Flameless torch type ultra-clean discharge process for high-ammonia nitrogen wastewater containing VOCs |
| CN113772892A (en) * | 2021-09-25 | 2021-12-10 | 广东新泰隆环保集团有限公司 | Coking wastewater and domestic sewage combined treatment system and treatment method |
| CN114735748A (en) * | 2022-04-28 | 2022-07-12 | 龙佰集团股份有限公司 | Method for washing titanium dioxide by using high ammonia nitrogen wastewater |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3847807A (en) * | 1973-03-21 | 1974-11-12 | Bethlehem Steel Corp | Removal of cyanide and color bodies from coke plant wastewater |
| CN103183431A (en) * | 2013-04-03 | 2013-07-03 | 江苏夏航环境工程有限公司 | Ammonia-nitrogen wastewater treatment technology |
-
2014
- 2014-02-21 CN CN201410059954.XA patent/CN104591458A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3847807A (en) * | 1973-03-21 | 1974-11-12 | Bethlehem Steel Corp | Removal of cyanide and color bodies from coke plant wastewater |
| CN103183431A (en) * | 2013-04-03 | 2013-07-03 | 江苏夏航环境工程有限公司 | Ammonia-nitrogen wastewater treatment technology |
Non-Patent Citations (1)
| Title |
|---|
| 刘华等: "蒸氨/氨吹脱两级工艺处理高浓度氨氮废水", 《中国给水排水》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830146A (en) * | 2017-02-15 | 2017-06-13 | 晨光生物科技集团股份有限公司 | Chilli extract produces the processing method and processing system of waste liquid |
| CN111115933A (en) * | 2019-12-05 | 2020-05-08 | 江苏中圣高科技产业有限公司 | Flameless torch type ultra-clean discharge process for high-ammonia nitrogen wastewater containing VOCs |
| CN113772892A (en) * | 2021-09-25 | 2021-12-10 | 广东新泰隆环保集团有限公司 | Coking wastewater and domestic sewage combined treatment system and treatment method |
| CN114735748A (en) * | 2022-04-28 | 2022-07-12 | 龙佰集团股份有限公司 | Method for washing titanium dioxide by using high ammonia nitrogen wastewater |
| CN114735748B (en) * | 2022-04-28 | 2023-10-13 | 龙佰集团股份有限公司 | Method for washing titanium white by using high ammonia nitrogen wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103435005B (en) | A kind of synthesis gas washing treatment process | |
| CN104326612A (en) | Method and system for recovering salt from waste water treatment system | |
| CN104058538B (en) | A kind of processing method of wastewater stripping depickling deamination | |
| CN104843813A (en) | Coal gasification high ammonia nitrogen wastewater treatment process | |
| CN105330110A (en) | Direct coal liquefaction sewage treatment system and method | |
| CN103880232A (en) | Treatment system and method for organic salt-containing wastewater | |
| CN104591458A (en) | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process | |
| CN105480988A (en) | Method for preparing high-purity ammonium salts from high-impurity ammonium salt waste liquor | |
| CN104030514B (en) | A kind of processing method of dual-effect energy-saving wastewater stripping depickling deamination | |
| CN105152863B (en) | Method for recovering ethylene glycol and acetaldehyde from polyester wastewater | |
| CN104843816A (en) | Method for combined production of ammonium sulfate and ammonia water through heat pump flash evaporation, stripping and deamination | |
| CN203295308U (en) | Organic salt-containing waste water treating system | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN104528989B (en) | A kind of high ammonia-nitrogen wastewater processes ammonia recovery system | |
| CN102167412B (en) | High-efficiency composite urea waste liquid deep hydrolysis desorption tower | |
| CN106430769A (en) | Coal chemical industry wastewater pretreatment deamination technology and system | |
| CN212222702U (en) | High-efficient low temperature negative pressure ammonia nitrogen waste water strip system | |
| CN205556409U (en) | Benzene hydrogenation waste water desulfurization deamination processing apparatus | |
| CN107902829A (en) | Cold rolling emulsion and oil-bearing wastewater reuse technology and its device | |
| CN104232133A (en) | Method and device for reducing potassium and sodium ion content of coal tar | |
| CN103482816B (en) | Denitrification treatment method and treatment system for wastewater containing DMF (N,N-dimethylformamide) and DMAC (dimethyl acetylamide) | |
| CN105884106A (en) | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same | |
| CN102351262B (en) | Method for treating coal chemical industry sewage | |
| CN114735876A (en) | System and method for reducing organic silicon wastewater treatment energy consumption by utilizing waste heat | |
| CN109399853B (en) | Ammonia nitrogen wastewater treatment device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20150506 |
|
| RJ01 | Rejection of invention patent application after publication |