CN103214047A - Method for recycling NH3-N from ammoninted waste liquid - Google Patents
Method for recycling NH3-N from ammoninted waste liquid Download PDFInfo
- Publication number
- CN103214047A CN103214047A CN201310144190XA CN201310144190A CN103214047A CN 103214047 A CN103214047 A CN 103214047A CN 201310144190X A CN201310144190X A CN 201310144190XA CN 201310144190 A CN201310144190 A CN 201310144190A CN 103214047 A CN103214047 A CN 103214047A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- tower
- waste liquid
- recovery method
- ammoniacal liquor
- 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.)
- Granted
Links
Images
Abstract
The invention provides a method for recycling NH3-N from ammoninted waste liquid, and further provides a method for recycling NH3-N from ammoninted waste liquid with low radioactivity and high concentration. The method comprises the following steps of: based on an intermittent feeding mode, evaporating and condensing waste liquid; and repeatedly absorbing NH3-N to recycle NH3-N from the waste liquid, wherein the final mass concentration of ammonia water can reach about 15%. The method is low in energy consumption, capable of reducing emission of radioactive substances, high in safety, high in concentration of recycled ammonia water and broad in application prospect.
Description
Technical field
The present invention relates to a kind of method for treating waste liquid, specifically, relate to a kind of NH in the ammonia waste liquid that contains
3The recovery method of-N.
Background technology
High temperature gas cooled reactor nuclear fuel element pottery UO
2Sol-gel method is adopted in the production of nuclear slug particle, and used gelling medium is mainly ammoniacal liquor, and technological process comprises wet method and dry method two portions, and wherein wet method partly comprises dissolving, glue, dispersion, ageing, washing, drying and other steps.At first, with analytically pure nitric acid heating for dissolving U
3O
8Pressed powder prepares the uranyl nitrate aqueous solution, is mixed with the colloid that contains certain uranium concentration with multiple additives by certain prescription and operation, comprising organism such as the urea that has complexing agent and buffer reagent effect concurrently, caking agent polyvinyl alcohol, linking agent tetrahydrofurfuryl alcohols; Then, glue is dispersed into even glue through the pressure type vibrating nozzle and drips, and dropping liquid enters behind the ammonia district and is solidified into gel ball in the ammoniacal liquor post gradually; The gained gel ball is used weak ammonia detergent gel ball again in the ammoniacal liquor ageing, to remove wherein ammonium nitrate; At last, the moisture of removing wherein by vacuum-drying obtains the desiccant gel ball.Therefore, can produce a large amount of low-activity waste water that contains materials such as ammonia, uranium, organism, nitrate in process of production.Because waste water composition more complicated, sewage treatment technology process is corresponding longer.Its first step is the volatile ammonia of removing and reclaiming wherein, and for the further processing of waste liquid creates conditions, the ammonia of recovery can be as the raw material reuse in sol-gel technology.
The radioactivity of waste water is lower than 2.6 * 10
2Bq/L, wherein ammonia concentration is greater than 5g/L, and exists with two kinds of forms: incorporate the free ammonia (NH in the water
3) and the ammonium radical ion (NH that produces behind the hydrolysis reaction takes place
4 +).The ammonia treatment recycle object overwhelming majority is an on-radiation waste water at present, processing method generally is under hot conditions, impel ammonia from water, to overflow by improving physical actions such as waste water ph, aeration, usually also can adopt condition of high voltage to impel ammonia to be dissolved in the absorption liquid, improve and reclaim ammonia concn.NH
3-N is an ammonia-nitrogen content index in the water (waste water), and the standard controlling valu is arranged.At containing higher concentration NH
3-N(concentration is greater than 5g/L) waste water, at present main methods has blow-off method and distillation method.And nuclear fuel element pottery UO
2The ammonia process waste liquid that contains that produces in the particle manufacture process belongs to the low-activity waste liquid, must effectively avoid radioactive substance to carry secretly simultaneously except that ammonia; To take into full account the security of processing unit simultaneously, avoid extreme conditions such as high temperature, high pressure as far as possible.Blow-off method processing low-activity contains the ammonia waste liquid and is easy to generate a large amount of radioactive emissions, also can form new pollution in application when increasing energy consumption; And if conventional distillation method can not the better controlled heating condition, the rapid release of ammonia can take place in the heat-processed, produce a large amount of entrainments, cause the effusion of radioactive substance.Therefore, still lack effective a processing at present and contain high density NH
3The technology of-N low-activity waste liquid.
Summary of the invention
The purpose of this invention is to provide a kind of method of wastewater treatment, especially a kind of high density contains NH in the ammonia waste liquid
3The recovery method of-N can be applied to the processing that the low-activity high density contains the ammonia waste liquid.
In order to realize the object of the invention, the invention provides a kind of NH in the ammonia waste liquid that contains
3The recovery method of-N, this method comprises:
(a) will contain the ammonia waste liquid and add in the heating container and heat, form the ammonia steam;
(b) the ammonia steam is fed condensation in the falling film type condensation absorption tower, the ammonia steam of condensation flows at the bottom of the tower, forms ammoniacal liquor;
(c) ammoniacal liquor at the bottom of the tower, and sprays to cat head through cooling for reflux, contacts with uncooled ammonia steam in entering tower;
(d) experience circulation absorbs, and obtains concentration greater than 5% ammoniacal liquor.
Primary contains the ammonia waste liquid can feed heating container through after the pre-treatment such as precipitation and heat exchange, and this heating container can be evaporating kettle.
After experience circulation absorbed, remaining tail gas can feed in the tail gas absorption cell and becomes ammonia solution with the water contact reacts; Waste gas afterwards can feed in the tail gas degraded groove and becomes ammonium salt solution with sour contact reacts.
More excellent, add in heating container in step (a) discontinuous and to contain the ammonia waste liquid, guarantee that containing ammonia waste liquid cumulative volume accounts for the heating container volumetrical more than 1/5th, below 4/5ths.
Treat waste liquid evaporation to being not less than heating container volume five/feed supplement in a period of time, can prevent that the system inner macromolecule from causing fouling because solution concentration becomes sticky thick.
More excellent, contain ammonia waste liquid cumulative volume and account for the heating container volumetrical more than 1/3rd, below 2/3rds.
More excellent, described recovery method comprises that also the detection heating container includes the pH value of ammonia waste liquid, when the pH value is lower than 8, stops heating, cooling, discharging; Ammoniacal liquor pH value at the bottom of the detection tower is when pH is higher than 11, with ammoniacal liquor discharging at the bottom of the tower.
More excellent, adopt the hydronic method of thermal oil of closed circuit control that heating container is heated.
More excellent, the interior temperature of heating container is 65-85 ℃ in the above-mentioned steps, pressure is 1.0-1.3MPa.
More excellent, the interior temperature of heating container is 67-75 ℃ in the above-mentioned steps.
Above-mentioned recovery method also comprises: the ammonia steam that forms in the step (a) through cooling, makes most of water and small part ammonia vapour condensation below 90 ℃ earlier, enters the condensation absorption tower again.
The water that process cooling condensation is got off and the liquid of ammonia steam flow to bottom, condensation absorption tower, form the rarer ammoniacal liquor of concentration.
Falling liquid film material filling type structure is adopted on the condensation absorption tower.The Raschig ring packing layer is adopted in the tower upper and lower, and the middle part is a tubular structure; The uniform flow distributed when the Raschig ring packing layer can increase contact area.The ammoniacal liquor that spray at the top, absorption tower in the step (c) flow to packing layer and contacts with uncooled ammonia steam by the tube wall in the middle falling liquid film device.
In the above-mentioned recovery method, the tower top temperature on condensation absorption tower is 20-40 ℃, and ammonia temperature is 20-35 ℃ at the bottom of the tower.
More excellent, the tower top temperature on condensation absorption tower is 25-30 ℃, ammonia temperature is 20-30 ℃ at the bottom of the tower.
Method provided by the present invention has following advantage:
(1) method of the present invention can make and contain ammonia concentration in the ammoniacal liquor of recovery and increase gradually, and concentration can reach more than 5%, and final quality concentration can reach about 15%, and corresponding pH value is about 11.And the ammoniacal liquor material concentration requires to be higher than 5% in the spherical fuel element production, and the ammoniacal liquor of recovery satisfies the reuse requirement fully;
(2) whole invented technology flow process compactness, the efficient height, pollution-free, economy and security greatly improve;
(3) the inventive method not only can be used for the processing that the high temperature gas cooled reactor fuel element is produced center core preparation technology waste water, and can be used for the processing that general high density contains the ammonia industrial effluent, has wide range of applications;
(4) the fed-batch step can guarantee NH
3-N discharges from the waste liquid system and dissolved running balance in absorption liquid, can prevent that also system makes fouling in the heating container because of excessive vaporization causes the polymer substance thicknessization in the heating container;
(5) use present method in handling low-activity high strength ammonia waste liquid, overcome problems such as violent boiling that lasting heating brings and radioactivity entrainment, extreme conditions such as High Temperature High Pressure have been avoided in the security that has improved equipment simultaneously, reduce energy consumption, avoided the effusion of radioactive substance;
(6) enter the rate of recovery that cooling step before the condensation absorption tower can reduce rate of water make-up, improve ammonia, the condensation absorption tower can increase the concentration of absorption ammoniacal liquor under condition of normal pressure.
Description of drawings
Fig. 1 is the NH in the ammonia waste liquid that contains of the present invention
3The process flow sheet of the recovery method of-N.
Embodiment
" high strength ammonia waste liquid " of the present invention refers to NH
3-N concentration is greater than the waste liquid of 5g/L.The inventive method is not only applicable to uranium-bearing 235, and is applicable to the waste liquid of radioactive substances such as containing uranium 238 and thorium 232, is not limited to that these are several, and " low-activity " is generally understood as content of radioactive substance and is lower than 10 in the inventive method
5Bq/L.Following examples are used to illustrate the present invention, but are not used for limiting the scope of the invention.
Embodiment 1
Have an appointment 250 liters in certain batch of fuel element production process and contain the ammonia process waste liquid and need to handle NH in the former water
3-N mass concentration is 8.9%, and main radioactive substance is a uranium 235, and concentration is about about 10ppm.For realizing the removal and the recovery of ammonia in the waste water, avoid the secondary pollution of radioactivity uranium 235 simultaneously, use the pattern of intermittent warming treatment, fed-batch to carry out distillation method recovery ammonia, whole flow process is seen shown in Figure 1, detailed process is as follows:
(1) contain the ammonia process waste liquid and leave standstill in waste liquid tank, the solid matter post precipitation in the waste liquid is sent supernatant liquor into interchanger with pump, heats through pumping into evaporating kettle again after the heat exchange raising temperature.
(2) at first pump into the feed liquid of 2/3rds volumes in evaporating kettle, using the hydronic mode of thermal oil of closed circuit control to control the evaporating kettle temperature is about 70 ℃; Pressure is 1.3MPa in the evaporating kettle, and when the pH meter reading was reduced to 8 left and right sides in the still, waste liquid accounted for the evaporating kettle volume more than 1/5th simultaneously, pumps into three/one buildup liquid again and be heated to 85 ℃ in still.Move in circles and reach 4/5ths (about 23 liters) of the maximum volume of evaporating kettle to feed liquid.Further processing is treated in discharging when pH is reduced to 8.
(3) in the ammonia absorption portion, extract the ammoniacal liquor of bottom, absorption tower by recycle pump, spray at the top that is back to the absorption tower through under meter and water cooler, the ammoniacal liquor that sprays is by the tube wall in the middle falling liquid film device, the high temperature ammoniacal liquor that flow to packing layer and bottom, absorption tower carries out heat exchange, and the control tower top temperature is about 40 ℃; Ammoniacal liquor after the heat exchange enters in the tower from tower top and sprays, and carries out heat and mass exchange with the ammonia steam that contains that rises, and containing ammonia concentration in the ammoniacal liquor increases gradually, and the control column bottom temperature is about 35 ℃.
(4) behind about two hours loop cycle, pH meter shows that reading is 11.2 at the bottom of the tower, and the ammoniacal liquor mass concentration in this moment absorption tower reaches 13.7%, and radioactivity can directly be carried out the technology reuse less than 0.1Bq/L.Table 1 changes contrast table for the Inlet and outlet water ammonia nitrogen concentration.
Table 1 Inlet and outlet water ammonia nitrogen concentration changes contrast table
| Project | Former water (g/L) | Water outlet (g/L) | Absorb ammoniacal liquor |
| NH 3-N | 13000 | 180 | 13700 |
Embodiment 2
Have an appointment 200 liters in certain batch of fuel element production process and contain the ammonia process waste liquid and need to handle NH in the former water
3-N mass concentration is 5.3%, and main radioactive substance is a uranium 235, and concentration is about 10ppm.For realizing the removal and the recovery of ammonia in the waste water, avoid the secondary pollution of radioactivity uranium 235 simultaneously, use the pattern of intermittent warming treatment, fed-batch to carry out distillation method recovery ammonia, whole flow process is seen shown in Figure 1, detailed process is as follows:
(1) contain the ammonia process waste liquid and leave standstill in waste liquid tank, the solid matter post precipitation in the waste liquid is sent supernatant liquor into interchanger with pump, heats through pumping into evaporating kettle again after the heat exchange raising temperature.
(2) at first pump into the feed liquid of 2/3rds volumes in evaporating kettle, using the hydronic mode of thermal oil of closed circuit control to control the evaporating kettle temperature is about 85 ℃; Pressure is 1.0MPa in the evaporating kettle, when the pH meter reading is reduced to 8 left and right sides in the still, pumps into five/one buildup liquid again and be heated to 70 ℃ in still.Move in circles successively and reach 4/5ths (about 23 liters) of the maximum volume of evaporating kettle to feed liquid.Further processing is treated in discharging when pH is reduced to 8.
(3) in the ammonia absorption portion, extract the ammoniacal liquor of bottom, absorption tower by recycle pump, spray at the top that is back to the absorption tower through under meter and water cooler, the ammoniacal liquor that sprays is by the tube wall in the middle falling liquid film device, the high temperature ammoniacal liquor that flow to packing layer and bottom, absorption tower carries out heat exchange, and the control tower top temperature is about 40 ℃; Ammoniacal liquor after the heat exchange enters in the tower from tower top and sprays, and carries out heat and mass exchange with the ammonia steam that contains that rises, and containing ammonia concentration in the ammoniacal liquor increases gradually, and the control column bottom temperature is about 35 ℃.
(4) behind about two hours loop cycle, pH meter shows that reading is 10.7 at the bottom of the tower, and the ammoniacal liquor mass concentration in this moment absorption tower reaches 13.2%, and radioactivity can directly be carried out the technology reuse less than 0.1Bq/L.Table 2 changes contrast table for the Inlet and outlet water ammonia nitrogen concentration.
Table 2 Inlet and outlet water ammonia nitrogen concentration changes contrast table
| Project | Former water (g/L) | Water outlet (g/L) | Absorb ammoniacal liquor |
| NH 3-N | 5300 | 120 | 13200 |
Embodiment 3
Have an appointment 200 liters in certain batch of fuel element production process and contain the ammonia process waste liquid and need to handle NH in the former water
3-N mass concentration is 7.8%, and main radioactive substance is a uranium 235, and concentration is about 10ppm.For realizing the removal and the recovery of ammonia in the waste water, avoid the secondary pollution of radioactivity uranium 235 simultaneously, use the pattern of intermittent warming treatment, fed-batch to carry out distillation method recovery ammonia, whole flow process is seen shown in Figure 1, detailed process is as follows:
(1) contain the ammonia process waste liquid and leave standstill in waste liquid tank, the solid matter post precipitation in the waste liquid is sent supernatant liquor into interchanger with pump, heats through pumping into evaporating kettle again after the heat exchange raising temperature.
(2) at first pump into the feed liquid of 1/3rd volumes in evaporating kettle, using the hydronic mode of thermal oil of closed circuit control to control the evaporating kettle temperature is about 65 ℃; Pressure is 1.0MPa in the evaporating kettle, when the pH meter reading is reduced to 8 left and right sides in the still, pumps into five/one buildup liquid again and be heated to 70 ℃ in still.Move in circles successively and reach 4/5ths (about 23 liters) of the maximum volume of evaporating kettle to feed liquid.Further processing is treated in discharging when pH is reduced to 8.
(3) in the ammonia absorption portion, extract the ammoniacal liquor of bottom, absorption tower by recycle pump, spray at the top that is back to the absorption tower through under meter and water cooler, the ammoniacal liquor that sprays is by the tube wall in the middle falling liquid film device, the high temperature ammoniacal liquor that flow to packing layer and bottom, absorption tower carries out heat exchange, and the control tower top temperature is about 20 ℃; Ammoniacal liquor after the heat exchange enters in the tower from tower top and sprays, and carries out heat and mass exchange with the ammonia steam that contains that rises, and containing ammonia concentration in the ammoniacal liquor increases gradually, and the control column bottom temperature is about 20 ℃.
(4) behind about two hours loop cycle, pH meter shows that reading is 10.7 at the bottom of the tower, and the ammoniacal liquor mass concentration in this moment absorption tower reaches 14.8%, and radioactivity can directly be carried out the technology reuse less than 0.1Bq/L.Table 3 changes contrast table for the Inlet and outlet water ammonia nitrogen concentration.
Table 3 Inlet and outlet water ammonia nitrogen concentration changes contrast table
| Project | Former water (g/L) | Water outlet (g/L) | Absorb ammoniacal liquor |
| NH 3-N | 7800 | 120 | 14800 |
Though above the present invention is described in detail with a general description of the specific embodiments, on basis of the present invention, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements all belong to the scope of protection of present invention without departing from theon the basis of the spirit of the present invention.
Claims (10)
1. one kind contains NH in the ammonia waste liquid
3The recovery method of-N, this method comprises:
(a) will contain the ammonia waste liquid and add in the heating container and heat, form the ammonia steam;
(b) the ammonia steam is fed condensation in the falling film type condensation absorption tower, the ammonia steam of condensation flows at the bottom of the tower, forms ammoniacal liquor;
(c) ammoniacal liquor at the bottom of the tower, and sprays to cat head through cooling for reflux, contacts with uncooled ammonia steam in entering tower;
(d) experience circulation absorbs, and obtains concentration greater than 5% ammoniacal liquor.
2. recovery method according to claim 1 is characterized in that, adds in heating container in step (a) discontinuous to contain the ammonia waste liquid, guarantees that containing ammonia waste liquid cumulative volume accounts for the heating container volumetrical more than 1/5th, below 4/5ths.
3. recovery method according to claim 2 is characterized in that containing ammonia waste liquid cumulative volume and accounts for the heating container volumetrical more than 1/3rd, below 2/3rds.
4. according to any described recovery method among the claim 1-3, it is characterized in that, also comprise and detect the pH value that heating container includes the ammonia waste liquid, when the pH value is lower than 8, stop heating, cooling, discharging; Ammoniacal liquor pH value at the bottom of the detection tower is when pH is higher than 11, with ammoniacal liquor discharging at the bottom of the tower.
5. according to any described recovery method among the claim 1-3, it is characterized in that, adopt the hydronic method of thermal oil of closed circuit control that heating container is heated.
6. according to any described recovery method among the claim 1-3, it is characterized in that temperature is 65-85 ℃ in the heating unit, pressure is 1.0-1.3MPa.
7. recovery method according to claim 6 is characterized in that, temperature is 67-75 ℃ in the heating container.
8. according to any described recovery method among the claim 1-3, it is characterized in that the ammonia steam that forms in the step (a) through cooling, makes most of water and small part ammonia vapour condensation below 90 ℃ earlier, enters the condensation absorption tower again.
9. according to any described recovery method of claim 1-3, it is characterized in that the tower top temperature on condensation absorption tower is 20-40 ℃, ammonia temperature is 20-35 ℃ at the bottom of the tower.
10. recovery method according to claim 9 is characterized in that the tower top temperature on condensation absorption tower is 25-30 ℃, and ammonia temperature is 20-30 ℃ at the bottom of the tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310144190.XA CN103214047B (en) | 2013-04-23 | 2013-04-23 | Method for recycling NH3-N from ammoninted waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310144190.XA CN103214047B (en) | 2013-04-23 | 2013-04-23 | Method for recycling NH3-N from ammoninted waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103214047A true CN103214047A (en) | 2013-07-24 |
| CN103214047B CN103214047B (en) | 2014-05-07 |
Family
ID=48812274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310144190.XA Active CN103214047B (en) | 2013-04-23 | 2013-04-23 | Method for recycling NH3-N from ammoninted waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103214047B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105883853A (en) * | 2016-06-28 | 2016-08-24 | 盐城工学院 | Method for preparing ammonia with urea |
| CN110853790A (en) * | 2019-11-21 | 2020-02-28 | 清华大学 | Treatment method and treatment system for production waste liquid of high-temperature gas cooled reactor fuel element |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5183577A (en) * | 1992-01-06 | 1993-02-02 | Zimpro Passavant Environmental Systems, Inc. | Process for treatment of wastewater containing inorganic ammonium salts |
| CN1539748A (en) * | 2003-10-31 | 2004-10-27 | 刘金成 | Technique for recycling waste fluid containing urea |
| CN201002976Y (en) * | 2006-12-05 | 2008-01-09 | 青岛天人环境工程有限公司 | Device for reclaiming ammonia from high-content ammonia nitrogen waste water |
| CN101549929A (en) * | 2009-05-18 | 2009-10-07 | 焦国辉 | Method for distilling absorption type negative-pressure thermal cycle coking wastewater |
| CN101560159A (en) * | 2009-05-12 | 2009-10-21 | 嘉兴金燕化工有限公司 | Method for reclaiming ammonia in production of cholamine |
| CN102167454A (en) * | 2011-03-04 | 2011-08-31 | 大连理工大学 | Device and method for recovering ammonia during wastewater treatment |
| CN202808402U (en) * | 2012-08-03 | 2013-03-20 | 济钢集团有限公司 | Residual ammonia water heat pump distillation system |
-
2013
- 2013-04-23 CN CN201310144190.XA patent/CN103214047B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5183577A (en) * | 1992-01-06 | 1993-02-02 | Zimpro Passavant Environmental Systems, Inc. | Process for treatment of wastewater containing inorganic ammonium salts |
| CN1539748A (en) * | 2003-10-31 | 2004-10-27 | 刘金成 | Technique for recycling waste fluid containing urea |
| CN201002976Y (en) * | 2006-12-05 | 2008-01-09 | 青岛天人环境工程有限公司 | Device for reclaiming ammonia from high-content ammonia nitrogen waste water |
| CN101560159A (en) * | 2009-05-12 | 2009-10-21 | 嘉兴金燕化工有限公司 | Method for reclaiming ammonia in production of cholamine |
| CN101549929A (en) * | 2009-05-18 | 2009-10-07 | 焦国辉 | Method for distilling absorption type negative-pressure thermal cycle coking wastewater |
| CN102167454A (en) * | 2011-03-04 | 2011-08-31 | 大连理工大学 | Device and method for recovering ammonia during wastewater treatment |
| CN202808402U (en) * | 2012-08-03 | 2013-03-20 | 济钢集团有限公司 | Residual ammonia water heat pump distillation system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105883853A (en) * | 2016-06-28 | 2016-08-24 | 盐城工学院 | Method for preparing ammonia with urea |
| CN105883853B (en) * | 2016-06-28 | 2019-01-04 | 盐城工学院 | A kind of method that urea prepares ammonia |
| CN110853790A (en) * | 2019-11-21 | 2020-02-28 | 清华大学 | Treatment method and treatment system for production waste liquid of high-temperature gas cooled reactor fuel element |
| CN110853790B (en) * | 2019-11-21 | 2021-12-14 | 清华大学 | Treatment method and treatment system for production waste liquid of high-temperature gas cooled reactor fuel element |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103214047B (en) | 2014-05-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104743728A (en) | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water | |
| CN206616035U (en) | Ammonia-containing water processing unit | |
| CN102351359B (en) | Device and method for radioactive waste water concentration treatment | |
| CN206350977U (en) | Waste gas recovery processing unit | |
| CN103214047B (en) | Method for recycling NH3-N from ammoninted waste liquid | |
| CN110853790B (en) | Treatment method and treatment system for production waste liquid of high-temperature gas cooled reactor fuel element | |
| CN206950931U (en) | The parsing of by-product hydrochloric acid and circulation and stress device in VCM synthesis | |
| CN103143237A (en) | Toluene-containing tail gas recycling process in refractory mica tape production | |
| CN102643189B (en) | System and method for recovering perfluoro caprylic acid from tail gas | |
| CN101538052B (en) | Technical method for preparing ammonium nitrate melt by pressurized neutralization | |
| CN204614460U (en) | Boron-containing radioactive waste liquid deep purifying reclaims the equipment of boric acid simultaneously | |
| CN205360984U (en) | Waste discharge production line of ammonia preparation ammonium sulfate crystallization of utilization | |
| CN108269637A (en) | A kind of spherical shape Nuclear Fuel Element Production Line liquid waste treating apparatus containing organic matter | |
| CN205288056U (en) | Useless ammonia processing system of propane diamine production line | |
| CN109003693B (en) | A kind of spherical shape Nuclear Fuel Element Production Line method for treating waste liquid containing organic matter | |
| CN102836618B (en) | Treating device for tail gas | |
| CN102698462A (en) | Acid mist condensing water-saving method of reaction kettle for producing aluminum polychlorid and system thereof | |
| CN209696301U (en) | Adipic acid plant dust technology concentration systems | |
| CN203816465U (en) | Waste gas absorption tower | |
| CN104549041B (en) | A kind of waste water treatment process | |
| CN104477939B (en) | Low-pressure hydrolysis technology | |
| CN207619159U (en) | A kind of condensate polishing treatment regenerative wastewater ammonia recovery system | |
| CN206001278U (en) | A kind of tail gas nitrogen envelope producing 4,6 dihydroxy-pyrimidines and absorption system | |
| CN203922752U (en) | A kind of device that removes ammonium sulfate and calcium carbonate mixture slurry free ammonia | |
| CN103623674A (en) | Absorbent absorbing gas containing epoxide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |