CN103204601A - Wastewater treatment method - Google Patents
Wastewater treatment method Download PDFInfo
- Publication number
- CN103204601A CN103204601A CN2013101438080A CN201310143808A CN103204601A CN 103204601 A CN103204601 A CN 103204601A CN 2013101438080 A CN2013101438080 A CN 2013101438080A CN 201310143808 A CN201310143808 A CN 201310143808A CN 103204601 A CN103204601 A CN 103204601A
- Authority
- CN
- China
- Prior art keywords
- uranium
- wastewater treatment
- waste water
- ammonia
- concentration
- 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
Abstract
The invention provides a treatment method of low-radioactivity wastewater with complex components and high salt content. The wastewater treatment method comprises the following steps of: removing ammonia by evaporating, and recycling ammonia vapor; removing solid substances and macromolecular substances in the wastewater by removing; adsorbing uranium after pre-treating the filtrate; leaching adsorbent, desorbing the uranium and regenerating the adsorbent; and carrying out concentration crystallization separation onto the uranium-removed wastewater to obtain the solid ammonium nitrate. The wastewater treatment method is capable of realizing the recycling of useful substances ammonia, uranium and ammonium nitrate without generating secondary liquid waste and waste.
Description
Technical field
The invention belongs to field of waste water treatment, relate to a kind of complicated component, supersalinity, low-activity wastewater treatment method.
Background technology
The Prepared by Sol Gel Method ceramic particle has had more widely to be used.The pottery nuclear core of high temperature gas cooled reactor nuclear fuel element namely adopts the sol-gel method preparation.The nuclear core has good security after coating through multilayer, so in nuclear reactor types such as MSR, pressurized-water reactor potential application prospect is arranged.Spherical nucleus core preparation process is to comprise wet method and dry method two portions (the Sol-Gel legal system is equipped with spherical UO2 ceramic particle, Journal of Inorganic Materials, 2007,22(2), 259).Wherein wet method partly comprises dissolving, glue, dispersion, ageing, washing, drying and other steps.At first, prepare the uranyl nitrate aqueous solution with analytically pure nitric acid heating for dissolving U3O8 pressed powder, be 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; Weak ammonia detergent gel ball is used in the ageing in ammoniacal liquor of gained gel ball again, 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.
In order to satisfy the economic index of nuclear fuel element, with the effective reuse of the material in the refuse, and minimizing need be carried out the recovery technical study to Industrial Wastewater Treatment to the harmful effect of environment.The present method of handling at radioactive wastewater mainly contains method of evaporation, ion-exchange-resin process, membrane separation process (radioactive wastewater Processing Technology Research progress, uranium ore smelting, 2010,29(3), 153) etc.
Method of evaporation can make radioelement obtain concentrating and stay in the debris, and its principle is that the waste water that enters vaporizer is heated to boiling by steam or electricradiator, and the moisture in the waste water just flashes to water vapour gradually, condenses into water through cooling; Most radioelement are all stayed in the residual solution and are concentrated.Its characteristics are to handle middle and high horizontal radiation wastewater and have higher enrichment factor and df, but heat energy consumption is bigger, and running cost is higher, simultaneously need also when design and operation to consider that fouling, blast, radioactivity problem such as carry secretly.
Ion-exchange-resin process is the group that can exchange mutually with radioelement in the waste water by on the ion exchange resin, and radioelement is adsorbed on the exchange resin.With ion exchange method handle low-level radioactivity, low salinity, waste water that turbidity is little often can access very high purification efficiency, correlation theory and equipment experience are all quite ripe; But can not handle supersalinity waste water, because the competitive ion in the water can cause radioelement to remove the obvious decline of efficient.
Membrane separation process is the film of selecting perviousness by having, is power with pressure difference, temperature head, potential difference etc., liquid mixture is implemented the method for separating.The membrane technique that adopts in radioactive wastewater is handled both at home and abroad mainly contains methods such as micro-filtration, ultrafiltration, reverse osmosis, nanofiltration and electrodialysis at present.Membrane separation process processing radioactive wastewater has efficiently, economic, reliable advantage, but feedwater quality also there is the higher requirement of ratio, if also contain other a large amount of pollutents (as organism or a large amount of inorganic salt) in the waste water system, can influence the soil removability to radioactive substance greatly.
Because the component of effluent complexity contains multiple organism, inorganic salt and low-level radioactive substance.Above method can be accomplished effective separation to the simple waste liquid of composition, but wastewater produced for the Prepared by Sol Gel Method nuclear fuel, and various materials interact, and adopts conventional any method all can not realize wherein useful component of effective Separation and Recovery.For example, in radioactive wastewater treatment process commonly used, method of evaporation is fit to handle middle and high radioactive wastewater, but it is then very uneconomical to handle low-level radioactive wastewater, also will consider the secondary pollution that reason such as entrainment causes except safety factors; And the high nitrate content in the waste water has increased the wastewater treatment difficulty of ion exchange method and embrane method greatly.The technical process of this waste water of processing that still none cover is complete up to now, in the face of the commercialization trend of high temperature gas cooled reactor, mass-producing is moved towards in fuel element production, presses for the fuel element manufacturing method of wastewater treatment that a cover adapts to production requirement.
Summary of the invention
In order to solve the problem that prior art exists, the purpose of this invention is to provide a kind of supersalinity low-activity wastewater treatment method at complicated component, the raw material that recovery can reuse (comprising ammonia, uranium and ammonium nitrate) reduces the waste discharge amount.
In order to realize purpose of the present invention, the invention provides a kind of wastewater treatment method, may further comprise the steps (as shown in Figure 1):
(1) with waste water evaporative removal ammonia, and reclaims the ammonia steam;
(2) waste water filtering after step (1) processing is removed solid matter and macromolecular substance;
(3) filtrate filtered is carried out pre-treatment, and carry out the absorption of uranium;
(4) to sorbent material drip washing, desorb uranium, adsorbent reactivation;
(5) step (3) except carrying out the condensing crystal separation, the waste water behind the uranium is obtained solid ammonium nitrate.As shown in Figure 1
Further, in the step (1), the mass percent of ammonia is not more than 1% in the final waste liquid.To waste water evaporation except ammonia be filter and silica gel adsorption technology desired.Especially (2～10mol/L), ammonia is handled conventional uranium and is reclaimed processing unit bigger corrodibility and destructiveness are arranged, so first step of wastewater treatment is removal and the recovery of ammonia to contain the ammonia of higher concentration in fuel element manufacturing process waste water.By the control temperature, the most ammonia in the system can be steamed and be unlikely to the evaporation of too much water and cause the solution thickness.Ammonia steam after the evaporation absorbs with deionized water or weak ammonia condensation, and obtaining strong aqua can reuse in sol gel process.Evaporation removes in the ammonia step, NH in the final waste liquid
3Mass percent is not more than at 1% o'clock, could guarantee carrying out smoothly of subsequent technique.
Further, in the step (2), adopt one or more combination of organic microfiltration membrane, gac filter membrane or organic fibre ultra-filtration membrane, remove in the waste water greater than the solid impurity of 5 μ m, require water-quality COD＜1000, turbidity＜0.1NTU.
As preferably, waste liquid passes through organic microfiltration membrane, gac filter membrane and organic fibre ultra-filtration membrane successively when filtering solid matter and macromolecular substance.
Be further used as preferably, organic microfiltration membrane aperture size is 0.1-1 μ m, and organic fibre ultra-filtration membrane aperture size is 50-500nm.
Handle in the water of back and can all remove greater than 5 μ m solid impurities, molecular weight can be removed more than 95% greater than the macromolecule organic of 5KD.
Further, in the step (3), filtrate is carried out pre-treatment, regulates the pH value to 7-8.5.
Further, in the step (3), the porous silica gel filled column is adopted in uranium absorption, and the breakthrough point uranium concentration is 0.05mg/L.
Filtrate is by containing the filled column of sorbent material, and uranium can be adsorbed on the sorbent material by selectivity, and nitrate concentration then is adsorbed hardly.According to the process requirements that ammonium nitrate reclaims, the breakthrough point uranium concentration is 0.05mg/L.
Further, in the step (4), after filled column absorption reaches breakthrough point, with leacheate drip washing sorbent material, be the drip washing qualifying liquid when the effluent liquid uranium concentration is not less than 1g/L, by precipitating with alkaline reagents, and separate; When the effluent liquid uranium concentration is the drip washing lean solution during less than 1g/L, return step (3) and carry out uranium absorption again.
Particularly, leacheate is strongly acidic solution, is preferably nitric acid.
The further recovery of above-mentioned uranium is separated out uranium in the solution by adding alkaline reagents with sedimentary form.Obtain the uranium-bearing solid chemical compound by centrifugal or filtration again.
Filled column behind the above-mentioned desorption, particularly porous silica gel filled column behind the drip washing desorption, can be regenerated, and continue to use.
Except main component in the waste water behind the uranium is ammonium nitrate, the effluent liquid before the breakthrough point is concentrated, by evaporation ammonium nitrate is concentrated.Produce potential safety hazard in order to reduce the ammonium nitrate solution overrich and guarantee ammonium nitrate energy crystallisation by cooling simultaneously, the concentrated solution mass percent concentration is preferably 5-12%.
Concentration liquid of ammonium nitrate after the evaporation concentration is placed naturally cooling under the room temperature, and oversaturated ammonium nitrate is separated out with crystalline form, and above process is a crystallization.Gained crystal by adopting filtration method makes solid-liquid separation, separates the back and cleans with a small amount of saturated ammonium nitrate solution; Scavenging solution and 4-5 criticize a crystallization mother liquor and concentrate, and evaporate to subtract to hold and the secondary crystallization.Crystalline mother solution behind the secondary crystallization is treated further processing.
The vaporize water that evaporative process produces is for the industrial production reuse.
The present invention also provides the application of above-mentioned method of wastewater treatment in handling supersalinity low-activity waste water.
Preferably, the nitrate concentration 5-50g/L of described waste water, organic cod 10
3-4 * 10
5, ammonia concentration is greater than 5g/L, metal ingredient concentration range 0.05-50mg/L.
Beneficial effect of the present invention is: provide a cover the complete supersalinity low-activity wastewater treatment method at complicated component; Realized the recovery of useful matter ammonia, uranium and ammonium nitrate; Substantially do not produce secondary waste liquid refuse.
The present invention also can be used for the processing of the similar waste water of common sol preparing gel ceramic process composition except can be used for the processing of process waste liquor in the production of high temperature gas cooled reactor fuel element nuclear core.
Description of drawings
Fig. 1 is the process flow sheet of a kind of method of wastewater treatment of the present invention.
Embodiment
Following examples are used for explanation 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 ammonia process waste water and need to handle NH in the former water
3-N mass concentration is 8.9%, and uranium concentration is about about 10mg/L, and ammonium nitrate concn is 12.4g/L, organic cod value 4 * 10
4For realizing removal and the recovery of main component in the waste water, take following scheme: method of evaporation reclaims ammonia → filtration and removes solid impurity and organic macromolecule → silica gel adsorption → desorb recovery uranium → crystallization process recovery ammonium nitrate (as shown in Figure 1).
At first by evaporating kettle heating in the evaporation ammonia removal device, the ammonia that steams absorbs with deionized water waste water.The ammonia mass concentration is reduced to 0.9% in except waste water behind the ammonia, and to obtain concentration be about 13.1% reuse ammoniacal liquor.
Except waste water behind the ammonia filters assembled unit through organic microfiltration membrane (aperture size 1 μ m), gac filter membrane and organic fibre ultra-filtration membrane (φ 100nm), remove solid impurity and macromolecular substance, to guarantee the water inlet requirement of silica gel adsorption unit, improve treatment effect.Filtering unit inlet pressure value is between 0.26-0.35MPa, and top hole pressure is between 0.10-0.22MPa.Intensity of variation through other compositions behind the filtering unit is: the uranium clearance is 4.5%, and the nitrate removal rate is about 1.8%, and larger molecular organics removes (KD〉500), and except rate is 82.3%, small organic molecule (KD＜500) clearance is 1.9%.
Enter the silica gel adsorption unit through the waste water after the filtration treatment.Selecting granularity is that 100-200 order, specific surface area are 550m
2The silica gel of/g is as sorbent material, and 50g silica gel is contained in the glass column of φ 3cm.Waste water ph is adjusted to 8.1, pumps into silica gel adsorption column by peristaltic pump, uranium can be adsorbed by selectivity in the waste water, and uranium content can be reduced to below the 0.05ppm in the effluent liquid, and nitrate radical then is not adsorbed.Under this pH condition, the loading capacity of silica gel is 22.3mg/g silica gel.
Silica gel is reversible to absorption and the desorption process of uranium.After silica gel adsorption reached breakthrough point, adopting concentration was 1mol L
-1HNO
3Solution gets off the uranium drip washing of absorption.Uranium concentration is higher than 1g/L drip washing qualifying liquid concentrates, obtaining uranium concentration is the concentrated stripping liquid of 102g/L, realizes the recovery of uranium by further chemical precipitation, method such as centrifugal; The drip washing lean solution that uranium concentration is lower than 1g/L is back to the silica gel adsorption processing; When uranium concentration is lower than 0.05mg/L in the effluent liquid, be neutrality with deionized water drip washing silica gel to effluent liquid, silica gel recycles.
The adsorption uranium breakthrough point is decided to be 0.05mg/L.Effluent liquid before the breakthrough point is concentrated, and every 5L is a collection of pending liquid, makes ammonium nitrate concn to 9.1% in the solution by the evaporation heating, stops heating and places cooling in room temperature.The ammonium nitrate crystal of separating out is filtered, with saturated ammonium nitrate solution washing back seasoning; 5 batches of crystallization post crystallization mother liquors are concentrated, carried out secondary and subtract the appearance crystallization, the secondary crystal mother liquor subtracts and holds to 1.8% of original volume, treats further processing.Uranium mass concentration mean value w (U) is 4.5 * 10 in the gained ammonium nitrate product
-7, than the limit standard 2 * 10 of regulation
-6(document) low approximately 1 order of magnitude.
Embodiment 2
Certain batch of collosol and gel preparation technology prepares to have an appointment 200 liters in the uranium oxide ceramics particle manufacture process and contains ammonia process waste water and need to handle NH in the former water
3-N mass concentration is 1.3%, and uranium concentration is about about 50mg/L, and ammonium nitrate concn is 5g/L, organic cod value 4 * 10
5For realizing removal and the recovery of main component in the waste water, take following scheme: method of evaporation reclaims ammonia → filtration and removes solid impurity and organic macromolecule → silica gel adsorption → desorb recovery uranium → crystallization process recovery ammonium nitrate.
At first by evaporating kettle heating in the evaporation ammonia removal device, the ammonia that steams absorbs with deionized water waste water.The ammonia mass concentration is reduced to 0.8% in except waste water behind the ammonia, and to obtain concentration be about 11.1% reuse ammoniacal liquor.
Except waste water behind the ammonia filters assembled unit through organic microfiltration membrane (aperture size 0.1 μ m), gac filter membrane and organic fibre ultra-filtration membrane (φ 500nm), remove solid impurity and macromolecular substance, to guarantee the water inlet requirement of silica gel adsorption unit, improve treatment effect.Filtering unit inlet pressure value is between 0.26-0.35MPa, and top hole pressure is between 0.10-0.22MPa.Intensity of variation through other compositions behind the filtering unit is: the uranium clearance is 2.5%, and the nitrate removal rate is about 1.3%, and larger molecular organics removes (KD〉500), and except rate is 75.3%, small organic molecule (KD＜500) clearance is 1.2%.
Enter the silica gel adsorption unit through the waste water after the filtration treatment.Selecting granularity is that 100-200 order, specific surface area are 550m
2The silica gel of/g is as sorbent material, and 50g silica gel is contained in the glass column of φ 3cm.Waste water ph is adjusted to 8.5, pumps into silica gel adsorption column by peristaltic pump, uranium can be adsorbed by selectivity in the waste water, and uranium content can be reduced to below the 0.05ppm in the effluent liquid, and nitrate radical then is not adsorbed.Under this pH condition, the loading capacity of silica gel is 20.5mg/g silica gel.
Silica gel is reversible to absorption and the desorption process of uranium.After silica gel adsorption reached breakthrough point, adopting concentration was 1mol L
-1HNO
3Solution gets off the uranium drip washing of absorption.Uranium concentration is higher than 1g/L drip washing qualifying liquid concentrates, obtaining uranium concentration is the concentrated stripping liquid of 45g/L, realizes the recovery of uranium by further chemical precipitation, method such as centrifugal; The drip washing lean solution that uranium concentration is lower than 1g/L is back to the silica gel adsorption processing; When uranium concentration is lower than 0.05mg/L in the effluent liquid, be neutrality with deionized water drip washing silica gel to effluent liquid, silica gel recycles.
The adsorption uranium breakthrough point is decided to be 0.05mg/L.Effluent liquid before the breakthrough point is concentrated, and every 5L is a collection of pending liquid, makes ammonium nitrate concn to 9.5% in the solution by the evaporation heating, stops heating and places cooling in room temperature.The ammonium nitrate crystal of separating out is filtered, with saturated ammonium nitrate solution washing back seasoning; 5 batches of crystallization post crystallization mother liquors are concentrated, carried out secondary and subtract the appearance crystallization, the secondary crystal mother liquor subtracts and holds to 1.5% of original volume, treats further processing.Uranium mass concentration mean value w (U) is 2.7 * 10 in the gained ammonium nitrate product
-7, than the limit standard 2 * 10 of regulation
-6(document) low approximately 1 order of magnitude.
Embodiment 3
Certain batch of collosol and gel preparation technology prepares to have an appointment 100 liters in the uranium oxide ceramics particle manufacture process and contains ammonia process waste water and need to handle NH in the former water
3-N mass concentration is 5.7%, and uranium concentration is about about 0.05mg/L, and ammonium nitrate concn is 50g/L, organic cod value 10
3For realizing removal and the recovery of main component in the waste water, take following scheme: method of evaporation reclaims ammonia → filtration and removes solid impurity and organic macromolecule → silica gel adsorption → desorb recovery uranium → crystallization process recovery ammonium nitrate.
At first by evaporating kettle heating in the evaporation ammonia removal device, the ammonia that steams absorbs with deionized water waste water.The ammonia mass concentration is reduced to 0.9% in except waste water behind the ammonia, and to obtain concentration be about 10.2% reuse ammoniacal liquor.
Except waste water behind the ammonia filters assembled unit through organic microfiltration membrane (aperture size 0.1 μ m), gac filter membrane and organic fibre ultra-filtration membrane (φ 50nm), remove solid impurity and macromolecular substance, to guarantee the water inlet requirement of silica gel adsorption unit, improve treatment effect.Filtering unit inlet pressure value is between 0.26-0.35MPa, and top hole pressure is between 0.10-0.22MPa.Intensity of variation through other compositions behind the filtering unit is: the uranium clearance is 2.0%, and the nitrate removal rate is about 1.5%, and larger molecular organics removes (KD〉500), and except rate is 78.9%, small organic molecule (KD＜500) clearance is 1.0%.
Enter the silica gel adsorption unit through the waste water after the filtration treatment.Selecting granularity is that 100-200 order, specific surface area are 550m
2The silica gel of/g is as sorbent material, and 50g silica gel is contained in the glass column of φ 3cm.Waste water ph is adjusted to 7.0, pumps into silica gel adsorption column by peristaltic pump, uranium can be adsorbed by selectivity in the waste water, and uranium content can be reduced to below the 0.05ppm in the effluent liquid, and nitrate radical then is not adsorbed.Under this pH condition, the loading capacity of silica gel is 29.0mg/g silica gel.
Silica gel is reversible to absorption and the desorption process of uranium.After silica gel adsorption reached breakthrough point, adopting concentration was 1mol L
-1HNO
3Solution gets off the uranium drip washing of absorption.Uranium concentration is higher than 1g/L drip washing qualifying liquid concentrates, obtaining uranium concentration is the concentrated stripping liquid of 87g/L, realizes the recovery of uranium by further chemical precipitation, method such as centrifugal; The drip washing lean solution that uranium concentration is lower than 1g/L is back to the silica gel adsorption processing; When uranium concentration is lower than 0.05mg/L in the effluent liquid, be neutrality with deionized water drip washing silica gel to effluent liquid, silica gel recycles.
The adsorption uranium breakthrough point is decided to be 0.05mg/L.Effluent liquid before the breakthrough point is concentrated, and every 5L is a collection of pending liquid, makes ammonium nitrate concn to 10.8% in the solution by the evaporation heating, stops heating and places cooling in room temperature.The ammonium nitrate crystal of separating out is filtered, with saturated ammonium nitrate solution washing back seasoning; 5 batches of crystallization post crystallization mother liquors are concentrated, carried out secondary and subtract the appearance crystallization, the secondary crystal mother liquor subtracts and holds to 1.5% of original volume, treats further processing.Uranium mass concentration mean value w (U) is 3.2 * 10 in the gained ammonium nitrate product
-7, than the limit standard 2 * 10 of regulation
-6(document) low approximately 1 order of magnitude.
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. wastewater treatment method may further comprise the steps:
(1) with waste water evaporative removal ammonia, and reclaims the ammonia steam;
(2) waste water filtering after step (1) processing is removed solid matter and macromolecular substance;
(3) filtrate filtered is carried out pre-treatment, and carry out the absorption of uranium;
(4) to sorbent material drip washing, desorb uranium, adsorbent reactivation;
(5) step (3) except carrying out the condensing crystal separation, the waste water behind the uranium is obtained solid ammonium nitrate.
2. method of wastewater treatment as claimed in claim 1 is characterized in that, in the step (1), the mass percent of ammonia is not more than 1% in the final waste liquid.
3. method of wastewater treatment as claimed in claim 1, it is characterized in that, in the step (2), adopt one or more combination of organic microfiltration membrane, gac filter membrane or organic fibre ultra-filtration membrane, remove in the waste water greater than the solid impurity of 5 μ m, require water-quality COD＜1000, turbidity＜0.1NTU.
4. method of wastewater treatment as claimed in claim 3 is characterized in that, waste liquid passes through organic microfiltration membrane, gac filter membrane and organic fibre ultra-filtration membrane successively when filtering solid matter and macromolecular substance.
5. as claim 3 or 4 described method of wastewater treatment, it is characterized in that organic microfiltration membrane aperture size is 0.1-1 μ m, organic fibre ultra-filtration membrane aperture size is 50-500nm.
6. method of wastewater treatment as claimed in claim 1 is characterized in that, in the step (3), filtrate is carried out pre-treatment, regulates the pH value to 7-8.5.
7. as method of wastewater treatment as described in the claim 6, it is characterized in that in the step (3), the porous silica gel filled column is adopted in uranium absorption, the breakthrough point uranium concentration is 0.05mg/L.
8. method of wastewater treatment as claimed in claim 1 is characterized in that, in the step (4), after filled column absorption reaches breakthrough point, with leacheate drip washing sorbent material, be the drip washing qualifying liquid when the effluent liquid uranium concentration is not less than 1g/L, by precipitating with alkaline reagents, and separate; When the effluent liquid uranium concentration is the drip washing lean solution during less than 1g/L, return step (3) and carry out uranium absorption again.
9. the application of each described method of wastewater treatment of claim 1-8 in handling supersalinity low-activity waste water.
10. application as claimed in claim 9 is characterized in that, the nitrate concentration 5-50g/L of described waste water, organic cod 10
3-4 * 10
5, ammonia concentration is greater than 5g/L, metal ingredient concentration range 0.05-50mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310143808.0A CN103204601B (en) | 2013-04-23 | 2013-04-23 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310143808.0A CN103204601B (en) | 2013-04-23 | 2013-04-23 | Wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103204601A true CN103204601A (en) | 2013-07-17 |
| CN103204601B CN103204601B (en) | 2014-05-07 |
Family
ID=48752043
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310143808.0A Active CN103204601B (en) | 2013-04-23 | 2013-04-23 | Wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103204601B (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103440894A (en) * | 2013-08-12 | 2013-12-11 | 清华大学 | Process for treating high-ammonia radioactive wastewater by membrane absorbing method |
| CN103474122A (en) * | 2013-09-04 | 2013-12-25 | 清华大学 | Method of removing tetrahydrofurfuryl alcohol from waste water in production of high temperature reactor fuel elements |
| CN104291489A (en) * | 2014-10-15 | 2015-01-21 | 清华大学 | Treatment method for process wastewater in preparation of high-temperature gas-cooled reactor element core |
| CN106629978A (en) * | 2016-12-30 | 2017-05-10 | 北京师范大学 | Adsorption and regeneration integrated reactor system for radioactive wastewater treatment |
| CN107032427A (en) * | 2017-04-28 | 2017-08-11 | 曹志平 | A kind of method and device for concentrating waste water or reclaiming nutrient |
| CN107665746A (en) * | 2016-07-27 | 2018-02-06 | 东华理工大学 | Device for uranium in graphene oxide dispersion adsorbing separation radioactive wastewater |
| CN108257706A (en) * | 2016-12-29 | 2018-07-06 | 中核建中核燃料元件有限公司 | A kind of uranium-containing waste water processing method |
| CN108766611A (en) * | 2018-08-29 | 2018-11-06 | 核工业理化工程研究院 | The zero discharge treatment device and its processing method of strong nitric acid system uranium-bearing waste liquid |
| CN109003693A (en) * | 2018-07-13 | 2018-12-14 | 清华大学 | A kind of spherical shape Nuclear Fuel Element Production Line method for treating waste liquid containing organic matter |
| CN109987738A (en) * | 2017-12-29 | 2019-07-09 | 中核四0四有限公司 | Uranium recovery process in a kind of uranium-bearing waste liquid |
| CN110204136A (en) * | 2019-04-07 | 2019-09-06 | 李英劼 | The method that electroplating waste water resource utilizes |
| CN113707353A (en) * | 2020-12-25 | 2021-11-26 | 核工业北京化工冶金研究院 | Sponge iron filter material activation and reuse method |
| CN115440404A (en) * | 2021-06-03 | 2022-12-06 | 西南科技大学 | Method for treating high-temperature gas cooled reactor fuel element core preparation process wastewater by using novel functional fibers |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57111244A (en) * | 1980-12-25 | 1982-07-10 | Power Reactor & Nuclear Fuel Dev Corp | Recovery of uranium |
| CN102031369A (en) * | 2010-12-01 | 2011-04-27 | 核工业北京化工冶金研究院 | Method for extracting uranium by using ion exchange fixed tower under alternate Ph condition |
| CN102101682A (en) * | 2010-12-23 | 2011-06-22 | 苏州市创新净化有限公司 | Continuous dehydration distillation purification system and process method for ammonia |
| CN102876890A (en) * | 2012-10-24 | 2013-01-16 | 南华大学 | Method for recovering uranium from beryllium uranium ore with wet process |
| CN102976543A (en) * | 2012-12-18 | 2013-03-20 | 深圳市能源环保有限公司 | Garbage leachate disposal method and system |
-
2013
- 2013-04-23 CN CN201310143808.0A patent/CN103204601B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57111244A (en) * | 1980-12-25 | 1982-07-10 | Power Reactor & Nuclear Fuel Dev Corp | Recovery of uranium |
| CN102031369A (en) * | 2010-12-01 | 2011-04-27 | 核工业北京化工冶金研究院 | Method for extracting uranium by using ion exchange fixed tower under alternate Ph condition |
| CN102101682A (en) * | 2010-12-23 | 2011-06-22 | 苏州市创新净化有限公司 | Continuous dehydration distillation purification system and process method for ammonia |
| CN102876890A (en) * | 2012-10-24 | 2013-01-16 | 南华大学 | Method for recovering uranium from beryllium uranium ore with wet process |
| CN102976543A (en) * | 2012-12-18 | 2013-03-20 | 深圳市能源环保有限公司 | Garbage leachate disposal method and system |
Non-Patent Citations (3)
| Title |
|---|
| 李彩翎 等: "低温蒸发处理核工业废水的研究", 《内蒙古工业大学学报》 * |
| 谷存礼 等: "铀同位素浓缩试验装置退役废水处理试验研究", 《辐射防护通讯》 * |
| 鄂学礼 等: "《饮用水深度净化与水质处理器》", 31 August 2004, 化学工业出版社 * |
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103440894A (en) * | 2013-08-12 | 2013-12-11 | 清华大学 | Process for treating high-ammonia radioactive wastewater by membrane absorbing method |
| CN103474122A (en) * | 2013-09-04 | 2013-12-25 | 清华大学 | Method of removing tetrahydrofurfuryl alcohol from waste water in production of high temperature reactor fuel elements |
| CN103474122B (en) * | 2013-09-04 | 2016-02-10 | 清华大学 | The minimizing technology of tetrahydrofurfuryl alcohol in a kind of high temperature nuclear reactor fuel element factory effluent |
| CN104291489A (en) * | 2014-10-15 | 2015-01-21 | 清华大学 | Treatment method for process wastewater in preparation of high-temperature gas-cooled reactor element core |
| CN104291489B (en) * | 2014-10-15 | 2015-12-02 | 清华大学 | The treatment process of high temperature gas-cooled Nuclear fuel core core preparation technology waste water |
| CN107665746B (en) * | 2016-07-27 | 2020-01-14 | 东华理工大学 | Device for adsorbing and separating uranium in radioactive wastewater by using graphene oxide dispersion liquid |
| CN107665746A (en) * | 2016-07-27 | 2018-02-06 | 东华理工大学 | Device for uranium in graphene oxide dispersion adsorbing separation radioactive wastewater |
| CN108257706B (en) * | 2016-12-29 | 2021-03-02 | 中核建中核燃料元件有限公司 | Uranium-containing wastewater treatment method |
| CN108257706A (en) * | 2016-12-29 | 2018-07-06 | 中核建中核燃料元件有限公司 | A kind of uranium-containing waste water processing method |
| CN106629978A (en) * | 2016-12-30 | 2017-05-10 | 北京师范大学 | Adsorption and regeneration integrated reactor system for radioactive wastewater treatment |
| CN107032427A (en) * | 2017-04-28 | 2017-08-11 | 曹志平 | A kind of method and device for concentrating waste water or reclaiming nutrient |
| CN109987738A (en) * | 2017-12-29 | 2019-07-09 | 中核四0四有限公司 | Uranium recovery process in a kind of uranium-bearing waste liquid |
| CN109003693A (en) * | 2018-07-13 | 2018-12-14 | 清华大学 | A kind of spherical shape Nuclear Fuel Element Production Line method for treating waste liquid containing organic matter |
| CN109003693B (en) * | 2018-07-13 | 2019-10-25 | 清华大学 | A kind of spherical shape Nuclear Fuel Element Production Line method for treating waste liquid containing organic matter |
| CN108766611A (en) * | 2018-08-29 | 2018-11-06 | 核工业理化工程研究院 | The zero discharge treatment device and its processing method of strong nitric acid system uranium-bearing waste liquid |
| CN108766611B (en) * | 2018-08-29 | 2024-02-13 | 核工业理化工程研究院 | Zero-emission treatment device and treatment method for uranium-containing waste liquid of strong nitric acid system |
| CN110204136A (en) * | 2019-04-07 | 2019-09-06 | 李英劼 | The method that electroplating waste water resource utilizes |
| CN113707353A (en) * | 2020-12-25 | 2021-11-26 | 核工业北京化工冶金研究院 | Sponge iron filter material activation and reuse method |
| CN115440404A (en) * | 2021-06-03 | 2022-12-06 | 西南科技大学 | Method for treating high-temperature gas cooled reactor fuel element core preparation process wastewater by using novel functional fibers |
| CN115440404B (en) * | 2021-06-03 | 2024-04-26 | 西南科技大学 | Method for treating high-temperature gas cooled reactor fuel element core preparation process wastewater by using functionalized fibers |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103204601B (en) | 2014-05-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103204601B (en) | Wastewater treatment method | |
| CN104291489B (en) | The treatment process of high temperature gas-cooled Nuclear fuel core core preparation technology waste water | |
| KR101749159B1 (en) | Forward osmosis separation processes | |
| CN103193289B (en) | Method for recycling uranium in uranium-contained waste water | |
| CN103738984A (en) | Method and device for extracting bitten lithium chloride | |
| CN101659673B (en) | Processing technology for recovering and utilizing mother solution of glyphosate as resource | |
| CN103143325B (en) | Preparation method of glutamic acid intercalated layer hydrotalcite heavy-metal adsorbent | |
| CN103397212B (en) | Membrane technology-based ionic rare earth ore extraction technology and device therefor | |
| CN106947864B (en) | A kind of system and its processing method recycling heavy metal from discarded SCR catalyst | |
| CN110853790B (en) | Treatment method and treatment system for production waste liquid of high-temperature gas cooled reactor fuel element | |
| CN100564276C (en) | A kind of preparation method who removes the modified hydrotalcite of Trace Mercury in the water, cadmium ion | |
| CN111517530A (en) | Waste acid liquid regeneration pretreatment method and system | |
| CN103030123B (en) | Recovery and treatment equipment and process of waste diluted phosphoric acid containing metal salt | |
| CN101894597B (en) | Pretreatment method for radioactive wastewater | |
| CN106971767B (en) | A kind of processing method and processing device of high temperature gas cooled reactor fuel element production waste water | |
| CN204614460U (en) | Boron-containing radioactive waste liquid deep purifying reclaims the equipment of boric acid simultaneously | |
| CN203741054U (en) | Extracting device of lithium chloride in bittern | |
| CN204162529U (en) | A kind of ion type rareearth mine wastewater membrane isolation technique treatment unit | |
| CN101781035B (en) | Method for recovering terramycin from terramycin production wastewater. | |
| CN104810071B (en) | Method and equipment for deep purifying of boron-containing radioactive waste liquid and recovery of boric acid | |
| CN108751480A (en) | A kind of method and system of the industrial high-salt wastewater of processing | |
| CN113981253B (en) | Recovery method of americium-containing waste | |
| CN106140108B (en) | Polyantimonic acid/polyacrylonitrile composite ion exchanger and preparation method and application thereof | |
| CN204529535U (en) | A kind of wiring board water of productive use treatment unit | |
| CN103318920B (en) | Method for recovering ammonium nitrate from radioactive waste liquid |
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 |