CN110379532B - Method and device for treating radioactive waste liquid - Google Patents
Method and device for treating radioactive waste liquid Download PDFInfo
- Publication number
- CN110379532B CN110379532B CN201810333535.9A CN201810333535A CN110379532B CN 110379532 B CN110379532 B CN 110379532B CN 201810333535 A CN201810333535 A CN 201810333535A CN 110379532 B CN110379532 B CN 110379532B
- Authority
- CN
- China
- Prior art keywords
- reverse osmosis
- stage
- subunit
- radioactive waste
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/04—Treating liquids
- G21F9/06—Processing
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/04—Treating liquids
- G21F9/06—Processing
- G21F9/12—Processing by absorption; by adsorption; by ion-exchange
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention discloses a radioactive waste liquid treatment method and a radioactive waste liquid treatment device. The method comprises the following steps: separating the radioactive waste liquid to obtain a first purified liquid and a concentrated liquid; the concentrated solution is subjected to radionuclide removal treatment to obtain second purified solution, wherein the radionuclide removal treatment of the concentrated solution comprises the treatment of the concentrated solution by a chemical precipitation process; and discharging the first purifying liquid and the second purifying liquid. The radioactive waste liquid treatment method and the radioactive waste liquid treatment device have higher radioactive waste liquid purification level, can obviously reduce the production of radioactive waste and realize the small quantity of radioactive waste.
Description
Technical Field
The invention relates to the technical field of radioactive waste liquid treatment, in particular to a radioactive waste liquid treatment method and a radioactive waste liquid treatment device.
Background
According to the salt content, radioactive waste solutions can be divided into three main categories: (1) The salt content is 0 g.L -1 ～2g·L -1 Low salt content radioactive waste; (2) The salt content is 2 g.L -1 ～10g·L -1 Medium salt content radioactive waste; (3) The salt content reaches 10 g.L -1 The radioactive waste liquid with high salt content.
Since the difficulty in completely separating salt and radionuclide is great, in the treatment of radioactive waste liquid, the radioactive waste liquid having a low salt content is generally treated with salt and radionuclide together as the treatment object. However, for radioactive waste solutions with a high salt content, the ratio of the amount of non-radioactive salts to the amount of radionuclides is generally greater than 10 5 Even higher, the treatment of non-radioactive salts together with radionuclides as treatment targets results in a large proportion of the concentrate being non-radioactive salts, thereby greatly increasing the amount of secondary radioactive waste produced.
Therefore, a new radioactive waste liquid treatment method and device are needed to solve the above technical problems.
Disclosure of Invention
The embodiment of the invention provides a radioactive waste liquid treatment method and a radioactive waste liquid treatment device, which have higher purification level, and can obviously reduce the generation amount of radioactive waste and realize the small amount of radioactive waste.
The radioactive waste liquid treatment method and device provided by the embodiment of the invention are particularly suitable for treating radioactive waste liquid with high salt content.
In one aspect, an embodiment of the present invention provides a method for treating radioactive waste liquid, including: separating the radioactive waste liquid to obtain a first purified liquid and a concentrated liquid; removing radionuclides from the concentrated solution to obtain a second purified solution, wherein the removing radionuclides from the concentrated solution comprises the treatment of the concentrated solution by a chemical precipitation process; and discharging the first purifying liquid and the second purifying liquid.
According to the radioactive waste liquid treatment method provided by the embodiment of the invention, the radioactive waste liquid is separated to obtain the first purified liquid which accords with or even is superior to the emission standard, most of radioactive nuclides are reserved in the concentrated liquid, the concentrated liquid has higher radioactive nuclide concentration, the concentrated liquid is treated by a chemical precipitation process, only the radioactive nuclides are selectively removed, non-radioactive salt is discharged along with the purified liquid, and the radioactive concentrated liquid is not generated, so that the amount of the non-radioactive salt entering the radioactive waste is greatly reduced, and the generation amount of secondary radioactive waste is remarkably reduced. Compared with the method of directly carrying out chemical precipitation treatment on radioactive waste liquid, the radioactive waste liquid in the method of the invention is greatly concentrated, the volume of the radioactive waste liquid to be treated is greatly reduced, the concentration of target radionuclide ions to be removed in the concentrated solution is improved, and the decontamination factor of the chemical precipitation technology on the radionuclides can be greatly improved, thereby obviously reducing the production of radioactive waste.
According to one aspect of an embodiment of the invention, the radionuclide removal treatment of the concentrate further comprises an inorganic adsorption process treatment; wherein, the concentrated solution is treated by a chemical precipitation process and then treated by an inorganic adsorption process to obtain a second purified solution. The method is characterized in that most radionuclides are removed through chemical precipitation, and radionuclides which are not easy to remove through chemical precipitation in the concentrated solution are removed through selective inorganic adsorption, so that the purification level is further improved.
According to one aspect of the embodiment of the invention, the separation treatment adopts one or more than two of a nanofiltration process, a reverse osmosis process and a continuous electric desalting process, or adopts one or more than two of a nanofiltration process, a reverse osmosis process and a continuous electric desalting process and an ion exchange process.
According to one aspect of an embodiment of the present invention, separating the radioactive waste into a first purified liquid and a concentrated liquid comprises: the radioactive waste liquid is treated by a one-stage or two-stage reverse osmosis process.
According to one aspect of the embodiment of the invention, the reverse osmosis process adopts one or more than two stages of reverse osmosis treatment, and when the reverse osmosis treatment is adopted by more than two stages, the intermediate concentrated solution of the reverse osmosis treatment of the previous stage is used as the water for the reverse osmosis treatment of the next stage, and the purified solution is sent out from each stage to be converged into the purified solution of the reverse osmosis process of the stage.
According to one aspect of an embodiment of the present invention, a two-stage reverse osmosis process comprises: the radioactive waste liquid is treated by a first-stage reverse osmosis process and a second-stage reverse osmosis process in sequence, the second-stage reverse osmosis concentrated solution sent out by the second-stage reverse osmosis process is returned to the first-stage reverse osmosis process, and the concentrated solution is sent out from the first-stage reverse osmosis process.
According to one aspect of the embodiment of the invention, after the radioactive waste is treated by the one-stage or two-stage reverse osmosis process, the method further comprises: purifying liquid obtained by one-stage or two-stage reverse osmosis process treatment is treated by one-stage or two-stage continuous electric desalting process; or the purifying liquid obtained by the one-stage or two-stage reverse osmosis process is treated by more than one-stage ion exchange process.
According to one aspect of an embodiment of the present invention, a two-stage continuous electrodeionization process comprises: purifying liquid obtained by one-stage or two-stage reverse osmosis process treatment is sequentially subjected to a first-stage continuous electric desalting process and a second-stage continuous electric desalting process to obtain a first purifying liquid; and returning the first-stage continuous electric desalting concentrated solution sent by the first-stage continuous electric desalting process and the second-stage continuous electric desalting concentrated solution sent by the second-stage continuous electric desalting process to the first-stage or two-stage reverse osmosis process.
According to one aspect of an embodiment of the present invention, an activator is added to the intermediate cleaning solution from the first stage continuous electrodeionization process before it is fed to the second stage continuous electrodeionization process.
According to one aspect of the embodiments of the present invention, the volume of the radioactive waste is more than 2 times the volume of the concentrate, and the concentration of the radionuclide in the concentrate is more than 2 times the concentration of the radionuclide in the radioactive waste.
According to one aspect of the embodiments of the present invention, the radioactive waste is pre-treated to remove one or more of oils, colloids, particulates and/or to adjust pH prior to separation.
In another aspect, the embodiment of the invention provides a radioactive waste liquid treatment device, which comprises a separation unit, a chemical precipitation unit and a drainage unit, wherein a concentrated solution outlet of the separation unit is connected with an inlet of the chemical precipitation unit; the purifying liquid outlet of the separating unit and the purifying liquid outlet of the chemical precipitation unit are respectively connected to the drainage unit.
According to another aspect of an embodiment of the present invention, the apparatus further comprises an inorganic adsorption unit; the purified liquid outlet of the chemical precipitation unit is connected to the drainage unit through the inorganic adsorption unit.
According to another aspect of embodiments of the present invention, the separation unit comprises one or a combination of two or more of a nanofiltration subunit, a reverse osmosis subunit, a continuous electrodeionization subunit; alternatively, the separation unit comprises one or more of a nanofiltration subunit, a reverse osmosis subunit, a continuous electrodeionization subunit, and an ion exchange subunit in combination.
According to another aspect of an embodiment of the invention, the separation unit comprises a reverse osmosis subunit, wherein the reverse osmosis subunit comprises a one-stage or two-stage reverse osmosis device.
According to another aspect of embodiments of the present invention, the separation unit further comprises a continuous electric desalination subunit, the reverse osmosis subunit and the continuous electric desalination subunit being connected in sequence, wherein the continuous electric desalination subunit comprises one or two stages of continuous electric desalination equipment; alternatively, the separation unit further comprises an ion exchange subunit, the reverse osmosis subunit and the ion exchange subunit are connected in sequence, wherein the ion exchange subunit comprises more than one stage of ion exchanger.
According to another aspect of the embodiments of the present invention, the reverse osmosis apparatus employs one reverse osmosis membrane module or more than two reverse osmosis membrane modules in series, and when more than two reverse osmosis membrane modules are employed, the concentrate outlet of the previous reverse osmosis membrane module is connected to the inlet of the next reverse osmosis membrane module.
According to another aspect of the embodiments of the present invention, the reverse osmosis subunit comprises a first-stage reverse osmosis device, wherein the concentrate outlet of the reverse osmosis device is divided into two branches through a pipeline, one branch is connected with the inlet of the reverse osmosis device, and the other branch is connected with the inlet of the chemical precipitation unit; alternatively, the reverse osmosis subunit comprises a two-stage reverse osmosis device, wherein the concentrate outlet of the first-stage reverse osmosis device is divided into two branches through a pipeline, one branch is connected with the inlet of the first-stage reverse osmosis device, and the other branch is connected with the inlet of the chemical precipitation unit.
According to another aspect of embodiments of the present invention, the reverse osmosis subunit comprises a two-stage reverse osmosis device, wherein the purified liquid outlet of the first stage reverse osmosis device is connected to the inlet of the second stage reverse osmosis device, the concentrate outlet of the second stage reverse osmosis device is connected to the inlet of the first stage reverse osmosis device, and the concentrate outlet of the first stage reverse osmosis device is connected to the inlet of the chemical precipitation unit.
According to another aspect of the embodiments of the present invention, the continuous electric desalination subunit comprises a two-stage continuous electric desalination device, wherein the purified liquid outlet of the reverse osmosis subunit is connected to the inlet of the first-stage continuous electric desalination device, the purified liquid outlet of the first-stage continuous electric desalination device is connected to the inlet of the second-stage continuous electric desalination device, the purified liquid outlet of the second-stage continuous electric desalination device is connected to the drainage unit, and the concentrate liquid outlet of the first-stage continuous electric desalination device and the concentrate liquid outlet of the second-stage continuous electric desalination device are respectively connected to the inlet of the reverse osmosis subunit.
According to another aspect of the embodiments of the present invention, the purified liquid outlet of the first stage continuous electric desalting device is connected to the inlet of the second stage continuous electric desalting device via an intermediate water tank, and the intermediate water tank is connected to the activator tank.
According to another aspect of the embodiments of the present invention, the radioactive waste treatment apparatus further includes a pretreatment unit connected to the inlet of the separation unit for removing one or more of oil, colloid, and particulate matter from the radioactive waste and/or adjusting the pH.
Drawings
In order to more clearly illustrate the technical solution of the embodiments of the present invention, the drawings that are needed to be used in the embodiments of the present invention will be briefly described, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 shows a schematic process flow diagram of a radioactive waste treatment method according to an embodiment of the present invention.
Fig. 2 shows a schematic process flow diagram of a radioactive waste treatment method according to another embodiment of the present invention.
Fig. 3 shows a schematic process flow diagram of a radioactive waste treatment method according to still another embodiment of the present invention.
Fig. 4 shows a schematic process flow diagram of a radioactive waste treatment device according to an embodiment of the present invention.
Fig. 5 shows a schematic process flow diagram of a radioactive waste treatment device according to another embodiment of the present invention.
Fig. 6 shows a schematic process flow diagram of a radioactive waste treatment device according to still another embodiment of the present invention.
Fig. 7 shows a process flow diagram of a radioactive waste treatment device according to another embodiment of the present invention.
Description of the reference numerals:
10, a water inlet buffer tank;
20, a water supply pump;
100, a pretreatment unit;
101, an oil removal filter; 102, an inorganic membrane filter;
200, a separation unit;
201, a buffer water tank; 202, a cartridge filter; 203, a high pressure pump; 204, a buffer water tank; 205, a circulation pump;
210, a reverse osmosis subunit; 211, a first stage reverse osmosis device; 212, a second stage reverse osmosis device; 213, reverse osmosis apparatus;
221, a first stage continuous electrical desalination apparatus; 222, a second stage continuous electrical desalination apparatus; 223, a continuous electrodeionization device; 224, an intermediate tank; 225, an activator tank;
230, an ion exchange subunit;
310, a chemical precipitation unit; 311, chemical precipitation reactor;
320, an inorganic adsorption unit; 321, inorganic adsorption columns;
400, a drainage unit; 410, monitoring the discharge tank.
Detailed Description
Features and exemplary embodiments of various aspects of the present invention will be described in detail below, and in order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail below with reference to the accompanying drawings and examples. It should be understood that the specific embodiments described herein are merely configured to illustrate the invention and are not configured to limit the invention. It will be apparent to one skilled in the art that the present invention may be practiced without some of these specific details. The following description of the embodiments is merely intended to provide a better understanding of the invention by showing examples of the invention.
It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising … …" does not exclude the presence of other like elements in a process, method, article or apparatus that comprises the element.
The radioactive wastewater has extremely low mass concentration of radionuclide ions, and the concentration of the radionuclide ions is further reduced to achieve the radioactivity lower than 10Bq/L required by environmental emission, which puts high demands on the treatment capacity of the radioactive wastewater treatment technology. Some radioactive waste water contains non-radioactive salt up to 10g.L -1 Above, even higher, the prior art deals with non-radioactive salts together with radionuclides as treatment objects, so that the amount of secondary radioactive waste generated is greatly increased, and an important principle of radioactive wastewater treatment is to require a small amount of radioactive waste. In addition, operability and maintainability of the apparatus under radioactive conditions need to be considered.
Based on the above special requirements of radioactive wastewater treatment, the embodiment of the invention provides a radioactive waste liquid treatment method and a radioactive waste liquid treatment device, which have higher purification level, and simultaneously remarkably reduce the production of radioactive waste and realize the small quantity of radioactive waste.
Herein, "concentration factor" is calculated as (volume of water fed)/(volume of concentrate); the "removal rate" is calculated as (mass concentration of radionuclide in the feed water-mass concentration of radionuclide in the produced water)/(mass concentration of radionuclide in the feed water); "recovery" is calculated as (water yield)/(water inflow); "decontamination factor" is calculated as (radioactivity of the incoming water)/(radioactivity of the produced water).
The radioactive waste liquid treatment method and device provided by the embodiment of the invention are particularly suitable for treating radioactive waste liquid with high salt content.
Fig. 1 shows a schematic process flow diagram of a radioactive waste liquid treatment method according to an embodiment of the present invention, according to which:
firstly, radioactive wastewater is separated to obtain a first purifying liquid and a concentrated liquid. Wherein the concentration multiple can be more than 2 times, such as 2-10 times, most of radionuclides in the radioactive wastewater are reserved in the concentrated solution, so that the mass concentration of the radionuclides in the concentrated solution can reach more than 2 times of the mass concentration of the radionuclides in the radioactive waste liquid, the mass concentration of the radionuclides in the first purifying solution is lower than the mass concentration of the radionuclides in the radioactive wastewater, and the requirements of even being superior to emission standards are met, and the emission treatment is performed.
Further, the concentrated solution is subjected to radionuclide removal treatment to obtain a second purified solution. The method comprises the steps of treating the concentrated solution by a chemical precipitation process, and adding a chemical precipitant into the concentrated solution to promote the conversion of radionuclide ions into insoluble substances to precipitate out, so as to remove the radionuclides. The chemical precipitant may be one or more of carbonate, phosphate, sulfide, sulfate, hydroxide, metal oxide, oxalic acid, and oxalate, but is not limited thereto, so long as conversion of the radionuclide into a poorly soluble substance and precipitation thereof can be achieved. Since chemical precipitation only selectively removes radionuclides, but for the majority of non-radioactive ions such as Na in water + 、K + 、Cl - 、OH - And the like do not work, the non-radioactive salt is discharged together with the purifying liquid, and no radioactive concentrated waste liquid is generated, so that the amount of the non-radioactive salt entering the radioactive waste is greatly reduced, and the generation amount of secondary radioactive waste is obviously reduced. The adding amount of the chemical precipitant in the chemical precipitation is directly related to the ion concentration of the radionuclide in the solution and the removal rate required to be achieved, and as the concentrated solution has higher radionuclide concentration, the concentrated solution is treated by the chemical precipitation process, compared with the direct chemical precipitation treatment of radioactive waste liquid, the radioactive waste liquid is greatly concentrated, the volume of the radioactive waste liquid required to be treated is greatly reduced, the concentration of the target radionuclide ions required to be removed in the concentrated solution is increased, the decontamination factor of the chemical precipitation process on the radionuclide can be greatly increased, and the chemical precipitant required to achieve the same removal rate is greatly reduced, or the adding amount of the chemical precipitant is greatly reducedThe degree is improved, so that the amount of radioactive waste generated can be significantly reduced.
The radioactivity of the second purifying liquid is detected to meet the requirement of the emission standard, and then the emission treatment is carried out, wherein the first purifying liquid and the second purifying liquid can be respectively and directly emitted, namely the first purifying liquid is emitted through a pipeline, and the second purifying liquid is emitted through a II pipeline; the two may be mixed and discharged, that is, the second purified liquid is merged with the first purified liquid through the I-th pipeline, and then the water is discharged. And after detecting that the second purifying liquid is mixed with the first purifying liquid, the second purifying liquid meets the requirement of the emission standard, and then the second purifying liquid is mixed with the first purifying liquid through the I-th pipeline and then is subjected to emission treatment.
Chemical precipitation is often difficult to achieve high decontamination factors, and if the discharged second purification liquid is pursued to achieve a lower radioactivity, the water produced by the chemical precipitation process can be further subjected to selective inorganic adsorption to remove radionuclides, thereby increasing the decontamination factor for the radionuclides. Wherein, the concentrated solution is treated by the chemical precipitation process and then treated by the inorganic adsorption process, thus reducing the treatment load of the inorganic adsorption process.
According to some embodiments of the present invention, the separation treatment may be performed by using one or more of a nanofiltration process, a reverse osmosis process, and a continuous electric desalting process, or using one or more of a nanofiltration process, a reverse osmosis process, and a continuous electric desalting process in combination with an ion exchange process, according to the actual conditions of the components, the contents, and the treatment requirements of the radioactive wastewater.
When the separation treatment process adopts a reverse osmosis process, one-stage or two-stage reverse osmosis process may be adopted, but the separation treatment process is not limited thereto, and a three-stage reverse osmosis process may be adopted according to actual conditions.
As an example, the separation treatment process adopts a first-stage reverse osmosis process, specifically, the radioactive waste liquid is treated by the first-stage reverse osmosis process, so as to obtain a first-stage reverse osmosis purified liquid and a first-stage reverse osmosis concentrated liquid, which are respectively used as a first purified liquid and a concentrated liquid.
Alternatively, the reverse osmosis process may employ one or more than two stages of reverse osmosis treatment, and when employing more than two stages of reverse osmosis treatment, the intermediate concentrate of the reverse osmosis treatment of the previous stage is used as the water inlet of the reverse osmosis treatment of the next stage, that is, the radioactive waste liquid sequentially passes through the reverse osmosis treatments of more than two stages to obtain concentrate, and meanwhile, the purifying liquid of each stage is sent out, and the purifying liquids sent out from all stages are combined into the first-stage reverse osmosis purifying liquid, so that the recovery rate of reverse osmosis can be improved.
As another example, the separation treatment process adopts a two-stage reverse osmosis process to further increase the reverse osmosis purification level, specifically, the radioactive waste liquid is sent to the first-stage reverse osmosis process to be treated to obtain a first-stage reverse osmosis purified liquid and a first-stage reverse osmosis concentrated liquid, and then the first-stage reverse osmosis purified liquid is sent to the second-stage reverse osmosis process to be treated to obtain a second-stage reverse osmosis purified liquid and a second-stage reverse osmosis concentrated liquid. The second-stage reverse osmosis concentrated solution is returned to the first-stage reverse osmosis process, and the first-stage reverse osmosis concentrated solution is taken as the concentrated solution and is sent to the chemical precipitation process for treatment; the second-stage reverse osmosis purifying liquid is lower than 10Bq/L, meets the requirement of emission standard, and is used as the first purifying liquid for emission treatment.
Alternatively, the first stage reverse osmosis process may employ one or more than two stages of reverse osmosis treatment, and when two or more than two stages of reverse osmosis treatment are employed, the stage concentrate produced by the previous stage of reverse osmosis treatment is used as the water inlet for the next stage of reverse osmosis treatment, that is, the radioactive waste liquid sequentially passes through two or more than two stages of reverse osmosis treatment to obtain concentrate, and meanwhile, the stage of purifying liquid is sent from each stage, and the purifying liquids sent from all stages are combined into the first stage of reverse osmosis purifying liquid.
Alternatively, the second stage reverse osmosis process may employ one or more than two stages of reverse osmosis treatment, and similarly, when two or more than two stages of reverse osmosis treatment are employed, the stage concentrate produced by the previous stage of reverse osmosis treatment is used as the water inlet for the next stage of reverse osmosis treatment, that is, the radioactive waste liquid sequentially passes through the two or more stages of reverse osmosis treatment, so as to obtain the second stage reverse osmosis concentrate, and meanwhile, the stage of purifying liquid is sent from each stage, and the purifying liquids sent from all stages are combined into the second stage reverse osmosis purifying liquid.
As an alternative scheme, the first-stage reverse osmosis process and the second-stage reverse osmosis process both adopt three-stage reverse osmosis treatment, and the two-stage three-stage reverse osmosis process is formed to separate radioactive wastewater, so that the method has higher purifying capacity and concentration multiple, reduces the load of a chemical precipitation treatment procedure, and improves the recovery rate.
When the radioactivity of the first purifying liquid discharged by the first reverse osmosis process or the second purifying liquid discharged by the second reverse osmosis process is more than 10Bq/L, or if the radioactivity of the first purifying liquid discharged by the first reverse osmosis process can reach lower radioactivity, the first purifying liquid discharged by the first reverse osmosis process or the second purifying liquid discharged by the second reverse osmosis process can be further finely processed by a continuous electric desalting process (shown in figure 2) or an ion exchange process (shown in figure 3).
As an example, the first purifying liquid is obtained by carrying out fine treatment on the first reverse osmosis purifying liquid produced by the first reverse osmosis process or the second reverse osmosis purifying liquid produced by the second reverse osmosis process through a first-stage continuous electric desalting process, the first purifying liquid often reaches the requirement of emission standard, even reaches the natural background level, almost contains no radionuclide, the emission treatment is carried out, and the produced first-stage continuous electric desalting concentrated liquid is returned to the first-stage reverse osmosis process in the first-stage reverse osmosis process or the second-stage reverse osmosis process.
In order to improve the purification level of the continuous electric desalting process, an activating agent can be added into the first-stage reverse osmosis purified liquid produced by the first-stage reverse osmosis process or the second-stage reverse osmosis purified liquid produced by the second-stage reverse osmosis process, and then the activating agent is sent into the first-stage continuous electric desalting process for deep purification treatment. The activator can be prepared from pure water with resistivity greater than 0.5MΩ cm and inorganic salts of different kinds, and contains ion Ca 2+ 、Na + 、Sr 2+ 、Zn 2+ 、Mg 2+ 、Fe 2+ And K + The concentration of the active agent stock solution is related to the dosage, so that the ions contained in the radioactive wastewater are ensured after the active agent is added into the radioactive wastewater and uniformly mixedThe concentrations were as follows: ca (Ca) 2+ 0.1mg/L～0.2mg/L、Na + 0.2mg/L～0.3mg/L、Sr 2+ 8mg/L～9mg/L、Zn 2+ 18mg/L～20mg/L、Mg 2+ 0.2mg/L～0.25mg/L、Fe 2+ 0.04mg/L to 0.05mg/L and K + 100mg/L～150mg/L。
As another example, the first-stage reverse osmosis purified liquid produced by the first-stage reverse osmosis process or the second-stage reverse osmosis purified liquid produced by the second-stage reverse osmosis process is subjected to fine treatment by a two-stage continuous electric desalting process, specifically, the first-stage reverse osmosis purified liquid produced by the first-stage reverse osmosis process or the second-stage reverse osmosis purified liquid produced by the two-stage reverse osmosis process is sent to the first-stage continuous electric desalting process to be treated to obtain the first-stage continuous electric desalting purified liquid and the first-stage continuous electric desalting concentrated liquid, and then the first-stage continuous electric desalting purified liquid is sent to the second-stage continuous electric desalting process to be treated to obtain the second-stage continuous electric desalting purified liquid and the second-stage continuous electric desalting concentrated liquid, wherein the second-stage continuous electric desalting purified liquid is the first purified liquid, and often reaches the requirements of discharge standards even reaches the natural background level, and is returned to the first-stage reverse osmosis process in the first-stage reverse osmosis process or the second-stage reverse osmosis process.
Similarly, in order to further improve the purification level of the continuous electric desalting process, an activating agent can be added into the first-stage continuous electric desalting purifying liquid, and then the activating agent is sent into the second-stage continuous electric desalting process for purifying treatment. The activator may be as described above.
The fine treatment may also be an ion exchange process employing more than one stage. Purifying liquid obtained by one-stage or two-stage reverse osmosis process treatment is treated by more than one-stage ion exchange process in sequence to obtain first purifying liquid.
It will be appreciated that the separation process is not limited to the above process, but may be a continuous electrodeionization process of more than one stage; nanofiltration-reverse osmosis combined process; nanofiltration-continuous electric desalting combined process; nanofiltration-reverse osmosis-continuous electric desalting combined process; nanofiltration-reverse osmosis-ion exchange combined process, etc., and can be determined according to practical situations by those skilled in the art.
Optionally, the radioactive waste is pretreated prior to the separation treatment, but this is not a necessary procedure.
Besides radionuclides and inorganic salts, the radioactive wastewater can also contain impurities such as oils, colloids, particles and the like, most of the impurities are nonradioactive, but the impurities can affect reverse osmosis, chemical precipitation, inorganic adsorption and other processes, and the pretreatment can remove the impurities, so that the service cycle of a reverse osmosis membrane and an inorganic adsorbent can be prolonged, the replacement of the reverse osmosis membrane and the inorganic adsorbent can be reduced, the efficiency of the chemical precipitant can be improved, and the production of the radioactive waste inorganic adsorbent and the production of radioactive chemical precipitates can be further reduced.
The pH value of the radioactive wastewater can be adjusted to 6-8 in advance, so that the treatment effect of the reverse osmosis process is better, and the reverse osmosis membrane has longer service life.
In order to implement the radioactive waste treatment method, an embodiment of the present invention further provides a radioactive waste treatment apparatus, which is described in detail below with reference to fig. 4 to 7.
Fig. 4 shows a schematic process flow diagram of a radioactive waste treatment device according to an embodiment of the present invention. The device comprises a separation unit 200, a chemical precipitation unit 310 and a drainage unit 400, wherein a concentrated solution outlet of the separation unit 200 is connected with an inlet of the chemical precipitation unit 310; the purified liquid outlets of the separation unit 200 and the chemical precipitation unit 310 are connected to the drain unit 400, respectively.
As an example, the drainage unit 400 includes a first drainage subunit and a second drainage subunit (not shown in the drawing), the purified liquid outlet of the separation unit 200 is connected to the first drainage subunit, the purified liquid outlet of the chemical precipitation unit 310 is connected to the second drainage subunit, and the first drainage subunit and the second drainage subunit may be in communication therebetween. Thus, when the radioactivity of the second purifying liquid meets the requirement of the emission standard through detection, the first purifying liquid and the second purifying liquid can be directly emitted respectively according to different requirements, or the two purifying liquids can be emitted after being mixed; and when the requirement of the emission standard is met after the second purifying liquid is detected to be mixed with the first purifying liquid, the second purifying liquid is mixed with the first purifying liquid and then is discharged.
It will be appreciated that the drain unit 400 may be a drain line alone, or a monitor drain tank 410 (as shown in fig. 6 and 7) may be connected to the drain line to monitor the radioactivity of the drain, or other forms of draining the cleaning solution, as the present invention is not limited.
If a higher decontamination factor is sought, the device further comprises an inorganic adsorption unit 320; the purified liquid outlet of the chemical precipitation unit 310 is connected to the drainage unit 400 through the inorganic adsorption unit 320.
Referring to fig. 6 and 7, the chemical precipitation unit 310 may be an integrated precipitation device capable of performing chemical dosing, chemical precipitation reaction and separation, and the chemical precipitant may be one or more of carbonate, phosphate, sulfide, sulfate, hydroxide, metal oxide, oxalic acid, and oxalate, but is not limited thereto, so long as the conversion of the radionuclide into insoluble substances and precipitation can be achieved.
Referring to fig. 6 and 7, according to some embodiments of the present invention, the inorganic adsorption unit 320 employs an inorganic adsorption column 321, and may employ one or more of an inorganic adsorption column for strontium, an inorganic adsorption column for cesium, and an inorganic adsorption column for strontium and cesium.
According to some embodiments of the invention, separation unit 200 comprises one or a combination of two or more of a nanofiltration subunit, a reverse osmosis subunit, a continuous electrodeionization subunit. According to further embodiments of the present invention, separation unit 200 comprises a combination of one or more of a nanofiltration subunit, a reverse osmosis subunit, a continuous electrodeionization subunit, and an ion exchange subunit.
As an example, referring to fig. 5 to 7, the separation unit 200 includes a reverse osmosis subunit 210, and one or two stages of reverse osmosis devices are used in the reverse osmosis subunit 210, but not limited thereto, and three stages of reverse osmosis devices may be used according to actual situations.
In some embodiments, referring to FIG. 6, a first stage reverse osmosis unit is employed in reverse osmosis subunit 210, with the concentrate outlet of reverse osmosis unit 213 connected to the inlet of chemical precipitation unit 310. The purified liquid sent from the reverse osmosis apparatus 213 is already below 10Bq/L, meets the requirements of the discharge standard, and a discharge process can be performed, at which time the purified liquid outlet of the reverse osmosis apparatus 213 is connected to the drain unit 400.
To increase the recovery rate of reverse osmosis, the concentrate outlet of the reverse osmosis apparatus 213 is divided into two branches via a pipe, one branch being connected to the inlet of the reverse osmosis apparatus 213 and the other branch being connected to the inlet of the chemical precipitation unit 310. Thus, the discharge amount of the concentrated solution is reduced, the load of the chemical precipitation unit 310 is reduced, the utilization rate of the chemical precipitant is further improved, the energy waste is avoided, and the energy consumption is saved.
Further, the reverse osmosis device 213 may adopt one reverse osmosis membrane module or more than two reverse osmosis membrane modules connected in series, when more than two reverse osmosis membrane modules are adopted, the concentrate outlet of the previous reverse osmosis membrane module is connected with the inlet of the next reverse osmosis membrane module, that is, the stage concentrate produced by the previous reverse osmosis membrane module is used as the water inlet of the next reverse osmosis membrane module, and the stage purified liquid sent by all the reverse osmosis membrane modules is merged into the purified liquid of the reverse osmosis device 213.
In some embodiments, referring to the process flow chart of the radioactive waste liquid treatment apparatus provided in one embodiment of the present invention shown in fig. 7, the reverse osmosis subunit 210 adopts two-stage reverse osmosis devices, wherein the first-stage reverse osmosis device 211 and the second reverse osmosis device 212 are connected in series in two stages, specifically, the purified liquid outlet of the first-stage reverse osmosis device 211 is connected to the inlet of the second-stage reverse osmosis device 212, the concentrate outlet of the second-stage reverse osmosis device 212 is connected to the inlet of the first-stage reverse osmosis device 211, and the concentrate outlet of the first-stage reverse osmosis device 211 is connected to the inlet of the chemical precipitation unit 310. The purified liquid sent from the second stage reverse osmosis unit 212 is less than 10Bq/L, meets the requirements of the discharge standard, and can be discharged, and at this time, the purified liquid outlet of the first stage reverse osmosis unit 212 is connected to the drain unit 400.
To increase the recovery rate of reverse osmosis, the concentrate outlet of the first stage reverse osmosis apparatus 211 is divided into two branches through a pipe, one branch is connected to the inlet of the first stage reverse osmosis apparatus 211, and the other branch is connected to the inlet of the chemical precipitation unit 310. Thus, the discharge amount of the concentrated solution is reduced, the load of the chemical precipitation unit 310 is reduced, the utilization rate of the chemical precipitant is further improved, the energy waste is avoided, and the energy consumption is saved.
Further, the first stage reverse osmosis device 211 may adopt one reverse osmosis membrane module or more than two reverse osmosis membrane modules connected in series, when more than two reverse osmosis membrane modules are adopted, the concentrate outlet of the previous reverse osmosis membrane module is connected with the inlet of the next reverse osmosis membrane module, that is, the stage concentrate produced by the previous reverse osmosis membrane module is used as the water inlet of the next reverse osmosis membrane module, and the stage purified liquid sent by all the reverse osmosis membrane modules is converged into the purified liquid of the first stage reverse osmosis device 211.
The second-stage reverse osmosis device 212 may be a reverse osmosis device with one reverse osmosis membrane module or more than two reverse osmosis membrane modules connected in series, and similarly, when more than two reverse osmosis membrane modules are adopted, the concentrate outlet of the previous reverse osmosis membrane module is connected with the inlet of the next reverse osmosis membrane module, that is, the stage concentrate produced by the previous reverse osmosis membrane module is used as the water inlet of the next reverse osmosis membrane module, and the stage purified liquid sent by all the reverse osmosis membrane modules is converged into the purified liquid of the second-stage reverse osmosis device 212.
As an alternative, the first stage reverse osmosis device 211 and the second stage reverse osmosis device 212 are all connected in series by adopting three-section reverse osmosis membrane components, so that the two-stage three-section reverse osmosis subunit 210 is formed to perform the separation treatment of radioactive wastewater, has higher purifying capacity and concentration multiple, reduces the load of the chemical precipitation unit 310, and improves the recovery rate of reverse osmosis.
When the radioactivity of the first-stage reverse osmosis purified liquid produced by the first-stage reverse osmosis apparatus or the second-stage reverse osmosis purified liquid produced by the second-stage reverse osmosis apparatus is greater than 10Bq/L, or when the discharged purified liquid is pursued to achieve lower radioactivity, a continuous electric desalting subunit (shown in fig. 6 and 7) or an ion exchange subunit 230 (shown in fig. 5) can be further arranged at the downstream of the reverse osmosis subunit, and the first-stage reverse osmosis purified liquid produced by the first-stage reverse osmosis apparatus or the second-stage reverse osmosis purified liquid produced by the second-stage reverse osmosis process can be sent to the continuous electric desalting subunit or the ion exchange subunit 230 for further fine treatment.
In some embodiments, referring to fig. 6, the continuous electric desalination subunit employs a first-stage continuous electric desalination device, wherein the purified liquid outlet of the reverse osmosis subunit 210 is connected to the inlet of the continuous electric desalination device 223, the purified liquid outlet of the continuous electric desalination device 223 is connected to the drainage unit 400, and the concentrated liquid outlet of the continuous electric desalination device 223 is connected to the inlet of the reverse osmosis subunit 210. When the reverse osmosis subunit 210 employs a first-stage reverse osmosis apparatus, referring to fig. 6, the inlet of the reverse osmosis subunit 210 refers to the inlet of the reverse osmosis apparatus 213; when the reverse osmosis subunit 210 employs a two-stage reverse osmosis apparatus, referring to fig. 7, the inlet of the reverse osmosis subunit 210 refers to the inlet of the first stage reverse osmosis apparatus 211.
In some embodiments, referring to fig. 7, the continuous electric salt removal subunit employs a two-stage continuous electric salt removal device, wherein the first-stage continuous electric salt removal device 221 is connected in series with the second-stage continuous electric salt removal device 222, specifically, a purified liquid outlet of the reverse osmosis subunit 210 is connected to an inlet of the first-stage continuous electric salt removal device 221, a purified liquid outlet of the first-stage continuous electric salt removal device 221 is connected to an inlet of the second-stage continuous electric salt removal device 222, a purified liquid outlet of the second-stage continuous electric salt removal device 222 is connected to the drainage unit 400, and a concentrated liquid outlet of the first-stage continuous electric salt removal device 221 and a concentrated liquid outlet of the second-stage continuous electric salt removal device 222 are respectively connected to an inlet of the reverse osmosis subunit 210.
In order to increase the purification level of the continuous electric desalination subunit, when the continuous electric desalination subunit employs a first-stage continuous electric desalination device, an intermediate water tank may be connected between the reverse osmosis subunit and the continuous electric desalination subunit, the intermediate water tank being connected to the activator tank. In this way, in the purified liquid sent out by the reverse osmosis subunit, for example, the first-stage reverse osmosis purified liquid produced by the first-stage reverse osmosis equipment or the second-stage reverse osmosis purified liquid produced by the second-stage reverse osmosis equipment, an activating agent is added, and then the mixed liquid is sent into the first-stage continuous electric desalting equipment for deep purification treatment. When the continuous electric salt removing subunit is connected in series by adopting two-stage continuous electric salt removing equipment, referring to fig. 7, an intermediate water tank 224 may be connected between the first-stage continuous electric salt removing equipment 221 and the second-stage continuous electric salt removing equipment 222, the intermediate water tank 224 is connected with an activator tank 225, and a dosing pump is arranged to control the adding amount of the activator, so that the purified liquid produced after the treatment of the continuous electric salt removing subunit reaches the natural background level.
The ion exchange subunit 230 may be subjected to fine processing by using ion exchangers of more than one stage in series, and may be used by using ion exchangers of one stage, two stages, three stages, four stages or more stages according to practical situations.
As shown in fig. 4, a pretreatment unit 100 may also be provided upstream of the separation unit 200, but is not required. The pretreatment unit 100 may be one or a combination of several of an oil removal filter, an activated carbon filter, an inorganic membrane filter, a cartridge filter, a paper core filter, a self-cleaning filter, and an ultra-filter, if necessary.
Besides radionuclides and inorganic salts, the radioactive wastewater contains oil, colloid, particulate matters and other impurities, most of which are nonradioactive, but the subsequent process is influenced, and the pretreatment can remove the impurities, so that the service cycle of reverse osmosis membranes and inorganic adsorbents can be prolonged, the replacement of the inorganic adsorbents and reverse osmosis membranes can be reduced, the utilization rate of chemical precipitants can be improved, and the production of the radioactive waste inorganic adsorbents and the production of radioactive chemical precipitated sludge can be further reduced. The oil removal filter 101 can stably remove oil in the radioactive wastewater for a long time, the inorganic membrane filter 102 can further remove oil in the radioactive wastewater, colloid and particulate matters in the radioactive wastewater can also be effectively removed, as shown in fig. 5 to 7, the oil removal filter 101 and the inorganic membrane filter 102 are sequentially connected, so that the radioactive wastewater is pretreated, the turbidity removal capability is high, and pretreatment process equipment and flow are simplified.
The separation unit 200 further includes a buffer tank 201 to buffer radioactive wastewater from the pretreatment unit 100. A cartridge filter 202 is further connected between the buffer tank 201 and the reverse osmosis subunit 210 for protecting the reverse osmosis equipment of the subsequent process. The separation unit 200 may also include a buffer tank 204 to buffer the purified liquid sent from the reverse osmosis subunit 210.
The apparatus further includes a suitable water supply pump 20, a high pressure pump 203 and a circulation pump 205, which may be various pumps commonly used in the art, such as a plunger pump, a centrifugal pump, etc. The apparatus may also include an influent buffer tank 10 to buffer radioactive wastewater.
The radioactive waste water device provided by the embodiment of the invention can be used for implementing the radioactive waste water method so as to realize high radioactive waste liquid purification level, and simultaneously can remarkably reduce the generation amount of radioactive waste and realize the small amount of radioactive waste.
The invention is illustrated below by means of examples, which in no way constitute a limitation of the invention.
In the following examples ion concentrations were determined using an inductively coupled plasma-mass spectrometry ICP-MS instrument and oil concentrations were characterized using a total organic carbon TOC analyzer.
Example 1
The radioactive wastewater treatment apparatus used in this example is different from the apparatus shown in fig. 6 in that the continuous electric desalting device 223 is not provided, i.e., the purified liquid outlet of the reverse osmosis device 213 is directly connected to the monitor discharge tank 410, and the other parts are the same as the apparatus shown in fig. 6. Wherein, reverse osmosis equipment 213 is three-stage reverse osmosis equipment formed by three reverse osmosis membrane components connected in series, chemical precipitation reactor 311 adopts integrated precipitation equipment, and inorganic membrane filter 102 adopts ceramic membrane.
The simulated radioactive wastewater treated in this example contains Cs + 10mg/L，Sr 2+ 10mg/L of NaCl 10g/L and oil content of 100ppm.
The design throughput of the radioactive wastewater treatment device is 1m 3 /h。
After the simulated radioactive wastewater passes through the oil removal filter 101, the oil content is reduced from 100ppm to 5ppm, and after the simulated radioactive wastewater further passes through the inorganic membrane filter 102, the oil content is reduced to 1ppm, so that the subsequent water inlet condition is met.
The reverse osmosis operation pressure is 5MPa, the simulated radioactive wastewater is highly concentrated by a primary reverse osmosis process, the reverse osmosis recovery rate is set to 80%, the concentration multiple is 5 times, the radionuclide concentration in the concentrated solution is improved by 5 times, wherein Cs is contained in the concentrated solution + The concentration is 49mg/L, sr 2+ The concentration of (C) was 50mg/L and the NaCl concentration was 49.5g/L. According to the principle of chemical precipitation, under the condition of a certain solubility product Ksp, when the concentration of cations is increased by 5 times, the concentration of the required anionic medicament can be reduced by 5 times, and simultaneously, as the water quantity of the concentrated solution is reduced to 1/5 of the original water quantity, the use amount of the chemical precipitant is reduced to 1/25 of the original required amount, the decontamination factor of the chemical precipitation technology on the radionuclides can be greatly improved, and the production amount of radioactive solid waste is greatly reduced.
The chemical precipitation reaction can be performed in an integrated precipitation device due to the reduction of the amount of water to be treated, and the chemical precipitant can be one or a combination of more than two of ferrous hydroxide, calcium carbonate, manganese dioxide, barium sulfate and the like, and in the embodiment, the chemical precipitant is calcium carbonate. Chemical precipitation of Sr 2+ The concentration of (2) is reduced to 0.5mg/L, and the chemical precipitation process has no removal effect on NaCl, and the concentration of NaCl is maintained at 49.5g/L after chemical precipitation, so that NaCl is not present in the solid waste, thereby reducing the content of the solid waste.
Cs due to chemical precipitation process + The decontamination effect of the water produced by the chemical precipitation process is lower, and the water produced by the chemical precipitation process is further sent into a cesium adsorption bed to be subjected to inorganic adsorption to remove cesium, so that the decontamination factor reaches 10 3 Cs in water produced by inorganic adsorption process (namely second purifying liquid) + The concentration is reduced to 49 mug/L, sr 2+ The concentration of (C) is 0.5mg/L, the concentration of NaCl is 49.5g/L, and the water yield is 0.2m 3 /h。
Cs in water produced by reverse osmosis process (namely first purified liquid) + The concentration is 100 mug/L, sr 2+ The concentration of (2) was 10. Mu.g/L, and the concentration of NaCl was 0.125g/L, water yield of 0.8m 3 And/h. The first purifying liquid and the second purifying liquid are mixed and discharged, and Cs is monitored + The concentration is 89.8 mug/L, sr 2+ The concentration of (2) was 108. Mu.g/L and the concentration of NaCl was 10g/L, and the decontamination factor for cesium and strontium was about 100.
A continuous electrodeionization device can also be provided after reverse osmosis device 213 to achieve higher decontamination factors.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes and substitutions of equivalents may be made without departing from the spirit and scope of the invention.
Claims (20)
1. A method for treating radioactive waste, the method comprising:
separating the radioactive waste liquid to obtain a first purified liquid and a concentrated liquid;
removing radionuclides from the concentrated solution to obtain a second purified solution; wherein the radionuclide removal treatment of the concentrated solution comprises chemical precipitation treatment and inorganic adsorption treatment of the concentrated solution; the concentrated solution is treated by the chemical precipitation process, and a chemical precipitator is added into the concentrated solution to promote the conversion of radionuclide ions into insoluble substances to precipitate out, so that the radionuclides are removed, and then the concentrated solution is treated by the inorganic adsorption process to further selectively remove the radionuclides through selective inorganic adsorption to obtain the second purifying solution;
And discharging the first purifying liquid and the second purifying liquid.
2. The method according to claim 1, wherein the separation treatment is performed by one or a combination of two or more of a nanofiltration process, a reverse osmosis process and a continuous electric desalting process, or by a combination of one or more of a nanofiltration process, a reverse osmosis process and a continuous electric desalting process and an ion exchange process.
3. The method of claim 1, wherein separating the radioactive waste to obtain a first purified solution and a concentrated solution comprises: the radioactive waste liquid is treated by a one-stage or two-stage reverse osmosis process.
4. A method according to claim 3, wherein the reverse osmosis process employs one or more stages of reverse osmosis treatment, and when employing more than two stages of reverse osmosis treatment, the intermediate concentrate of the upper stage of reverse osmosis treatment is used as the feed water for the next stage of reverse osmosis treatment, and the purified liquid is fed from each stage to be combined into the purified liquid of the reverse osmosis process.
5. A method according to claim 3, wherein the two-stage reverse osmosis process treatment comprises:
the radioactive waste liquid is sequentially treated by a first-stage reverse osmosis process and a second-stage reverse osmosis process, the second-stage reverse osmosis concentrated solution sent out by the second-stage reverse osmosis process is returned to the first-stage reverse osmosis process, and the concentrated solution is sent out from the first-stage reverse osmosis process.
6. The method of claim 3, wherein said subjecting the radioactive waste to one or more stages of reverse osmosis further comprises:
purifying liquid obtained by the one-stage or two-stage reverse osmosis process is treated by a one-stage or two-stage continuous electric desalting process;
or the purifying liquid obtained by the one-stage or two-stage reverse osmosis process is treated by more than one-stage ion exchange process.
7. The method of claim 6, wherein the two-stage continuous electrodeionization process treatment comprises:
the purifying liquid obtained by the one-stage or two-stage reverse osmosis process is sequentially subjected to a first-stage continuous electric desalting process and a second-stage continuous electric desalting process to obtain the first purifying liquid; and returning the first-stage continuous electric desalting concentrated solution sent by the first-stage continuous electric desalting process and the second-stage continuous electric desalting concentrated solution sent by the second-stage continuous electric desalting process to the one-stage or two-stage reverse osmosis process.
8. The method of claim 7, wherein an activator is added to the intermediate cleaning solution from the first stage continuous electrodeionization process before it is fed to the second stage continuous electrodeionization process.
9. The method of claim 1, wherein the volume of the radioactive waste is greater than 2 times the volume of the concentrate, and the concentration of the radionuclide in the concentrate is greater than 2 times the concentration of the radionuclide in the radioactive waste.
10. The method of claim 1, wherein the radioactive waste is pre-treated to remove one or more of oils, colloids, particulates and/or to adjust pH prior to the separation process.
11. A radioactive waste liquid treatment device is characterized by comprising a separation unit, a chemical precipitation unit, an inorganic adsorption unit and a drainage unit,
wherein the concentrated solution outlet of the separation unit is connected with the inlet of the chemical precipitation unit;
the purifying liquid outlet of the chemical precipitation unit is connected with the inlet of the inorganic adsorption unit;
the purified liquid outlet of the separation unit and the purified liquid outlet of the inorganic adsorption unit are respectively connected to the drainage unit.
12. The apparatus of claim 11, wherein the separation unit comprises one or a combination of two or more of a nanofiltration subunit, a reverse osmosis subunit, a continuous electrodeionization subunit; alternatively, the separation unit comprises one or more of a nanofiltration subunit, a reverse osmosis subunit, a continuous electrodeionization subunit, and an ion exchange subunit in combination.
13. The apparatus of claim 12, wherein the separation unit comprises a reverse osmosis subunit, wherein the reverse osmosis subunit comprises a one-stage or two-stage reverse osmosis device.
14. The apparatus of claim 13, wherein the separation unit further comprises a continuous electrical desalination subunit, the reverse osmosis subunit and the continuous electrical desalination subunit being connected in sequence, wherein the continuous electrical desalination subunit comprises one or two stages of continuous electrical desalination equipment; or alternatively, the process may be performed,
the separation unit further comprises an ion exchange subunit, wherein the reverse osmosis subunit and the ion exchange subunit are sequentially connected, and the ion exchange subunit comprises more than one stage of ion exchangers.
15. The apparatus according to claim 13 or 14, wherein the reverse osmosis device is a single reverse osmosis membrane module or two or more reverse osmosis membrane modules connected in series, and when two or more reverse osmosis membrane modules are used, the concentrate outlet of the previous reverse osmosis membrane module is connected to the inlet of the next reverse osmosis membrane module.
16. The apparatus according to claim 13 or 14, wherein the reverse osmosis subunit comprises a primary reverse osmosis device, the concentrate outlet of which is divided into two branches by a pipe, one branch being connected to the inlet of the reverse osmosis device and the other branch being connected to the inlet of the chemical precipitation unit; or alternatively, the process may be performed,
The reverse osmosis subunit comprises two stages of reverse osmosis equipment, wherein a concentrated solution outlet of the first stage of reverse osmosis equipment is divided into two branches through a pipeline, one branch is connected with an inlet of the first stage of reverse osmosis equipment, and the other branch is connected with an inlet of the chemical precipitation unit.
17. The apparatus of claim 13 or 14, wherein the reverse osmosis subunit comprises a two-stage reverse osmosis device, wherein the purified liquid outlet of the first stage reverse osmosis device is connected to the inlet of the second stage reverse osmosis device, the concentrate outlet of the second stage reverse osmosis device is connected to the inlet of the first stage reverse osmosis device, and the concentrate outlet of the first stage reverse osmosis device is connected to the inlet of the chemical precipitation unit.
18. The apparatus of claim 14, wherein the continuous electric desalination subunit comprises a two-stage continuous electric desalination device, wherein the purified liquid outlet of the reverse osmosis subunit is connected to the inlet of the first-stage continuous electric desalination device, the purified liquid outlet of the first-stage continuous electric desalination device is connected to the inlet of the second-stage continuous electric desalination device, the purified liquid outlet of the second-stage continuous electric desalination device is connected to the drainage unit, and the concentrate liquid outlet of the first-stage continuous electric desalination device and the concentrate liquid outlet of the second-stage continuous electric desalination device are connected to the inlet of the reverse osmosis subunit, respectively.
19. The apparatus of claim 18, wherein the purified liquid outlet of the first stage continuous electric desalination device is connected to the inlet of the second stage continuous electric desalination device via an intermediate water tank, the intermediate water tank being connected to the activator tank.
20. The apparatus of claim 11, further comprising a pretreatment unit coupled to the inlet of the separation unit for removing one or more of oils, colloids, and particulates from the radioactive waste and/or for adjusting pH.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810333535.9A CN110379532B (en) | 2018-04-13 | 2018-04-13 | Method and device for treating radioactive waste liquid |
| PCT/CN2018/085069 WO2019196143A1 (en) | 2018-04-13 | 2018-04-28 | Radioactive waste liquid treatment method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810333535.9A CN110379532B (en) | 2018-04-13 | 2018-04-13 | Method and device for treating radioactive waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110379532A CN110379532A (en) | 2019-10-25 |
| CN110379532B true CN110379532B (en) | 2023-08-25 |
Family
ID=68163875
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810333535.9A Active CN110379532B (en) | 2018-04-13 | 2018-04-13 | Method and device for treating radioactive waste liquid |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN110379532B (en) |
| WO (1) | WO2019196143A1 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111768885B (en) * | 2020-06-10 | 2022-07-26 | 清华大学 | Radioactive waste liquid treatment system and method |
| CN112340917B (en) * | 2020-11-04 | 2023-12-22 | 江汉大学 | Method and system for treating radioactive wastewater |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59204796A (en) * | 1983-05-09 | 1984-11-20 | 株式会社東芝 | Method of processing torus water |
| CN103177784A (en) * | 2013-03-28 | 2013-06-26 | 清华大学 | Method for treating radioactive wastewater |
| JP2013156130A (en) * | 2012-01-30 | 2013-08-15 | Hitachi-Ge Nuclear Energy Ltd | Radioactive waste liquid treatment method and radioactive waste liquid treatment apparatus |
| JP2014119417A (en) * | 2012-12-19 | 2014-06-30 | Hitachi-Ge Nuclear Energy Ltd | Method for treating radioactive waste liquid |
| CN105018754A (en) * | 2014-04-17 | 2015-11-04 | 上海凯鑫分离技术有限公司 | Extraction technology of ion-absorbed rare earth mine |
| CN105244068A (en) * | 2015-08-31 | 2016-01-13 | 中国核电工程有限公司 | Device and method for treating high-salt content radioactive waste liquid |
| CN205451799U (en) * | 2016-02-17 | 2016-08-10 | 杭州上拓环境科技有限公司 | Processing system of uranium ore waste water |
| CN212181940U (en) * | 2019-12-02 | 2020-12-18 | 国家电投集团远达环保工程有限公司重庆科技分公司 | High salt content radioactive waste water's processing apparatus |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6739802B2 (en) * | 2002-07-11 | 2004-05-25 | Bga Limited Partnership | Fish test circuit and method for evaluation of waterway barrier fish bypass systems |
| JP6090095B2 (en) * | 2013-10-03 | 2017-03-08 | Ｊｆｅエンジニアリング株式会社 | Fly ash cleaning device and fly ash cleaning method |
| CN203631141U (en) * | 2013-11-07 | 2014-06-04 | 中国核电工程有限公司 | Reverse osmosis treatment device for nuclear power plant waste liquid treatment system |
| CN103745759B (en) * | 2014-01-09 | 2017-01-18 | 清华大学 | Method and device for processing radioactive wastewater |
| CN104900286B (en) * | 2015-05-26 | 2018-02-06 | 清华大学 | By Spent Radioactive water process to the horizontal system of natural background radioactivity and application |
-
2018
- 2018-04-13 CN CN201810333535.9A patent/CN110379532B/en active Active
- 2018-04-28 WO PCT/CN2018/085069 patent/WO2019196143A1/en active Application Filing
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59204796A (en) * | 1983-05-09 | 1984-11-20 | 株式会社東芝 | Method of processing torus water |
| JP2013156130A (en) * | 2012-01-30 | 2013-08-15 | Hitachi-Ge Nuclear Energy Ltd | Radioactive waste liquid treatment method and radioactive waste liquid treatment apparatus |
| JP2014119417A (en) * | 2012-12-19 | 2014-06-30 | Hitachi-Ge Nuclear Energy Ltd | Method for treating radioactive waste liquid |
| CN103177784A (en) * | 2013-03-28 | 2013-06-26 | 清华大学 | Method for treating radioactive wastewater |
| CN105018754A (en) * | 2014-04-17 | 2015-11-04 | 上海凯鑫分离技术有限公司 | Extraction technology of ion-absorbed rare earth mine |
| CN105244068A (en) * | 2015-08-31 | 2016-01-13 | 中国核电工程有限公司 | Device and method for treating high-salt content radioactive waste liquid |
| CN205451799U (en) * | 2016-02-17 | 2016-08-10 | 杭州上拓环境科技有限公司 | Processing system of uranium ore waste water |
| CN212181940U (en) * | 2019-12-02 | 2020-12-18 | 国家电投集团远达环保工程有限公司重庆科技分公司 | High salt content radioactive waste water's processing apparatus |
Non-Patent Citations (1)
| Title |
|---|
| 刘雪梅等.放射性污染监测.《环境监测》.2017, * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110379532A (en) | 2019-10-25 |
| WO2019196143A1 (en) | 2019-10-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR0185487B1 (en) | Method of manufacturing pure water or ultrapure water and apparatus for manufacturing the same | |
| CN104108813B (en) | Refinery sewage desalination integrated processing technique and device | |
| CN110451704B (en) | Method for treating fluorine-containing reuse water | |
| CN110349689B (en) | Radioactive waste liquid treatment device for nuclear power station | |
| US7708890B2 (en) | Method of rendering a radioactive and aqueous heat transfer liquid in a nuclear reactor to a reduced radwaste quantitative state and returning the remaining waste water volumes to an environmental release point for liquid effluents | |
| CN110379532B (en) | Method and device for treating radioactive waste liquid | |
| CN110349690B (en) | Method and device for treating radioactive waste liquid | |
| CN105321589A (en) | Method for treating radioactive wastewater through whole membrane technology | |
| US7645387B2 (en) | Method of utilizing ion exchange resin and reverse osmosis to reduce environmental discharges and improve effluent quality to permit recycle of aqueous or radwaste fluid | |
| JP5909096B2 (en) | Radioactive liquid processing equipment | |
| WO2018096700A1 (en) | System for producing ultrapure water and method for producing ultrapure water | |
| RU2342720C1 (en) | Method of treating liquid radioactive wastes | |
| TW201641438A (en) | Method for removing boron from a boron-containing wastewater | |
| CN203269712U (en) | Zero discharge treatment device for heavy metal wastewater | |
| CN203754515U (en) | Double membrane system for treating circulating water for coke dry quenching power generation | |
| CN210559747U (en) | Industrial heavy metal sewage treatment system | |
| CN212181940U (en) | High salt content radioactive waste water's processing apparatus | |
| CN109411106B (en) | Near-zero emission treatment device and treatment method for decontaminating waste liquid containing uranium and detergent | |
| CN106746049A (en) | A kind of ultrapure water production system and its production method | |
| CN106045169A (en) | Treatment system and method for realizing flue gas desulfurization wastewater zero discharge of coal-fired power plant | |
| JP6071201B2 (en) | Radioactive liquid processing equipment | |
| CN207498149U (en) | Circulating Wastewater-free water purifier | |
| CN205838758U (en) | The many qualities of electroplating waste-water reutilizing produce water device | |
| CN211170284U (en) | Wastewater treatment and recycling system containing high-concentration heavy metals and organic matters | |
| RU2817393C1 (en) | Method of processing liquid radioactive wastes |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |