CN114684954A - Reverse osmosis recycling method and device for uranium mine hydrochloric acid well-flushing waste liquid - Google Patents
Reverse osmosis recycling method and device for uranium mine hydrochloric acid well-flushing waste liquid Download PDFInfo
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- CN114684954A CN114684954A CN202011621359.2A CN202011621359A CN114684954A CN 114684954 A CN114684954 A CN 114684954A CN 202011621359 A CN202011621359 A CN 202011621359A CN 114684954 A CN114684954 A CN 114684954A
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- 239000007788 liquid Substances 0.000 title claims abstract description 147
- 239000002699 waste material Substances 0.000 title claims abstract description 137
- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 135
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 124
- 238000011010 flushing procedure Methods 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 77
- 229910052770 Uranium Inorganic materials 0.000 title claims abstract description 69
- 238000004064 recycling Methods 0.000 title claims abstract description 68
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 title claims abstract description 67
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- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000004062 sedimentation Methods 0.000 claims abstract description 21
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910001425 magnesium ion Inorganic materials 0.000 claims abstract description 10
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 8
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- 150000002500 ions Chemical class 0.000 claims description 16
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 6
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical group [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 claims description 6
- 238000013327 media filtration Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims description 5
- 238000006386 neutralization reaction Methods 0.000 claims description 5
- 230000003647 oxidation Effects 0.000 claims description 5
- 238000007254 oxidation reaction Methods 0.000 claims description 5
- 239000002455 scale inhibitor Substances 0.000 claims description 5
- 239000013535 sea water Substances 0.000 claims description 5
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- 230000000694 effects Effects 0.000 abstract description 15
- 239000000460 chlorine Substances 0.000 abstract description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 3
- 229910052801 chlorine Inorganic materials 0.000 abstract description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 abstract description 2
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- 229910052791 calcium Inorganic materials 0.000 description 3
- 239000000701 coagulant Substances 0.000 description 3
- 238000007654 immersion Methods 0.000 description 3
- 238000011065 in-situ storage Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 3
- 229920000742 Cotton Polymers 0.000 description 2
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- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 235000013980 iron oxide Nutrition 0.000 description 2
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- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
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- 238000009434 installation Methods 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
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Images
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- 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
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
Abstract
The invention belongs to a recycling method and a recycling device, and particularly relates to a reverse osmosis recycling method and a reverse osmosis recycling device for uranium mine hydrochloric acid well-flushing waste liquid. It includes: the method comprises the following steps: adjusting the pH value; controlling the pH value of the waste liquid within the range of 6.5-8; step two: coagulating sedimentation; coagulating and precipitating the waste liquid by using a flocculating agent; step three: filtering by using a plurality of media; filtering with quartz sand, activated carbon and ion exchange resin; step four: filtering by security; filtering the waste liquid by a filter element; step five: reverse osmosis; and (4) performing reverse osmosis on the waste liquid by using a reverse osmosis membrane. Significant effects of the inventionComprises the following steps: reverse osmosis stage for removing U and Ca2+、Mg2+、SO4 2‑、Cl‑Fe and conductivity have obvious effect, the concentration of the removed chlorine root is basically controlled below 0.37g/L, and the turbidity is reduced.
Description
Technical Field
The invention belongs to a recycling method and a recycling device, and particularly relates to a reverse osmosis recycling method and a reverse osmosis recycling device for uranium mine hydrochloric acid well-flushing waste liquid.
Background
Uranium ores are indispensable mineral resources in the nuclear industry, and exploitation of the uranium ores directly influences the operation effect of a nuclear power station. In the prior art, an immersion method is mostly adopted for uranium ore exploitation, and since the immersion method uses acid liquor as immersion liquid, the environmental influence is caused, reverse osmosis treatment needs to be carried out on the mined mine.
On the one hand, against CO2+O2The current situation that the pumping and liquid injection amount is obviously reduced in the neutral in-situ leaching uranium mining process is adopted, and a hydrochloric acid chemical well flushing mode is adopted to perform blockage removal and seepage increase, so that a good effect is achieved. Along with the increase of the number of the chemical well-flushing with the hydrochloric acid, the generated well-flushing waste liquid greatly rises. The well-flushing waste liquid contains a large amount of Cl-Ions, Cl-Ions have an influence on hydrometallurgical processes on the one hand and have a corrosive effect on process pipelines on the other hand. At present, natural evaporation is adopted to treat well washing waste liquid in Mongolian neutral leaching uranium mining mines, the well washing quantity is limited due to small treatment amount in the mode, and the on-site production requirement cannot be met.
On the other hand, in order to save resources and reduce wastewater discharge, a leaching liquid recycling process is generally adopted in modern leaching mines. The non-mineral ion concentration in the leach solution gradually increases with the extended use period. By investigating the practical requirements of the existing water treatment process and neutral in-situ leaching uranium mining mine, the method effectively removes Cl in well flushing waste liquid-And selecting a reverse osmosis process with a high-efficiency desalting function. Through reverse osmosis treatment, a large amount of harmful components, namely chloride ions in the hole washing water can be reliably removed, and the hole washing water also has good removal effects on calcium ions and sulfate ions. The reverse osmosis produced water is reused in the liquid injection and distribution pool, so that the scaling tendency of liquid injection can be reduced, the blockage condition of an underground ore bed can be improved after long-term operation, the stable liquid pumping and injection amount can be maintained, and the long-term benefit is provided for the yield increase of the neutral in-situ leaching uranium mining mine.
However, there is no mature product on the market at present how to realize the desalination process. Therefore, a reverse osmosis recycling method and a reverse osmosis recycling device for uranium mine hydrochloric acid well-flushing waste liquid are needed to be established.
Disclosure of Invention
The invention provides a reverse osmosis recycling method and device for uranium mine hydrochloric acid well-flushing waste liquid, aiming at the defects of the prior art.
The invention is realized by the following steps:
a reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps:
the method comprises the following steps: pH adjustment
Controlling the pH value of the waste liquid within the range of 6.5-8;
step two: coagulating sedimentation
Coagulating and precipitating the waste liquid by using a flocculating agent;
step three: multi-media filtration
Filtering with quartz sand, activated carbon and ion exchange resin;
step four: safety filter
Filtering the waste liquid by a filter element;
step five: reverse osmosis
And (4) performing reverse osmosis on the waste liquid by using a reverse osmosis membrane.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps:
using 15m3After the tank body is filled with clear water, 400Kg of caustic soda flakes (NaOH) are added; after 1 hour of uninterrupted stirring, the pH value can reach more than 12, and the uniformly stirred flake caustic soda solution is pumped into a well-flushing waste liquid pool with the capacity of 1200m by using a pressure pump3。
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: in order to fully perform acid-base neutralization reaction on the well flushing waste liquid and the caustic soda flakes solution, an air compressor is used for blowing the well flushing waste liquid pool.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: blowing for 24 hours, detecting the pH value of the waste liquid after 24 hours, and stopping blowing if the pH value reaches a preset value; if the pH value is still lower than the preset value, air blowing is continued, the pH value is detected every hour, and air blowing is stopped until the pH value is higher than the preset value.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the preset value is 6.5.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the blowing is that compressed air is injected into the mixed solution of the waste liquid and the caustic soda flake solution, and the flow velocity range of the blowing air is 3-5 cubic meters per second, preferably 3 cubic meters per second.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the flocculating agent is polyacrylamide.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: at 10m34kg of polyacrylamide is added into the clear water to realize the preparation of the flocculant.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: adding polyacrylamide into clear water, and continuously stirring for more than 3 h.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: quartz sand filtration, active carbon filtration and ion exchange resin filtration are carried out in series.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the quartz sand filtration, the active carbon filtration and the ion exchange resin filtration are all subjected to forward and back washing.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the quartz sand filter is subjected to forward and back washing in a cycle of every three days, wherein the back washing time is 15min, and the forward washing time is 5 min.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the active carbon filter carries out positive and back flushing in a cycle of every three days, the back flushing time is 10min, and the positive flushing time is 5 min.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the ion exchange resin filter is subjected to forward and back washing in a cycle of every three days, wherein the back washing time is 5min, and the forward washing time is 5 min.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the grain sizes of the filter materials of the quartz sand filter are 1-2mm and 2-4mm, and the filter materials are alternately paved in a filter container.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the grain diameter of the active carbon filter material of the active carbon filter is 1-2mm and 2-4mm, and the active carbon filter material is alternately paved in a filter container.
The reverse osmosis recycling method of the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the ion exchange resin is internally provided with sodium ion exchange resin.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps: the filtration precision was 5 μm.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following fifth step: eight reverse osmosis membranes are arranged.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following fifth step: the waste liquid is pressurized before entering the reverse osmosis membrane, and the pressure is 1.5 Mpa.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following fifth step: an anti-reverse osmosis membrane oxidation link is added before the waste liquid enters the reverse osmosis membrane.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following fifth step: the anti-reverse osmosis membrane oxidation link is that clear water and 5kg of sodium bisulfite are added into a 100L cartridge and are added according to 3L per hour after being uniformly stirred.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following fifth step: the link of preventing calcium and magnesium ions from scaling on the reverse osmosis membrane is added.
The reverse osmosis recycling method for the uranium mine hydrochloric acid well-flushing waste liquid comprises the following fifth step: the link of preventing calcium and magnesium ions from scaling on the reverse osmosis membrane is that clean water and 2.5kg of seawater scale inhibitor are added into a 100L cartridge, and after the mixture is uniformly stirred, the mixture is added according to 3L per hour.
A reverse osmosis recycling device for uranium mine hydrochloric acid well-flushing waste liquid, which comprises,
a pH adjusting device: the device is used for adjusting the pH value of the waste liquid, the target pH value range is adjusted to 6.5-8, and the adjusted waste liquid enters a coagulating sedimentation device;
a coagulating sedimentation device: the colloidal particles used in the waste liquid are mutually polymerized to form colloid, a polyacrylamide solution is arranged in the coagulating sedimentation device to be mixed with the waste liquid to realize coagulating sedimentation, the waste liquid after coagulating sedimentation enters a multi-medium filtering device,
a multi-media filtration device: comprises a quartz sand filter, an active carbon filter and an ion exchange resin filter which are connected in series, wherein each filter is provided with a positive and a back flushing device, the filtered waste liquid is conveyed to a security filter,
the security filter device: a filtering filter element is arranged in the reverse osmosis membrane, the filtering precision is 5 mu m, the filtered waste liquid is conveyed to a reverse osmosis device,
a reverse osmosis device: the water treatment device is composed of four sections of membrane shells, wherein two reverse osmosis membranes are arranged in each section of membrane shell, the total number of the reverse osmosis membranes is eight, two water outlets are formed in a reverse osmosis device, one part of the reverse osmosis device is fresh water, the fresh water is used as treated water and enters a liquid preparation pool to be re-injected underground, the other part of the reverse osmosis device is concentrated water, the content of each ion in the concentrated water is high, the concentrated water cannot be recycled, and the concentrated water is pumped into an evaporation pool to be evaporated.
The reverse osmosis recycling device for the uranium mine hydrochloric acid well-flushing waste liquid is characterized in that,
the grain sizes of filter materials used by the quartz sand filter are divided into two types: 1-2mm and 2-4mm, the filter material particles with two particle sizes are alternatively paved in a quartz sand filter to realize the filtering function,
the grain sizes of filter materials used by the activated carbon filter are divided into two types: 1-2mm and 2-4mm, the filter material particles with two particle sizes are alternatively paved in a quartz sand filter to realize the filtering function,
the ion exchange resin filter contains sodium ion exchange resin.
The invention has the following remarkable effects: the Cl in the well-flushing waste liquid is removed by analyzing the change degree of the raw water sample of the well-flushing waste liquid and the ions at the fresh water end and the concentrated water end of the reverse osmosis device-Concentration of Cl-The concentration is lower than 0.4g/L, and U and Ca are removed in the reverse osmosis stage at present through the actual operation on site2+、Mg2+、SO4 2-、Cl-Fe and conductivity have obvious effect, the concentration of the removed chlorine root is basically controlled below 0.37g/L, and the turbidity is reduced.
Drawings
FIG. 1 is a schematic diagram of a process flow of reverse osmosis recycling of well-flushing waste liquid
The system comprises a pH adjusting device 1, a coagulating sedimentation device 2, a multi-medium filtering device 3, a security filtering device 4, a reverse osmosis device 5, a quartz sand filter 6, an active carbon filter 7 and an ion exchange resin filter 8.
Detailed Description
A reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid comprises the following steps:
the method comprises the following steps: pH adjustment
The pH value of the waste liquid needs to be controlled within the range of 6.5-8.
The specific operation steps are as follows: using 15m3After the tank body is filled with clear water, 400Kg of flake caustic soda (NaOH) is added; after 1 hour of uninterrupted stirring, the pH value can reach more than 12. Pumping the uniformly stirred flake caustic soda solution into a well-flushing waste liquid pool (1200 m)3). In order to fully perform acid-base neutralization reaction on the well flushing waste liquid and the caustic soda flakes solution, an air compressor is used for blowing the well flushing waste liquid pool.
Blowing for 24 hours, detecting the pH value of the waste liquid after 24 hours, and stopping blowing if the pH value reaches a preset value; if the pH value is still lower than the preset value, air blowing is continued, the pH value is detected every hour, and air blowing is stopped until the pH value is higher than the preset value. The preset value is 6.5, and can be arbitrarily selected from 6.5-8 according to actual conditions.
The blowing is that compressed air is injected into the mixed solution of the waste liquid and the caustic soda flake solution, and the flow velocity range of the blowing air is 3-5 cubic meters per second, preferably 3 cubic meters per second.
Step two: coagulating sedimentation
In the industrial wastewater treatment, there is a very important physical and chemical treatment method, namely a coagulation method. The water treatment method has wide application and high removal rate of various pollution indexes. The coagulation aims at adding certain medicaments (generally called coagulants and coagulant aids) into water, wherein the coagulants enable colloidal particles which are difficult to precipitate in the water to mutually polymerize through chemical actions such as ionization, hydrolysis and the like in the water to form colloid, and then the colloid is combined with impurities and organic matter colloid in water to form larger particle flocs through compression double-layer action, adsorption electric neutralization, adsorption bridging action, precipitate net catching action and the like of the colloid, and the particle flocs are easy to collide and adsorb with each other in turbulent flow of the water to form flocs (also called flocks or alums). The flocculating constituent has strong adsorption capacity, can adsorb suspended matters, and can adsorb partial bacteria and soluble substances. The flocs sink down by increasing their volume through adsorption.
Flocculant for use hereinFor Polyacrylamide (PAM), the tank body configured with the Polyacrylamide (PAM) must be cleaned, and no redundant ions are ensured to appear. Adding 10m into the tank body3Adding 4kg of Polyacrylamide (PAM) into the left and right clear water, and stirring for more than 3h to fully dissolve the PAM in the clear water. After being stirred evenly, the mixture is pumped into a well-flushing waste liquid pool (1200 m) by a pressure pump3). After Polyacrylamide (PAM) is added, a large amount of brown floccules are generated in the well washing waste liquid pool, and the coagulating sedimentation effect is achieved.
Step three: multi-media filtration
The multi-medium filter can remove large suspended particles in water, thereby reducing the turbidity value of water and meeting the water quality requirement of deep purification. The multi-medium filtration is to remove partial suspended matters, mechanical particles, flaky matters, adsorbed metal ions in water through a multi-medium filter bed and adhesive colloid matters which cannot be removed by a precipitation method.
The multi-medium filter used in the application is a quartz sand filter, an activated carbon filter or an ion exchange resin filter. The three filters are connected in series, a forward washing device and a backward washing device are arranged on each filter, and the backward washing time is independently controlled by each filter. The back washing time of the quartz sand filter is 15min, the positive washing time is 5min, and the back washing period is once every three days. The back flushing time of the activated carbon filter is 10min, the positive flushing time is 5min, and the back flushing period is once every three days. The back flushing time of the ion exchange resin filter and the activated carbon filter is 5min, the positive flushing time is 5min, and the back flushing period is once every three days. And the front end and the rear end of each filter are provided with sampling valves, so that the change conditions of each ion can be conveniently sampled and analyzed.
Quartz sand filter
The purpose of installation quartz sand filter is in order to dispel the large granule suspended solid in the well-flushing waste liquid to reduce the turbidity, the turbidity value is lower, and it is more obvious to explain the effect of dispelling the large granule suspended solid. The grain diameter of the filter material used by the quartz sand is mainly 1-2mm and 2-4mm, and the filter material is paved in the tank body in layers. The change of front and back turbidity of the quartz sand filter is found, the effect of removing large-particle suspended matters in water is obvious, and the turbidity reduction rate is basically maintained at 36.94-52.17%. Through analyzing the ion change conditions of the water inlet end and the filtered water outlet end of the quartz sand filter, the situation that each ion is not changed is found.
② active carbon filter
The active carbon filter is mainly used for removing macromolecular organic matters and iron oxides. This is because organic matter and iron oxide tend to poison ion exchange resins. The active carbon filter material used by the active carbon filter mainly has the grain diameter of 1-2mm and 2-4mm and is paved in the tank body in layers. Through discovering the front and back turbidity change condition of the activated carbon filter, the effect of removing large-particle suspended matters in the well-flushing waste liquid is poor, simultaneously, the turbidity of the well-flushing waste liquid is increased, and the turbidity reduction rate is basically maintained at 24.05% -57.1%. Through analyzing the ion change conditions of the water inlet end and the filtered water outlet end of the quartz sand filter, only SiO is found2The ion reduction is 5mg/L and the Fe reduction is 0.28mg/L, and the rest ions are basically unchanged.
(iii) ion exchange resin Filter
The ion exchange resin filter contains sodium ion exchange resin with a large amount of sodium ions, and the resin is mainly used for removing calcium and magnesium ions and reducing the hardness of well washing waste liquid. The change of front and back turbidity of the ion exchange resin filter shows that the effect of removing large-particle suspended matters in water is obvious, the turbidity reduction rate is basically maintained at 30.28-38.96%, and Ca content is maintained2+、Mg2+The reduction is 50-60 mg/L.
Step four: safety filter
The security filtration technology is also called as a precise filtration technology, mostly adopts stainless steel as a shell, and a filtration filter element is arranged in the shell and is mainly used after the multi-medium pretreatment filtration and before the reverse osmosis equipment. The filter element is used for filtering fine substances filtered by a plurality of media so as to ensure the water quality filtering precision and protect the membrane filter element from being damaged by large-particle substances. It is characterized in that suspended matters, rust and the like in the liquid are effectively removed; can bear higher filtering pressure.
The safety filter is also called a precision filter, and a filtering filter element (pp cotton) is arranged in the safety filter and is mainly used after the multi-medium pretreatment filtration and before the reverse osmosis equipment. The filter is used for filtering fine substances filtered by the multi-media, and the filtering precision is 5 mu m. The change of turbidity before and after the cartridge filter is found, the effect of removing fine substances in water is particularly obvious, and the turbidity reduction rate is basically maintained between 77.94 and 98.29 percent. Through analyzing the ion change conditions of the water inlet end and the filtered water outlet end of the cartridge filter, the fact that all ions are unchanged is found.
Step five: reverse osmosis
Reverse osmosis is also known as Reverse Osmosis (RO). The solvent in the solution is separated by a reverse osmosis membrane (or semi-permeable membrane) under certain pressure. Reverse osmosis is known because it is in the opposite direction to natural osmosis. According to different osmotic pressures of various materials, the reverse osmosis method with the osmotic pressure higher than that can achieve the purposes of separation, extraction, purification and concentration.
The reverse osmosis device mainly comprises four sections of membrane shells, wherein two reverse osmosis membranes are arranged in each section of membrane shell, and the total number of the reverse osmosis membranes is eight. The well-flushing waste liquid filtered by the cartridge filter is pumped into the membrane shell by a pressure pump, and the pressure is controlled to be 1.5 Mpa. Because the oxidation-reduction potential in the well-flushing waste liquid is higher, generally more than 500mv, the oxidation of the reverse osmosis membrane is easily caused due to higher oxidation-reduction potential, and the service life of the reverse osmosis membrane is greatly reduced. For this purpose, sodium bisulfite is added at the rear end of the security filter to reduce the redox potential, and then clear water and 5kg of sodium bisulfite are added into a 100L cartridge, and after stirring uniformly, the amount of sodium bisulfite is added according to 3L per hour. In order to prevent calcium and magnesium ions from scaling on the reverse osmosis membrane, causing the reverse osmosis membrane to be blocked and reducing the service life of the reverse osmosis membrane, adding a seawater scale inhibitor, adding clean water and 2.5kg of seawater scale inhibitor into a 100L cartridge, stirring uniformly, and adding 3L of the seawater scale inhibitor per hour. The effluent of the membrane module is divided into two parts, one part is fresh water, and the fresh water is used as treated water and enters the liquid preparation pool to be injected underground again. The other part is concentrated water, the content of each ion in the concentrated water is high, and the concentrated water cannot be recycled and pumped into an evaporation tank for evaporation.
The Cl in the well-flushing waste liquid is removed by analyzing the change degree of the raw water sample of the well-flushing waste liquid and the ions at the fresh water end and the concentrated water end of the reverse osmosis device-Concentration of Cl-The concentration is lower than 0.4g/L, and U and Ca are removed in the reverse osmosis stage at present through the actual operation on site2+、Mg2+、SO4 2-、Cl-Fe and conductivity have obvious effect, the concentration of the removed chlorine root is basically controlled below 0.37g/L, and the turbidity is reduced.
A reverse osmosis recycling device for uranium mine hydrochloric acid well-flushing waste liquid comprises
A pH adjusting device: the device is used for adjusting the pH value of the waste liquid, the target pH value range is adjusted to 6.5-8, and the adjusted waste liquid enters a coagulating sedimentation device;
the pH value of the waste liquid is adjusted by mixing the caustic soda flake solution and the waste liquid; the specific process is as follows: using 15m3After the tank body is filled with clear water, 400Kg of caustic soda flakes (NaOH) are added; after 1 hour of uninterrupted stirring, the pH value can reach more than 12. Pumping the uniformly stirred flake caustic soda solution into a well-flushing waste liquid pool (1200 m)3). In order to fully perform acid-base neutralization reaction on the well flushing waste liquid and the caustic soda flakes solution, an air compressor is used for blowing the well flushing waste liquid pool.
Blowing for 24 hours, detecting the pH value of the waste liquid after 24 hours, and stopping blowing if the pH value reaches a preset value; if the pH value is still lower than the preset value, air blowing is continued, the pH value is detected every hour, and air blowing is stopped until the pH value is higher than the preset value. The preset value is 6.5, and can be arbitrarily selected from 6.5-8 according to actual conditions.
The blowing is that compressed air is injected into the mixed solution of the waste liquid and the caustic soda flake solution, and the flow velocity range of the blowing air is 3-5 cubic meters per second, preferably 3 cubic meters per second.
A coagulating sedimentation device: the method is characterized in that colloidal particles used in the waste liquid are mutually polymerized to form colloid, a polyacrylamide solution is arranged in a coagulating sedimentation device and is mixed with the waste liquid to realize coagulating sedimentation, and the waste liquid after coagulating sedimentation enters a multi-medium filtering device.
A multi-media filtration device: comprises a quartz sand filter, an active carbon filter and an ion exchange resin filter which are connected in series, wherein each filter is provided with a positive and a back flushing device,
the grain sizes of filter materials used by the quartz sand filter are divided into two types: 1-2mm and 2-4mm, and filter material particles with two particle sizes are alternately paved in a quartz sand filter to realize the filtering function.
The grain sizes of filter materials used by the activated carbon filter are divided into two types: 1-2mm and 2-4mm, and filter material particles with two particle sizes are alternately paved in a quartz sand filter to realize the filtering function.
The ion exchange resin filter contains sodium ion exchange resin.
And conveying the filtered waste liquid to a security filter device.
The security filter device: the inside is provided with a filter element with the filtering precision of 5 μm.
The filter element is pp cotton.
Multiple stages of filtration may be provided as desired.
And conveying the filtered waste liquid to a reverse osmosis device.
A reverse osmosis device: the membrane consists of four sections of membrane shells, wherein two reverse osmosis membranes are arranged in each section of membrane shell, and the total number of the reverse osmosis membranes is eight. The reverse osmosis device is provided with two water outlets, one part of the reverse osmosis device is fresh water, and the fresh water is used as treated water and enters the liquid preparation pool to be injected underground again. The other part is concentrated water, the content of each ion in the concentrated water is high, and the concentrated water cannot be recycled and pumped into an evaporation tank for evaporation.
Claims (26)
1. A reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid is characterized by comprising the following steps:
the method comprises the following steps: pH adjustment
Controlling the pH value of the waste liquid within the range of 6.5-8;
step two: coagulating sedimentation
Coagulating and precipitating the waste liquid by using a flocculating agent;
step three: multi-media filtration
Filtering with quartz sand, activated carbon and ion exchange resin;
step four: safety filter
Filtering the waste liquid by a filter element;
step five: reverse osmosis
And (4) performing reverse osmosis on the waste liquid by using a reverse osmosis membrane.
2. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 1, characterized by comprising the following steps: the first step comprises the following steps:
using 15m3After the tank body is filled with clear water, 400Kg of caustic soda flakes (NaOH) are added; after 1 hour of uninterrupted stirring, the pH value can reach more than 12, and the uniformly stirred flake caustic soda solution is pumped into a well-flushing waste liquid pool with the capacity of 1200m by using a pressure pump3。
3. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 2, characterized by comprising the following steps: the first step comprises the following steps: in order to fully perform acid-base neutralization reaction on the well flushing waste liquid and the caustic soda flakes solution, an air compressor is used for blowing the well flushing waste liquid pool.
4. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 3, characterized by comprising the following steps: the first step comprises the following steps: blowing for 24 hours, detecting the pH value of the waste liquid after 24 hours, and stopping blowing if the pH value reaches a preset value; if the pH value is still lower than the preset value, air blowing is continued, the pH value is detected every hour, and air blowing is stopped until the pH value is higher than the preset value.
5. The reverse osmosis recycling method for uranium mine hydrochloric acid well flushing waste liquid according to claim 4, characterized by comprising the following steps: the first step comprises the following steps: the preset value is 6.5.
6. The reverse osmosis recycling method for uranium mine hydrochloric acid well flushing waste liquid according to claim 5, characterized by comprising the following steps: the first step comprises the following steps: the blowing is that compressed air is injected into the mixed solution of the waste liquid and the caustic soda flake solution, and the flow velocity range of the blowing air is 3-5 cubic meters per second, preferably 3 cubic meters per second.
7. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 1, characterized by comprising the following steps: the second step comprises the following steps: the flocculating agent is polyacrylamide.
8. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 7, characterized by comprising the following steps: the second step comprises the following steps: at 10m34kg of polyacrylamide is added into the clear water to realize the preparation of the flocculant.
9. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 8, characterized by comprising the following steps: the second step comprises the following steps: adding polyacrylamide into clear water, and continuously stirring for more than 3 h.
10. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 1, characterized by comprising the following steps: the third step comprises the following steps: quartz sand filtration, active carbon filtration and ion exchange resin filtration are carried out in series.
11. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 10, characterized by comprising the following steps: the third step comprises the following steps: the quartz sand filtration, the active carbon filtration and the ion exchange resin filtration are all subjected to forward and back washing.
12. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 11, characterized by comprising the following steps: the third step comprises the following steps: the quartz sand filter is subjected to forward and back washing in a cycle of every three days, wherein the back washing time is 15min, and the forward washing time is 5 min.
13. The reverse osmosis recycling method for uranium mine hydrochloric acid well flushing waste liquid according to claim 12, characterized by comprising the following steps: the third step comprises the following steps: the active carbon filter carries out positive and back flushing in a cycle of every three days, the back flushing time is 10min, and the positive flushing time is 5 min.
14. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 13, characterized by comprising the following steps: the third step comprises the following steps: the ion exchange resin filter is subjected to forward and back washing in a cycle of every three days, wherein the back washing time is 5min, and the forward washing time is 5 min.
15. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 14, characterized by comprising the following steps: the third step comprises the following steps: the grain sizes of the filter materials of the quartz sand filter are 1-2mm and 2-4mm, and the filter materials are alternately paved in a filter container.
16. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 14, characterized by comprising the following steps: the third step comprises the following steps: the grain diameter of the active carbon filter material of the active carbon filter is 1-2mm and 2-4mm, and the active carbon filter material is alternatively paved in a filter container.
17. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 14, characterized by comprising the following steps: the third step comprises the following steps: the ion exchange resin is internally provided with sodium ion exchange resin.
18. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 1, characterized by comprising the following steps: the fourth step comprises the following steps: the filtration precision was 5 μm.
19. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 1, characterized by comprising the following steps: the fifth step comprises the following contents: eight reverse osmosis membranes are arranged.
20. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 19, characterized by comprising the following steps: the fifth step comprises the following contents: the waste liquid is pressurized before entering the reverse osmosis membrane, and the pressure is 1.5 Mpa.
21. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 20, characterized by comprising the following steps: the fifth step comprises the following contents: an anti-reverse osmosis membrane oxidation link is added before the waste liquid enters the reverse osmosis membrane.
22. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 21, characterized by comprising the following steps: the fifth step comprises the following contents: the anti-reverse osmosis membrane oxidation link is that clear water and 5kg of sodium bisulfite are added into a 100L cartridge and are added according to 3L per hour after being uniformly stirred.
23. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 20, characterized by comprising the following steps: the fifth step comprises the following contents: the link of preventing calcium and magnesium ions from scaling on the reverse osmosis membrane is added.
24. The reverse osmosis recycling method for uranium mine hydrochloric acid well-flushing waste liquid according to claim 23, characterized by comprising the following steps: the fifth step comprises the following contents: the link of preventing calcium and magnesium ions from scaling on the reverse osmosis membrane is that clean water and 2.5kg of seawater scale inhibitor are added into a 100L cartridge, and after the mixture is uniformly stirred, the mixture is added according to 3L per hour.
25. The utility model provides a uranium mine hydrochloric acid well-flushing waste liquid reverse osmosis recycle device which characterized in that: comprises the steps of (a) preparing a mixture of a plurality of raw materials,
a pH adjusting device: the device is used for adjusting the pH value of the waste liquid, the target pH value range is adjusted to 6.5-8, and the adjusted waste liquid enters a coagulating sedimentation device;
a coagulating sedimentation device: the colloidal particles used in the waste liquid are mutually polymerized to form colloid, a polyacrylamide solution is arranged in the coagulating sedimentation device to be mixed with the waste liquid to realize coagulating sedimentation, the waste liquid after coagulating sedimentation enters a multi-medium filtering device,
a multi-media filtration device: comprises a quartz sand filter, an active carbon filter and an ion exchange resin filter which are connected in series, wherein each filter is provided with a positive and a back flushing device, the filtered waste liquid is conveyed to a security filter,
the security filter device: a filtering filter element is arranged in the reverse osmosis membrane, the filtering precision is 5 mu m, the filtered waste liquid is conveyed to a reverse osmosis device,
a reverse osmosis device: the water treatment device is composed of four sections of membrane shells, wherein two reverse osmosis membranes are arranged in each section of membrane shell, the total number of the reverse osmosis membranes is eight, two water outlets are formed in a reverse osmosis device, one part of the reverse osmosis device is fresh water, the fresh water is used as treated water and enters a liquid preparation pool to be re-injected underground, the other part of the reverse osmosis device is concentrated water, the content of each ion in the concentrated water is high, the concentrated water cannot be recycled, and the concentrated water is pumped into an evaporation pool to be evaporated.
26. The reverse osmosis recycling device for uranium mine hydrochloric acid well-flushing waste liquid according to claim 25, characterized in that:
the grain sizes of filter materials used by the quartz sand filter are divided into two types: 1-2mm and 2-4mm, the filter material particles with two particle sizes are alternatively paved in a quartz sand filter to realize the filtering function,
the grain sizes of filter materials used by the activated carbon filter are divided into two types: 1-2mm and 2-4mm, the filter material particles with two particle sizes are alternatively paved in a quartz sand filter to realize the filtering function,
the ion exchange resin filter contains sodium ion exchange resin.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114984804A (en) * | 2022-07-15 | 2022-09-02 | 兰州凯宏中原石油科技有限公司 | Oil field oil-water well composite acid mixing and blending method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1872742A (en) * | 2006-06-22 | 2006-12-06 | 葫芦岛北方膜技术工业有限公司 | Technical methd for treating mine wastewater by using membrane technology |
| CN101643284A (en) * | 2008-08-06 | 2010-02-10 | 郭静 | Reverse osmosis water treatment method and equipment with high desalination and high water productivity |
| CN101767904A (en) * | 2009-12-15 | 2010-07-07 | 南华大学 | Process for treating polluted groundwater of retired mining area of acid in-situ leaching uranium mine by using microbial method |
| CN105217844A (en) * | 2015-11-03 | 2016-01-06 | 安徽洋森环保节能科技有限公司 | A kind of processing method of coal mine wastewater reuse |
| CN206512042U (en) * | 2017-03-03 | 2017-09-22 | 烟台和盛康洁环保科技有限公司 | A kind of mine wastewater treatment and reclaiming system |
-
2020
- 2020-12-31 CN CN202011621359.2A patent/CN114684954A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1872742A (en) * | 2006-06-22 | 2006-12-06 | 葫芦岛北方膜技术工业有限公司 | Technical methd for treating mine wastewater by using membrane technology |
| CN101643284A (en) * | 2008-08-06 | 2010-02-10 | 郭静 | Reverse osmosis water treatment method and equipment with high desalination and high water productivity |
| CN101767904A (en) * | 2009-12-15 | 2010-07-07 | 南华大学 | Process for treating polluted groundwater of retired mining area of acid in-situ leaching uranium mine by using microbial method |
| CN105217844A (en) * | 2015-11-03 | 2016-01-06 | 安徽洋森环保节能科技有限公司 | A kind of processing method of coal mine wastewater reuse |
| CN206512042U (en) * | 2017-03-03 | 2017-09-22 | 烟台和盛康洁环保科技有限公司 | A kind of mine wastewater treatment and reclaiming system |
Non-Patent Citations (1)
| Title |
|---|
| 赖磊;师振峰;熊威;路乾乾;汤义伟;: "铀矿石中性浸出液吸附饱和树脂的酸性淋洗工艺研究", 铀矿冶, vol. 38, no. 02, pages 98 - 102 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114984804A (en) * | 2022-07-15 | 2022-09-02 | 兰州凯宏中原石油科技有限公司 | Oil field oil-water well composite acid mixing and blending method |
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