CN112779426B - CO (carbon monoxide) 2 +O 2 Method for recycling uranium in wastewater of in-situ leaching uranium mining evaporation pool - Google Patents

CO (carbon monoxide) 2 +O 2 Method for recycling uranium in wastewater of in-situ leaching uranium mining evaporation pool Download PDF

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CN112779426B
CN112779426B CN202011378637.6A CN202011378637A CN112779426B CN 112779426 B CN112779426 B CN 112779426B CN 202011378637 A CN202011378637 A CN 202011378637A CN 112779426 B CN112779426 B CN 112779426B
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uranium
membrane
nanofiltration
filtrate
concentration
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CN112779426A (en
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闻振乾
郑剑平
崔玉峰
周越
胥国龙
胡柏石
姚益轩
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Beijing Research Institute of Chemical Engineering and Metallurgy of CNNC
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Beijing Research Institute of Chemical Engineering and Metallurgy of CNNC
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
    • C22B60/02—Obtaining thorium, uranium, or other actinides
    • C22B60/0204—Obtaining thorium, uranium, or other actinides obtaining uranium
    • C22B60/0217—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes
    • C22B60/0252—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • 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
    • G21F9/08—Processing by evaporation; by distillation
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Abstract

The invention belongs to the technical field of hydrometallurgy of uranium, and particularly relates to CO 2 +O 2 A method for recycling uranium in-situ leaching uranium mining evaporation pond wastewater relates to a uranium separation and extraction technology and a wastewater treatment technology in a uranium hydrometallurgy process, in particular to a method and a process for extracting uranium by adopting a membrane separation process. The method is mainly characterized in that the evaporation tank wastewater is pretreated by adopting mechanical filtration and ultrafiltration to remove solid particles and suspended matters, uranium is enriched by adopting first-stage nanofiltration, and the enriched liquid is acidified by hydrochloric acid and then enriched by adopting second-stage nanofiltration to obtain a high-concentration uranium solution. The method can realize the aims of effectively enriching uranium at high power, improving the recovery rate of uranium and reducing the influence of wastewater on the environment.

Description

CO (carbon monoxide) 2 +O 2 Method for recycling uranium in wastewater of in-situ leaching uranium mining evaporation pool
Technical Field
The invention belongs to the technical field of hydrometallurgy of uranium, and particularly relates to CO 2 +O 2 A method for recovering uranium from waste water of an in-situ leaching uranium mining evaporation pool.
Background
In-situ leaching uranium mining has become an important method for mining sandstone-type uranium ores in Hassakestan, Utzibekstan, Australia, America, China and other countries. CO 2 2 +O 2 The in-situ leaching uranium mining process adopts CO 2 As leaching agent, O 2 The in-situ leaching uranium mining process is used as oxidant for leaching uranium in sandstone uranium ore with high selectivity. At present, China has built a plurality of CO 2 +O 2 In-situ leaching of mine, in-situ leaching uranium will account for about 90% of natural uranium yield in our country, and CO 2 +O 2 The yield of the in-situ leaching uranium mining process is more than 65%. The in-situ leaching uranium mining technology has become the national technologyImportant technology for uranium mining and metallurgy, especially CO 2 +O 2 The in-situ leaching process is more and more dominant.
In the in-situ leaching uranium extraction process, leaching of uranium and solution migration occur in an ore-bearing aquifer, in order to control a leaching range, the pumping capacity of a well site is required to be larger than the injection capacity by a certain proportion, the nuclear industry uranium metallurgy engineering design specification (GB 50521-2009) requires that the pumping capacity and the injection capacity are basically balanced, and the pumping capacity is larger than the injection capacity by 0.3-1.0%, so that an underground water falling funnel is formed in a leaching area, and diffusion of the leaching solution is controlled. The in-situ leaching uranium mining mines produced in China are mainly located in places such as Xinjiang and inner Mongolia, the annual evaporation capacity of the surface of the mines is large, and evaporation ponds relying on natural evaporation are built in the mines and used for containing and evaporating 0.3% -1.0% of waste liquid which is extracted in large quantity. Meanwhile, in the in-situ leaching uranium mining process, physical and chemical blockage is formed around an ore-containing layer and a filter along with the change of the pH value and the ion concentration of a leaching solution system, so that the pumping and injection liquid amount is influenced. To remove the blockage, a physical or chemical flushing is usually performed, and the flushing water is also drained into the evaporation pond. According to statistics, CO 2 +O 2 The concentration of uranium in the waste liquid of the in-situ leaching uranium mining evaporation pond can reach n mg/L- (n x 100) mg/L, but the components in the waste water are complex and contain CO 3 2- 、HCO 3 - 、Cl - 、SO 4 2- 、 NO 3 - And various impurity ions are added, and the concentration is higher. The difficulty of recycling uranium from the evaporation pool is high, and no mature process technology exists at present.
Disclosure of Invention
In view of the above disadvantages, the present invention provides a CO 2 +O 2 A method for recovering uranium from waste water of an in-situ leaching uranium mining evaporation pool aims at realizing the recovery of CO with high salinity and complex components 2 +O 2 The uranium is recycled from the waste liquid of the in-situ leaching uranium mining evaporation pool, the waste water components are reduced, the resource waste is avoided, and the comprehensive recovery rate and the resource utilization rate of the uranium are improved.
The technical scheme of the invention is as follows:
CO (carbon monoxide) 2 +O 2 The method for recovering uranium from waste water of an in-situ leaching uranium mining evaporation pool comprises five steps, namely step one, evaporationConveying the waste liquid to a machine for filtration by using a pump to remove solid particles, wherein clear liquid is primary filtrate, removing the step II, and washing the solid particles remained in the filter bag and discarding the solid particles to a tailing pond;
step two, conveying the primary filtrate from the step one as a raw material liquid of an ultrafiltration system to the ultrafiltration system to remove suspended solids, macromolecular organic matters and colloids, and discharging ultrafiltration concentrated liquid to an evaporation tank in step three, wherein ultrafiltration dialyzate is secondary filtrate;
step three, conveying the secondary filtrate from the step two as raw material liquid of the primary nanofiltration system to a nanofiltration system for uranium enrichment, wherein the concentrated solution is tertiary filtrate, and removing the filtrate from the step four to a waste liquid pool for evaporation treatment;
step four, feeding the third-stage filtrate from the step three into a stirring tank, adding concentrated hydrochloric acid with the mass fraction of about 35% into the stirring tank while stirring to acidify the third-stage filtrate, and fully reacting;
and fifthly, conveying the acidified tertiary filtrate from the fourth step to a secondary nanofiltration system for re-enrichment of uranium, wherein the concentrated solution is a product solution, and the secondary filtrate from the third step of the dialysate is used as a raw material solution of the primary nanofiltration system.
In the first step, the concentration of uranium in the waste liquid of the evaporation pool is 10-500mg/L, CO 3 2- The concentration is 0-2000mg/L, SO 4 2- Concentration of 0-50g/L, Cl - The concentration is 0-50 g/L.
The mechanical filtration is bag filtration, the aperture of the filter bag is 50-100um, and the filter bag is replaced when the pressure of the filter is more than 0.5 MPa.
In the second step, the ultrafiltration membrane adopts a roll-shaped membrane or a plate-shaped membrane, the material of the membrane is polyamide, and the aperture specification of the ultrafiltration membrane is 0.05um-1 nm.
In the second step, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the ultrafiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:10-1:100, the ultrafiltration operation is finished.
In the third step, the nanofiltration membrane adopts a coiled membrane or a plate-shaped membrane, the membrane material is polyamide, the nanofiltration membrane has a molecular weight cut-off of 200-600, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the nanofiltration system is intermittent operation, the concentrated solution returns to the raw material tank, the dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:5-1:30, the nanofiltration operation is completed; the uranium concentration of nanofiltration product liquid is 1-10g/L, and the uranium concentration of dialysate is less than 10 mg/L;
in the fourth step, the pH value of the third-stage filtrate is 2-4;
in the fifth step, the nanofiltration membrane adopts a coiled membrane or a plate-shaped membrane, the membrane material is polyamide, the nanofiltration membrane has the molecular weight cut-off of 200-600, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the nanofiltration system is intermittent operation, the concentrated solution returns to the raw material tank, and the dialysate is discharged to the secondary filtrate.
When the separation volume ratio of the concentrated solution to the dialyzate is 1:3-1:10, the nanofiltration operation is finished; the uranium concentration of the nanofiltration product liquid is 20-50g/L, and the uranium concentration of the dialysate is 50-500 mg/L.
The invention has the beneficial effects that:
CO 2 +O 2 the waste liquid of the in-situ leaching uranium mining evaporation pool contains a certain concentration of uranium, but CO 3 2- 、SO 4 2- 、Cl - And the concentration of impurities and anions is high, so that the extraction of uranium cannot be realized by anion exchange resin. By adopting the method, the effective high-power enrichment of uranium is realized, the recovery rate of uranium is improved, and the economic benefit is increased; meanwhile, the uranium concentration of the wastewater and the influence degree on the environment are reduced.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
CO (carbon monoxide) 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool comprises the following steps:
conveying the waste liquid of the evaporation tank to a machine by using a pump for filtering to remove solid particles, wherein clear liquid is primary filtrate, and removing the solid particles remained in a filter bag to a tailing pond by using a step two;
step two, conveying the primary filtrate from the step one as a raw material liquid of an ultrafiltration system to the ultrafiltration system to remove suspended solids, macromolecular organic matters and colloids, and discharging ultrafiltration concentrated liquid to an evaporation tank in step three, wherein ultrafiltration dialyzate is secondary filtrate;
step three, conveying the secondary filtrate from the step two as raw material liquid of the primary nanofiltration system to a nanofiltration system for uranium enrichment, wherein the concentrated solution is tertiary filtrate, and removing the filtrate from the step four to a waste liquid pool for evaporation treatment;
and step four, feeding the third-stage filtrate from the step three into a stirring tank, adding concentrated hydrochloric acid with the mass fraction of about 35% into the stirring tank while stirring to acidify the third-stage filtrate, and fully reacting.
And fifthly, conveying the acidified tertiary filtrate from the fourth step to a secondary nanofiltration system for re-enrichment of uranium, wherein the concentrated solution is a product solution, and the secondary filtrate from the third step of the dialysate is used as a raw material solution of the primary nanofiltration system.
In the first step, the concentration of uranium in the waste liquid of the evaporation pool is 10-500mg/L, CO 3 2- The concentration is 0-2000mg/L, SO 4 2- Concentration of 0-50g/L, Cl - The concentration is 0-50 g/L. The mechanical filtration is bag filtration, the aperture of the filter bag is 50-100um, and when the pressure of the filter is higher>Replacing the filter bag at 0.5 MPa;
in the second step, the ultrafiltration membrane adopts a roll-shaped membrane or a plate-shaped membrane, the material of the membrane is polyamide, and the aperture specification of the ultrafiltration membrane is 0.05um-1 nm. The operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the ultrafiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and the ultrafiltration operation is finished when the separation volume ratio of the concentrated solution to the dialysate is 1:10-1: 100.
In the third step, the nanofiltration membrane adopts a coiled membrane or a plate-shaped membrane, the membrane material is polyamide, the nanofiltration membrane has a molecular weight cut-off of 200-600, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the nanofiltration system is intermittent operation, the concentrated solution returns to the raw material tank, the dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:5-1:30, the nanofiltration operation is completed. The uranium concentration of the nanofiltration product liquid is 1-10g/L, and the uranium concentration of the dialysate liquid is less than 10 mg/L.
In the fourth step, the pH value of the third-stage filtrate is 2-4.
In the fifth step, the nanofiltration membrane adopts a rolled membrane or a plate-shaped membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 200-600, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the nanofiltration system is in intermittent operation, the concentrated solution returns to the raw material tank, the dialysate is discharged to the secondary filtrate, and when the separation volume ratio of the concentrated solution to the dialysate is 1:3-1:10, the nanofiltration operation is completed. The concentration of uranium in the nanofiltration product liquid is 20-50g/L, and the concentration of uranium in the dialysate is 50-500 mg/L.
Example 1
Certain sandstone uranium mine adopting CO 2 +O 2 The uranium is leached by the ground leaching process, and the uranium concentration in the waste water of the evaporation pond is 307mg/L, CO 3 2- The concentration is 620mg/L, SO 4 2- Concentration 11g/L, Cl - The concentration was 1.2 g/L. The method of the invention is adopted to treat the wastewater.
Step 1, conveying the waste liquid of the evaporation pool to a mechanical filter by a pump to remove solid particles, wherein the mechanical filter is a bag filter, the aperture specification of meshes of a filter bag is 50um, and when the pressure of the filter is more than 0.5MPa, replacing the filter bag; the clear liquid is first-stage filtrate, the step 2 is carried out, and solid particles remained in the filter bag are washed and discarded to a tailing pond;
step 2, conveying the primary filtrate from the step 1 to an ultrafiltration system as a raw material liquid of the ultrafiltration system to remove suspended solids, macromolecular organic matters and colloids, and removing ultrafiltration dialysate to obtain a secondary filtrate, and performing the step 3 to discharge the ultrafiltration concentrated liquid to an evaporation tank; the ultrafiltration membrane is a coiled membrane or a plate-shaped membrane, the material of the membrane is polyamide, and the pore diameter specification of the ultrafiltration membrane is 0.05 um. The operation temperature is room temperature, the operation pressure is 0.5MPa, the ultrafiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and the ultrafiltration operation is finished when the separation volume ratio of the concentrated solution to the dialysate is 1: 10.
Step 3, conveying the secondary filtrate from the step 2 as a raw material liquid of the primary nanofiltration system to a nanofiltration system for uranium enrichment, wherein the concentrated solution is a tertiary filtrate, and performing step 4, and removing the dialysate from a waste liquid pool for evaporation treatment; the nanofiltration membrane is a coiled membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 300, the operation temperature is room temperature, the operation pressure is 0.5MPa, the nanofiltration system is operated intermittently, concentrated solution returns to a raw material tank, dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:10, the nanofiltration operation is completed. The uranium concentration of the nanofiltration product liquid is 3.3g/L, and the uranium concentration of the dialysate liquid is 8 mg/L.
And 4, feeding the tertiary filtrate from the step 3 into a stirring tank, adding concentrated hydrochloric acid with the mass fraction of about 35% into the stirring tank while stirring to acidify the tertiary filtrate, and controlling the pH value of the acidified tertiary filtrate to be 4 and fully reacting.
And 5, conveying the acidified tertiary filtrate from the step 4 to a secondary nanofiltration system for re-enrichment of uranium, wherein the concentrated solution is a product solution, and the secondary filtrate from the step 3 is used as a raw material solution of the primary nanofiltration system. The nanofiltration membrane is a coiled membrane or a plate-shaped membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 200, the operation temperature is room temperature, the operation pressure is 0.5MPa, the nanofiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged to the secondary filtrate, and when the separation volume ratio of the concentrated solution to the dialysate is 1:10, the nanofiltration operation is completed. The uranium concentration of the nanofiltration product liquid is 33.6g/L, the uranium concentration of the dialysate is 264mg/L, and the dialysate returns to the raw material liquid for continuous treatment.
Example 2
Certain sandstone uranium mine adopts CO 2 +O 2 The uranium is leached by the ground leaching process, and the uranium concentration in the waste water of the evaporation pond is 31mg/L, CO 3 2- The concentration is 501mg/L, SO 4 2- Concentration of 20g/L, Cl - The concentration was 438 mg/L.
Step 1, conveying the waste liquid of the evaporation pool to a mechanical filter by a pump to remove solid particles, wherein the mechanical filter is a bag filter, the aperture specification of meshes of a filter bag is 75um, and the filter bag is replaced when the pressure of the filter is more than 0.5 MPa; the clear liquid is first-level filtrate, the step 2 is carried out, and the solid particles remained in the filter bag are washed and discarded to a tailing pond;
step 2, conveying the primary filtrate from the step 1 serving as raw material liquid of an ultrafiltration system to the ultrafiltration system to remove suspended solids, macromolecular organic matters and colloids, and discharging ultrafiltration dialysate serving as secondary filtrate to an evaporation tank in the step 3; the ultrafiltration membrane is roll-shaped membrane or plate-shaped membrane, the material of the membrane is polyamide, and the pore diameter specification of the ultrafiltration membrane is 0.05 um. The operation temperature is room temperature, the operation pressure is 0.5MPa, the ultrafiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and the ultrafiltration operation is finished when the separation volume ratio of the concentrated solution to the dialysate is 1: 100.
Step 3, conveying the secondary filtrate from the step 2 as a raw material liquid of the primary nanofiltration system to a nanofiltration system for uranium enrichment, wherein the concentrated solution is a tertiary filtrate, and performing evaporation treatment on the concentrated solution in a waste liquid pool in the step 4; the nanofiltration membrane is a coiled membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 200, the operation temperature is room temperature, the operation pressure is 0.5MPa, the nanofiltration system is operated intermittently, concentrated solution returns to a raw material tank, dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:50, the nanofiltration operation is completed. The uranium concentration of the nanofiltration product liquid is 1.1g/L, and the uranium concentration of the dialysate liquid is 9 mg/L.
And 4, feeding the third-stage filtrate from the step 3 into a stirring tank, adding concentrated hydrochloric acid with the mass fraction of about 35% into the stirring tank while stirring to acidify the third-stage filtrate, wherein the pH of the acidified third-stage filtrate is 3, and the third-stage filtrate is reacted fully.
And 5, conveying the acidified tertiary filtrate from the step 4 to a secondary nanofiltration system for carrying out secondary enrichment on uranium, wherein the concentrated solution is a product solution, and the secondary filtrate from the step 3 is removed from the dialysate to be used as a raw material solution of the primary nanofiltration system. The nanofiltration membrane is a coiled membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 300, the operation temperature is room temperature, the operation pressure is 1.5MPa, the nanofiltration system is operated intermittently, concentrated solution returns to a raw material tank, dialyzate is discharged to secondary filtrate, and the nanofiltration operation is finished when the separation volume ratio of the concentrated solution to the dialyzate is 1: 20. The uranium concentration of the nanofiltration product liquid is 22.1g/L, and the uranium concentration of the dialysate liquid is 50 mg/L.
Example 3
Certain sandstone uranium mine adopts CO 2 +O 2 The uranium is leached by the ground leaching process, and the uranium concentration in the waste water of the evaporation pond is 500mg/L, CO 3 2- The concentration is 1.8g/L, SO 4 2- Concentration 33g/L, Cl - The concentration was 35 g/L.
Step 1, conveying the waste liquid of the evaporation pool to a mechanical filter by a pump to remove solid particles, wherein the mechanical filter is a bag filter, the aperture specification of meshes of a filter bag is 100um, and when the pressure of the filter is more than 0.5MPa, replacing the filter bag; the clear liquid is first-level filtrate, the step 2 is carried out, and the solid particles remained in the filter bag are washed and discarded to a tailing pond;
step 2, conveying the primary filtrate from the step 1 serving as raw material liquid of an ultrafiltration system to the ultrafiltration system to remove suspended solids, macromolecular organic matters and colloids, and discharging ultrafiltration dialysate serving as secondary filtrate to an evaporation tank in the step 3; the ultrafiltration membrane is roll-shaped membrane or plate-shaped membrane, the material of the membrane is polyamide, and the pore diameter specification of the ultrafiltration membrane is 0.05 um. The operation temperature is room temperature, the operation pressure is 0.5MPa, the ultrafiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and the ultrafiltration operation is finished when the separation volume ratio of the concentrated solution to the dialysate is 1: 100.
Step 3, conveying the secondary filtrate from the step 2 as a raw material liquid of the primary nanofiltration system to a nanofiltration system for uranium enrichment, wherein the concentrated solution is a tertiary filtrate, and performing step 4, and removing the dialysate from a waste liquid pool for evaporation treatment; the nanofiltration membrane is a coiled membrane, the membrane material is polyamide, the cut-off molecular weight of the nanofiltration membrane is 200, the operation temperature is room temperature, the operation pressure is 0.5MPa, the nanofiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:10, the nanofiltration operation is completed. The uranium concentration of the nanofiltration product liquid is 5.3g/L, and the uranium concentration of the dialysate is 19 mg/L.
And 4, feeding the third-stage filtrate from the step 3 into a stirring tank, adding concentrated hydrochloric acid with the mass fraction of about 35% into the stirring tank while stirring to acidify the third-stage filtrate, wherein the pH value of the acidified third-stage filtrate is 2, and the third-stage filtrate is reacted fully.
And 5, conveying the acidified tertiary filtrate from the step 4 to a secondary nanofiltration system for re-enrichment of uranium, wherein the concentrated solution is a product solution, and the secondary filtrate from the step 3 is used as a raw material solution of the primary nanofiltration system. The nanofiltration membrane is a coiled membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 600, the operation temperature is room temperature, the operation pressure is 3MPa, the nanofiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged to the secondary filtrate, and when the separation volume ratio of the concentrated solution to the dialysate is 1:7, the nanofiltration operation is completed. The uranium concentration of the nanofiltration product liquid is 42g/L, and the uranium concentration of the dialysate is 64 mg/L.
In the attached drawings of the disclosed embodiment of the invention, only methods related to the disclosed embodiment are related, other methods can refer to common design, and the same embodiment and different embodiments of the invention can be combined mutually under the condition of no conflict;
the above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the scope of the present invention.

Claims (8)

1. CO (carbon monoxide) 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool comprises five steps and is characterized in that:
conveying the waste liquid of the evaporation tank to a machine by using a pump for filtering to remove solid particles, wherein clear liquid is primary filtrate, and removing the solid particles remained in a filter bag to a tailing pond by using a step two;
step two, conveying the primary filtrate from the step one as a raw material liquid of an ultrafiltration system to the ultrafiltration system to remove suspended solids, macromolecular organic matters and colloids, and discharging ultrafiltration concentrated liquid to an evaporation tank in step three, wherein ultrafiltration dialyzate is secondary filtrate;
step three, conveying the secondary filtrate from the step two as raw material liquid of the primary nanofiltration system to a nanofiltration system for uranium enrichment, wherein the concentrated solution is tertiary filtrate, and removing the filtrate from the step four to a waste liquid pool for evaporation treatment;
step four, feeding the third-stage filtrate from the step three into a stirring tank, adding concentrated hydrochloric acid with the mass fraction of about 35% into the stirring tank while stirring to acidify the third-stage filtrate, and fully reacting;
fifthly, conveying the acidified tertiary filtrate from the fourth step to a secondary nanofiltration system for re-enrichment of uranium, wherein the concentrated solution is a product solution, and the secondary filtrate from the third step is used as a raw material solution of the primary nanofiltration system;
in the second step, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the ultrafiltration system is operated intermittently, the concentrated solution returns to the raw material tank, the dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:10-1:100, the ultrafiltration operation is finished.
2. CO as claimed in claim 1 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: in the first step, the concentration of uranium in the waste liquid of the evaporation pool is 10-500mg/L, CO 3 2- The concentration is 0-2000mg/L, SO 4 2- Concentration of 0-50g/L, Cl - The concentration is 0-50 g/L.
3. A CO as claimed in claim 2 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: the mechanical filtration is bag filtration, the aperture of the filter bag is 50-100 μm, and the pressure of the filter is measured>The filter bag is replaced under 0.5 MPa.
4. CO as claimed in claim 1 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: in the second step, the ultrafiltration membrane is a roll-shaped membrane or a plate-shaped membrane, the material of the membrane is polyamide, and the pore size of the ultrafiltration membrane is 0.05 μm-1 nm.
5. A process as claimed in claim 1CO 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: in the third step, the nanofiltration membrane adopts a coiled membrane or a plate-shaped membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 200-600, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the nanofiltration system is intermittent operation, the concentrated solution returns to the raw material tank, the dialysate is discharged, and when the separation volume ratio of the concentrated solution to the dialysate is 1:5-1:30, the nanofiltration operation is finished; the uranium concentration of nanofiltration product liquid is 1-10g/L, and the uranium concentration of dialysate liquid<10mg/L。
6. CO as claimed in claim 1 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: in the fourth step, the pH value of the third-stage filtrate is 2-4.
7. CO as claimed in claim 1 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: in the fifth step, the nanofiltration membrane adopts a coiled membrane or a plate-shaped membrane, the material of the membrane is polyamide, the molecular weight cut-off of the nanofiltration membrane is 200-600, the operation temperature is room temperature, the operation pressure is 0.5-3.0MPa, the nanofiltration system is in intermittent operation, the concentrated solution returns to the raw material tank, and the dialysate is discharged to the secondary filtrate.
8. A CO as claimed in claim 7 2 +O 2 The method for recovering uranium from the waste water of the in-situ leaching uranium mining evaporation pool is characterized by comprising the following steps: when the separation volume ratio of the concentrated solution to the dialyzate is 1:3-1:10, the nanofiltration operation is finished; the uranium concentration of the nanofiltration product liquid is 20-50g/L, and the uranium concentration of the dialysate is 50-500 mg/L.
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WO1999023263A1 (en) * 1997-10-30 1999-05-14 Hw Process Technologies, Inc. Method for removing contaminants from process streams in metal recovery processes
US6156186A (en) * 1997-10-30 2000-12-05 Hw Process Technologies, Inc. Method for removing contaminants from process streams in metal recovery processes
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