CN106507867B - Soak and leach liquid processing method in Bicarbonatetypegroundwater plus CO2 and O2 ground - Google Patents
Soak and leach liquid processing method in Bicarbonatetypegroundwater plus CO2 and O2 groundInfo
- Publication number
- CN106507867B CN106507867B CN201110011773.6A CN201110011773A CN106507867B CN 106507867 B CN106507867 B CN 106507867B CN 201110011773 A CN201110011773 A CN 201110011773A CN 106507867 B CN106507867 B CN 106507867B
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- liquid
- uranium
- resin
- leaching
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Links
- 239000007788 liquid Substances 0.000 title claims abstract description 146
- 238000003672 processing method Methods 0.000 title claims abstract description 13
- 239000011347 resin Substances 0.000 claims abstract description 93
- 229920005989 resin Polymers 0.000 claims abstract description 93
- 229910052770 Uranium Inorganic materials 0.000 claims abstract description 85
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 claims abstract description 85
- 238000002386 leaching Methods 0.000 claims abstract description 78
- 239000000243 solution Substances 0.000 claims abstract description 53
- 238000000605 extraction Methods 0.000 claims abstract description 48
- 238000001556 precipitation Methods 0.000 claims abstract description 40
- 238000010521 absorption reaction Methods 0.000 claims abstract description 25
- 230000032683 aging Effects 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims abstract description 15
- 239000002002 slurry Substances 0.000 claims abstract description 15
- 238000001035 drying Methods 0.000 claims abstract description 14
- 238000005342 ion exchange Methods 0.000 claims abstract description 14
- 238000005406 washing Methods 0.000 claims abstract description 10
- 239000003513 alkali Substances 0.000 claims abstract description 8
- 238000001914 filtration Methods 0.000 claims abstract description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 70
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 57
- 239000003480 eluent Substances 0.000 claims description 35
- 239000011780 sodium chloride Substances 0.000 claims description 35
- VEXZGXHMUGYJMC-UHFFFAOYSA-N HCl Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 30
- 238000007792 addition Methods 0.000 claims description 27
- UIIMBOGNXHQVGW-UHFFFAOYSA-M sodium bicarbonate Substances [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 23
- 238000010828 elution Methods 0.000 claims description 22
- 239000012452 mother liquor Substances 0.000 claims description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-O ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 17
- 238000001223 reverse osmosis Methods 0.000 claims description 16
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 16
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 15
- 239000002351 wastewater Substances 0.000 claims description 15
- 238000001764 infiltration Methods 0.000 claims description 14
- 238000001704 evaporation Methods 0.000 claims description 13
- 239000002585 base Substances 0.000 claims description 9
- 239000002244 precipitate Substances 0.000 claims description 8
- 239000000047 product Substances 0.000 claims description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 8
- 239000004793 Polystyrene Substances 0.000 claims description 7
- 239000003957 anion exchange resin Substances 0.000 claims description 7
- 239000011259 mixed solution Substances 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 229920002223 polystyrene Polymers 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 238000004458 analytical method Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 238000004080 punching Methods 0.000 claims 1
- 239000003153 chemical reaction reagent Substances 0.000 abstract description 5
- 238000002360 preparation method Methods 0.000 abstract description 4
- 238000002347 injection Methods 0.000 abstract description 3
- 239000007924 injection Substances 0.000 abstract description 3
- 238000003911 water pollution Methods 0.000 abstract description 3
- 239000011734 sodium Substances 0.000 description 28
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 23
- 238000011065 in-situ storage Methods 0.000 description 10
- 239000002253 acid Substances 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 9
- 239000001099 ammonium carbonate Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 238000007598 dipping method Methods 0.000 description 5
- 239000004575 stone Substances 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L Calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 3
- PRKQVKDSMLBJBJ-UHFFFAOYSA-N Ammonium carbonate Chemical compound N.N.OC(O)=O PRKQVKDSMLBJBJ-UHFFFAOYSA-N 0.000 description 3
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 3
- 235000012501 ammonium carbonate Nutrition 0.000 description 3
- 150000001450 anions Chemical class 0.000 description 3
- ATRRKUHOCOJYRX-UHFFFAOYSA-N azanium;hydron;carbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate dianion Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 238000000151 deposition Methods 0.000 description 2
- 230000001131 transforming Effects 0.000 description 2
- 241000208340 Araliaceae Species 0.000 description 1
- 229960005069 Calcium Drugs 0.000 description 1
- 229960003563 Calcium Carbonate Drugs 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000000903 blocking Effects 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 229910052570 clay Inorganic materials 0.000 description 1
- 230000002860 competitive Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000005035 ginseng Nutrition 0.000 description 1
- 235000008434 ginseng Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 230000000116 mitigating Effects 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 239000011028 pyrite Substances 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000001187 sodium carbonate Substances 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N sodium cation Chemical group [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 230000001502 supplementation Effects 0.000 description 1
Abstract
The present invention is provided in a kind of Bicarbonatetypegroundwater plus CO2And O2Ground leaching and leaching liquid processing method, which comprises the steps：(1) leaching solution adds CO2And O2Injection underground Leaching Uranium, obtains Uranium extraction liquid；(2) CO is added in Uranium extraction liquid2Uranium extraction liquid pH value is adjusted, then mechanical filter；(3) ion exchange absorption is carried out to Uranium extraction liquid in adsorption tower；(4) drip washing is carried out to saturated resin, obtains Cl-The lean resin of type and drip washing qualifying liquid；(5) to Cl-The lean resin of type is made the transition with adsorption tail liquid；(6) acidifying plus the aging precipitation of alkali room temperature is carried out to drip washing qualifying liquid, and uranium product is obtained to precipitation slurry washing, filtration, drying.The inventive method only adds O2And CO2And without other reagents, do not result in jamming of ore bed and underground water pollution；Preparation process realizes integration simultaneously, simplifies operation, cost-effective.
Description
Technical field
The present invention relates to a kind of ground-dipping uranium extraction leaching method and leaching liquid processing method, and in particular to one
Plant in Bicarbonatetypegroundwater plus CO2And O2Ground-dipping uranium extraction method and leach liquid processing method.
Technical characteristic be elute after poor resin new transition mode and transition waste water by counter-infiltration at
The technology of reuse after reason.
Background technology
Ground-dipping uranium extraction (in-situ leaching uranium) is will by the fluid injection well from earth drilling to ledge
The leaching solution prepared by a certain percentage be injected into ore bed, the leaching solution and ore of injection it is useful into
The biochemical reaction of tap triggering, the soluble compound of generation the leaving under diffusion and convection action
Reaction zone enters forms leachate along along the solution liquid stream of ore bed infiltration migration；Leachate passes through ore deposit
Layer is promoted to earth's surface from drawing liquid well, and the leachate of extraction is delivered to recovery workshop and carries out ion exchange etc.
PROCESS FOR TREATMENT, finally obtains qualified products.In-situ leaching uranium method is widely used in permeable sand
Lithotype uranium deposit is a kind of centralized procurement, smelting in the new uranium mining method of one.
In-situ leaching uranium is leached by underground and leachate processing two large divisions constitutes.Leached in ore body
Part can be divided to two classes according to the difference of the leaching solution of selection：Acid in-situ leaching and alkaline in situ leach.Acid system
Leaching is exactly the dipped journey in ground for using acid solution as leachant.Acid in-situ leaching leachant can be used as
Reagent has：Sulfuric acid, nitric acid, hydrochloric acid etc..Alkaline in situ leach is used as leachant using alkaline solution
The dipped journey in ground.Can mainly have as the leachant of alkaline in situ leach：Sodium carbonate, ammonium carbonate, bicarbonate
Sodium, ammonium hydrogen carbonate etc..Acid system easily causes underground ore bed blocking, and acid-base method all can be different degrees of
Cause the pollution of underground water in ground.
In Pregnant Solution From In-situ Leaching processing method includes the steps such as absorption, elution, precipitation, filtering.Ground
The ion exchange absorption process commonly used in uranium is adopted in leaching ADSORPTION IN A FIXED BED and fluidised bed adsorption two
Kind.Ion exchange absorption technique in, poor resin enter next time adsorb before generally require into
Row transition, generally using the higher reagent of concentration as transition agent, transition agent leading ion can not be kept away
It can be transferred in the tail washings of subsequent adsorbtion with exempting from；If resin does not make the transition, the leading ion of eluent
It can be transferred in subsequent adsorbtion tail washings.Accumulation if things go on like this, not only polluted underground water environment, may be used also
The adsorption efficiency of uranium in leachate can be influenceed due to the competitive Adsorption of these ions.
For the uranium-bearing ore bed in bicarbonate root type water-bearing layer, because carbonate content is high, in water-bearing layer
Bicarbonate concentration reached 2600mg/L or so.Such mineral deposit uses traditional ground-dipping uranium extraction
Method occurs in that various problems.Ore and acid consumpting substance in underground water are more, when conventional acid is leached not
Only acid consumption is high, and as pH value declines, the calcium sulfate that ore bed can be generated is blocked.The opposing party
Face, pyrite content is also higher in this uranium-bearing ore bed, it is oxidized after can produce sulfuric acid, and with
Carbonate reaction in ore, during alkaline in situ leach, can consume substantial amounts of alkaline leachant, due to pH
The rise of value, ore bed is easy to produce calcium carbonate and calcium sulfate precipitation and block again.
The content of the invention
It is an object of the invention to provide add CO in a kind of Bicarbonatetypegroundwater2And O2Ground soak and
Liquid processing method is leached, it adds O2And CO2And without other reagents, do not result in ore bed
Block and underground water pollution；Preparation process realizes integration simultaneously, simplifies operation, cost-effective.
Realize the technical scheme of the object of the invention：Add CO in a kind of Bicarbonatetypegroundwater2And O2Ground
Leaching and leaching liquid processing method, it comprises the following steps：
(1) leaching solution adds CO2And O2Underground Leaching Uranium is injected, Uranium extraction liquid is obtained；It is described
CO2Addition is controlled in 100~300mg/L, O2Addition is controlled in 100~300mg/L,
Leaching solution is adsorption tail liquid obtained by underground water or step (3)；
(2) CO is added in the Uranium extraction liquid obtained to step (1)2Uranium extraction liquid pH value is adjusted,
Then mechanical filter；Described CO2Addition is controlled in 100~300mg/L, CO2Pressure control
System adjusts the pH value of Uranium extraction liquid 6.0~8.5 in 0.2~0.7MPa；
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, adopted
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated tree is obtained after absorption
Fat and adsorption tail liquid；
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and pouring
Wash qualifying liquid；Described eluent is NaCl and NaHCO3Mixed solution, wherein NaCl's is dense
Degree control is in 50~100g/L, NaHCO3Concentration control in 10~50g/L；
(5) Cl obtained to step (4)-The poor resin of type utilizes the absorption tail that step (3) is obtained
Liquid is made the transition, and is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining elution
Agent is flowed out；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin of type
The flow control of bed removes the debris remained between most of resin particle and elution in 4~6BV/h
Agent composition, it is 1~2BV to rinse adsorption tail liquid amount；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through
Cl-The flow control of the poor resin bed of type is in 0.5~1BV/h, and the time is 40~20 hours；
(d) reverse-osmosis treated is taken to transition waste water, controls Cl-Clearance reaches more than 95%,
Concentrated water obtained by reverse-osmosis treated is discharged into evaporation tank, fresh water return to step (1) obtained by reverse-osmosis treated
Leaching solution is prepared to recycle.
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation,
When first adding hydrochloric acid and being acidified to pH=4.0~5.0, stop adding hydrochloric acid；Add NaOH tune
It is 11~13 to save pH, is precipitated by the aging of 6~12h normal temperature, and upper solution is containing Na2CO3、
NaCl and NaOH mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry；To Na2U2O7
It is that can obtain uranium product that precipitation slurry, which is washed, filtered, drying,.
Add CO in a kind of Bicarbonatetypegroundwater as described above2And O2Soak and leachate processing on ground
Method, its adsorption tail liquid obtained to step (3) adds CO2And O2, it is configured to leaching solution and returns
Return step (1) to recycle, CO is added in adsorption tail liquid2And O2Concentration controls 100~
300mg/L；
Add CO in a kind of Bicarbonatetypegroundwater as described above2And O2Soak and leachate processing on ground
Method, it contains Na by what step (6) was obtained2CO3, NaCl and NaOH upper strata precipitation it is female
Eluent is prepared in liquid reuse, i.e., NaCl and NaHCO is added into the mother liquor of precipitation of ammonium3, regulationization
Scope of the part required by eluent is studied, return to step (4) is recycled.
Effect of the invention is that：
Add CO in Bicarbonatetypegroundwater of the present invention2And O2Soak and leachate processing side on ground
Method, it adds O2And CO2And without other reagents, add O2Purpose be in ore bed create
Make the inverse process environment of U metallogeny process, CO2Addition just to supplementing HCO3 -Ion is in leaching
Consumption during going out, will not change the pH value of underground water, you can reach the purpose of Leaching Uranium,
Certainly jamming of ore bed and underground water pollution are not resulted in yet.
The present invention adds CO to Uranium extraction liquid before ion exchange absorption is carried out2, to adjust leaching
Go out [UO in liquid pH, increase leachate2(CO3)3]4-[UO2(CO3)2]2-Percentage, can be with
The saturated adsorption capacity of resin is more effectively improved, resin bed is hardened when mitigating absorption.Meanwhile,
The bicarbonate concentration in tail washings is improved, tail washings is used as leaching solution, underground recycling can be injected.
Relatively conventional other acid-base methods leaching method need special leaching solution preparation process, the present invention
So that the preparation process that ion-exchange absorption echos leaching solution realizes integration, operation is simplified,
Cost has been saved, production technology is optimized.
The present invention is a kind of ground dipping uranium extracting process method of economical rationality.CO is dissolved in water2As molten
Immersion liquid is better than alkaline Leaching systems such as ammonium carbonate/ammonium hydrogen carbonate, because ammonium carbonate/ammonium hydrogen carbonate can lead to
Cross ammonium ion and be contained in stratum in clay calcium, sodium ion exchange, improve underground water salinity,
The pollution of underground water is caused, jamming of ore bed is also easily caused, is unfavorable for the leaching process of uranium.
The present invention utilizes the HCO contained in adsorption tail liquid3 -Ion, is carried out to the poor resin after elution
Transition, it is to avoid Cl-Polluted underground water, process economicses are rationally, easy to operate, and transformation efficiency is high,
Macroreticular resin by transition is HCO3 -Type, HCO when adsorbing again3 -Ion enters absorption tail
Liquid, on underground water without influence.Transition waste water reverse osmosis handling process reduces the outer discharge capacity of waste water, instead
Fresh water can be with leaching solution be prepared after infiltration processing, concentrated water is discharged into evaporation tank, it is to avoid Cl-Over the ground
The pollution of lower water.
The depositing technology that the present invention is provided eliminates high-temperature heating and set compared with traditional depositing technology
It is standby so that energy consumption, equipment investment are substantially reduced, acid consumption and alkaline consumption are reduced, control ginseng has been refined
Number, significantly reduces production cost, meanwhile, mother liquor of precipitation of ammonium, which can be converted, does eluent recycling,
Outer pollution discharging is reduced to greatest extent, and this precipitation invented technology is simple to operate, and production cost is low,
Production efficiency is high.
Brief description of the drawings
Fig. 1 be Bicarbonatetypegroundwater of the present invention in plus CO2And O2Soak and leachate on ground
Processing method process chart.
Embodiment
Below in conjunction with the accompanying drawings with specific embodiment to of the present invention a kind of in heavy carbonic type underground
Add CO in water2And O2Ground leaching method and leaching liquid processing method are further described.
Embodiment 1
Certain uranium ore water-bearing layer containing ore deposit underground water is melted into classifying type with HCO3- Na and HCO3·Cl-
Based on Na types, ledge roof and floor is mainly mud stone, and thickness is relatively stablized, and water isolating is preferable.
Salinity 3.5g/L, 15 DEG C of water temperature, pH value is that 6.8, Eh values are 150mv, HCO3 -Ion
Concentration is 2000mg/L, and dissociate O2Concentration ＜ 2mg/L, hydro-geochemical environment is in weak
Redox zone state.
As shown in figure 1, carrying out underground leaching and leachate processing using method of the present invention：
(1) leaching solution adds CO2And O2Go to well site to inject underground Leaching Uranium, obtain Uranium extraction liquid；
Described CO2Addition is controlled in 300mg/L, O2Addition is controlled in 300mg/L, leaching solution
For underground water.
(2) uranium concentration obtained to step (1) for 45mg/L Uranium extraction liquid in add CO2
Uranium extraction liquid pH value is adjusted, then mechanical filter；Described CO2Addition control exists
300mg/L, CO2Stress control adjusts the pH value of Uranium extraction liquid 6.5 in 0.6MPa.Herein
PH value condition Uranium extraction liquid is easily formed the [UO for being dissolved in water2(CO3)3]4-Or [UO2(CO3)2]2-Network
Anion, the need for this step is not only leachate processing, while being also that leaching solution prepares supplement
The HCO of consumption3 -The need for.
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, adopted
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated tree is obtained after absorption
Fat and adsorption tail liquid.
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and pouring
Wash qualifying liquid；Described eluent is NaCl and NaHCO3Mixed solution, wherein NaCl's is dense
Degree control is in 80g/L, NaHCO3Concentration control in 20g/L；
The adsorption tail liquid obtained to step (3) adds CO2And O2, it is configured to leaching solution return to step
(1) recycle, CO is added in adsorption tail liquid2And O2Concentration is controlled in 300mg/L, leaching solution
Middle HCO3 -Concentration is that 2560mg/L (adds CO2The HCO of consumption can be supplemented3 -, make HCO3 -
Content is in 2000~2600mg/L).
(5) Cl obtained after terminating to step (4) elution technique-The poor resin of type utilizes step (3)
Obtained adsorption tail liquid is made the transition, and is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining elution
Agent is flowed out, and is discharged into eluent with liquid pool；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin of type
The flow control of bed in 5BV/h, remove the debris remained between most of resin particle and eluent into
Point, it is 2BV to rinse adsorption tail liquid amount, and recoil waste water is discharged into evaporation tank；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through
Cl-The flow control of the poor resin bed of type is in 0.7BV/h, and the time is 32 hours；
(d) reverse-osmosis treated is taken to transition waste water, the counter-infiltration system rate of recovery is set to 75%,
Control Cl-Clearance reaches more than 95%, and concentrated water obtained by reverse-osmosis treated is discharged into evaporation tank, instead
Infiltration processing gained fresh water return to step (1) is prepared leaching solution and recycled.
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation,
When first addition hydrochloric acid is acidified to pH=4.3, stop adding hydrochloric acid；Add NaOH regulation pH
For 13, precipitated by the aging of 12h normal temperature, upper solution is containing Na2CO3, NaCl and NaOH
Mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry.To Na2U2O7The washing of precipitation slurry,
Filtering, drying is that can obtain uranium product.Na will be contained2CO3, NaCl and NaOH upper strata precipitation
Eluent is prepared in mother liquor reuse, i.e., NaCl and NaHCO is added into the mother liquor of precipitation of ammonium3, regulation
Chemical analysis is the scope required by eluent, and return to step (4) is recycled.
The resin after the transition of adsorption tail liquid circular treatment is used for multiple times, its absorption property keeps stable,
The average chloride content of resin is 60.82mg/mL wet resins before transition, after being made the transition using adsorption tail liquid
The average chloride content of resin is 1.52mg/mL wet resins, transformation efficiency 97.6%.
Embodiment 2
Certain uranium ore water-bearing layer containing ore deposit underground water is melted into classifying type with HCO3- Na and HCO3·Cl-
Based on Na types, ledge roof and floor is mainly mud stone, and thickness is relatively stablized, and water isolating is preferable.
Salinity 3.5g/L, 15 DEG C of water temperature, pH value is that 6.8, Eh values are 150mv, HCO3 -Ion
Concentration is 2300mg/L, and dissociate O2Concentration ＜ 2mg/L, hydro-geochemical environment is in weak
Redox zone state.
As shown in figure 1, carrying out underground leaching and leachate processing using method of the present invention：
(1) leaching solution adds CO2And O2Go to well site to inject underground Leaching Uranium, obtain Uranium extraction liquid；
Described CO2Addition is controlled in 200mg/L, O2Addition is controlled in 200mg/L, leaching solution
The adsorption tail liquid obtained by step (3).
(2) uranium concentration obtained to step (1) for 50mg/L Uranium extraction liquid in add CO2
Uranium extraction liquid pH value is adjusted, then mechanical filter；Described CO2Addition control exists
200mg/L, CO2Stress control adjusts the pH value of Uranium extraction liquid 6.9 in 0.4MPa.Herein
PH value condition Uranium extraction liquid is easily formed the [UO for being dissolved in water2(CO3)3]4-Or [UO2(CO3)2]2-Network
Anion, the need for this step is not only leachate processing, while being also that leaching solution prepares supplement
The HCO of consumption3 -The need for.
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, adopted
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated tree is obtained after absorption
Fat and adsorption tail liquid.
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and pouring
Wash qualifying liquid；Described eluent is NaCl and NaHCO3Mixed solution, wherein NaCl's is dense
Degree control is in 90g/L, NaHCO3Concentration control in 30g/L；
The adsorption tail liquid obtained to step (3) adds CO2And O2, it is configured to leaching solution return to step
(1) recycle, CO is added in adsorption tail liquid2And O2Concentration is controlled in 200mg/L, leaching solution
Middle HCO3 -Concentration is that 2470mg/L (adds CO2The HCO of consumption can be supplemented3 -, make HCO3 -
Content is in 2000~2600mg/L).
(5) Cl obtained after terminating to step (4) elution technique-The poor resin of type utilizes step (3)
Obtained adsorption tail liquid is made the transition, and is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining elution
Agent is flowed out, and is discharged into eluent with liquid pool；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin of type
The flow control of bed in 4BV/h, remove the debris remained between most of resin particle and eluent into
Point, it is 1.5BV to rinse adsorption tail liquid amount, and recoil waste water is discharged into evaporation tank；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through
Cl-The flow control of the poor resin bed of type is in 0.5BV/h, and the time is 28 hours；
(d) reverse-osmosis treated is taken to transition waste water, the counter-infiltration system rate of recovery is set to 75%,
Control Cl-Clearance reaches more than 95%, and concentrated water obtained by reverse-osmosis treated is discharged into evaporation tank, instead
Infiltration processing gained fresh water return to step (1) is prepared leaching solution and recycled.
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation,
When first addition hydrochloric acid is acidified to pH=4.7, stop adding hydrochloric acid；Add NaOH regulation pH
For 12.8, precipitated by the aging of 11h normal temperature, upper solution is containing Na2CO3, NaCl and NaOH
Mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry.To Na2U2O7The washing of precipitation slurry,
Filtering, drying is that can obtain uranium product.Na will be contained2CO3, NaCl and NaOH upper strata precipitation
Eluent is prepared in mother liquor reuse, i.e., NaCl and NaHCO is added into the mother liquor of precipitation of ammonium3, regulation
Chemical analysis is the scope required by eluent, and return to step (4) is recycled.
Embodiment 3
Certain uranium ore water-bearing layer containing ore deposit underground water is melted into classifying type with HCO3- Na and HCO3·Cl-
Based on Na types, ledge roof and floor is mainly mud stone, and thickness is relatively stablized, and water isolating is preferable.
Salinity 3.5g/L, 15 DEG C of water temperature, pH value is that 6.8, Eh values are 150mv, HCO3 -Ion
Concentration is 2600mg/L, and dissociate O2Concentration ＜ 2mg/L, hydro-geochemical environment is in weak
Redox zone state.
As shown in figure 1, carrying out underground leaching and leachate processing using method of the present invention：
(1) leaching solution adds CO2And O2Go to well site to inject underground Leaching Uranium, obtain Uranium extraction liquid；
Described CO2Addition is controlled in 100mg/L, O2Addition is controlled in 100mg/L, leaching solution
The adsorption tail liquid obtained by underground water or step (3).
(2) uranium concentration obtained to step (1) for 45mg/L Uranium extraction liquid in add CO2
Uranium extraction liquid pH value is adjusted, then mechanical filter；Described CO2Addition control exists
100mg/L, CO2Stress control adjusts the pH value of Uranium extraction liquid 7.5 in 0.3MPa.Herein
PH value condition Uranium extraction liquid is easily formed the [UO for being dissolved in water2(CO3)3]4-Or [UO2(CO3)2]2-Network
Anion, the need for this step is not only leachate processing, while being also that leaching solution prepares supplement
The HCO of consumption3 -The need for.
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, adopted
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated tree is obtained after absorption
Fat and adsorption tail liquid.
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and pouring
Wash qualifying liquid；Described eluent is NaCl and NaHCO3Mixed solution, wherein NaCl's is dense
Degree control is in 100g/L, NaHCO3Concentration control in 40g/L；
The adsorption tail liquid obtained to step (3) adds CO2And O2, it is configured to leaching solution return to step
(1) recycle, CO is added in adsorption tail liquid2And O2Concentration is controlled in 100mg/L, leaching solution
Middle HCO3 -Concentration is that 2330mg/L (adds CO2The HCO of consumption can be supplemented3 -, make HCO3 -
Content is in 2000~2600mg/L).
(5) Cl obtained after terminating to step (4) elution technique-The poor resin of type utilizes step (3)
Obtained adsorption tail liquid is made the transition, and is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining elution
Agent is flowed out, and is discharged into eluent with liquid pool；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin of type
The flow control of bed in 6BV/h, remove the debris remained between most of resin particle and eluent into
Point, it is 2BV to rinse adsorption tail liquid amount, and recoil waste water is discharged into evaporation tank；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through
Cl-The flow control of the poor resin bed of type is in 0.6BV/h, and the time is 30 hours；
(d) reverse-osmosis treated is taken to transition waste water, the counter-infiltration system rate of recovery is set to 75%,
Control Cl-Clearance reaches more than 95%, and concentrated water obtained by reverse-osmosis treated is discharged into evaporation tank, instead
Infiltration processing gained fresh water return to step (1) is prepared leaching solution and recycled.
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation,
When first addition hydrochloric acid is acidified to pH=4.5, stop adding hydrochloric acid；Add NaOH regulation pH
For 12.7, precipitated by the aging of 12h normal temperature, upper solution is containing Na2CO3, NaCl and NaOH
Mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry.To Na2U2O7The washing of precipitation slurry,
Filtering, drying is that can obtain uranium product.Na will be contained2CO3, NaCl and NaOH upper strata precipitation
Eluent is prepared in mother liquor reuse, i.e., NaCl and NaHCO is added into the mother liquor of precipitation of ammonium3, regulation
Chemical analysis is the scope required by eluent, and return to step (4) is recycled.
Embodiment 4
Certain uranium ore water-bearing layer containing ore deposit underground water is melted into classifying type with HCO3- Na and HCO3·Cl-
Based on Na types, ledge roof and floor is mainly mud stone, and thickness is relatively stablized, and water isolating is preferable.
Salinity 3.5g/L, 15 DEG C of water temperature, pH value is that 6.8, Eh values are 150mv, HCO3 -Ion
Concentration is 2300mg/L, and dissociate O2Concentration ＜ 2mg/L, hydro-geochemical environment is in weak
Redox zone state.
As shown in figure 1, carrying out underground leaching and leachate processing using method of the present invention：
(1) leaching solution adds CO2And O2Go to well site to inject underground Leaching Uranium, obtain Uranium extraction liquid；
Described CO2Addition is controlled in 150mg/L, O2Addition is controlled in 150mg/L, leaching solution
The adsorption tail liquid obtained by step (3).
(2) uranium concentration obtained to step (1) for 45mg/L Uranium extraction liquid in add CO2
Uranium extraction liquid pH value is adjusted, then mechanical filter；Described CO2Addition control exists
150mg/L, CO2Stress control adjusts the pH value of Uranium extraction liquid 6.0 in 0.2MPa.
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, adopted
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated tree is obtained after absorption
Fat and adsorption tail liquid.
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and pouring
Wash qualifying liquid；Described eluent is NaCl and NaHCO3Mixed solution, wherein NaCl's is dense
Degree control is in 50g/L, NaHCO3Concentration control in 10g/L；
The adsorption tail liquid obtained to step (3) adds CO2And O2, it is configured to leaching solution return to step
(1) recycle, CO is added in adsorption tail liquid2And O2Concentration is controlled in 150mg/L so that
HCO3 -Content is in 2000~2600mg/L.
(5) Cl obtained after terminating to step (4) elution technique-The poor resin of type utilizes step (3)
Obtained adsorption tail liquid is made the transition, and is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining elution
Agent is flowed out, and is discharged into eluent with liquid pool；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin of type
The flow control of bed in 5BV/h, remove the debris remained between most of resin particle and eluent into
Point, it is 1BV to rinse adsorption tail liquid amount, and recoil waste water is discharged into evaporation tank；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through
Cl-The flow control of the poor resin bed of type is in 1BV/h, and the time is 20 hours；
(d) reverse-osmosis treated is taken to transition waste water, the counter-infiltration system rate of recovery is set to 75%,
Control Cl-Clearance reaches more than 95%, and concentrated water obtained by reverse-osmosis treated is discharged into evaporation tank, instead
Infiltration processing gained fresh water return to step (1) is prepared leaching solution and recycled.
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation,
When first addition hydrochloric acid is acidified to pH=4.0, stop adding hydrochloric acid；Add NaOH regulation pH
For 11, precipitated by the aging of 6h normal temperature, upper solution is containing Na2CO3, NaCl and NaOH
Mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry.To Na2U2O7The washing of precipitation slurry,
Filtering, drying is that can obtain uranium product.Na will be contained2CO3, NaCl and NaOH upper strata precipitation
Eluent is prepared in mother liquor reuse, i.e., NaCl and NaHCO is added into the mother liquor of precipitation of ammonium3, regulation
Chemical analysis is the scope required by eluent, and return to step (4) is recycled.
Embodiment 5
Certain uranium ore water-bearing layer containing ore deposit underground water is melted into classifying type with HCO3- Na and HCO3·Cl-
Based on Na types, ledge roof and floor is mainly mud stone, and thickness is relatively stablized, and water isolating is preferable.
Salinity 3.5g/L, 15 DEG C of water temperature, pH value is that 6.8, Eh values are 150mv, HCO3 -Ion
Concentration is 2000mg/L, and dissociate O2Concentration ＜ 2mg/L, hydro-geochemical environment is in weak
Redox zone state.
As shown in figure 1, carrying out underground leaching and leachate processing using method of the present invention：
(1) leaching solution adds CO2And O2Go to well site to inject underground Leaching Uranium, obtain Uranium extraction liquid；
Described CO2Addition is controlled in 250mg/L, O2Addition is controlled in 250mg/L, leaching solution
For underground water.
(2) uranium concentration obtained to step (1) for 50mg/L Uranium extraction liquid in add CO2
Uranium extraction liquid pH value is adjusted, then mechanical filter；Described CO2Addition control exists
250mg/L, CO2Stress control adjusts the pH value of Uranium extraction liquid 8.5 in 0.7MPa.
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, adopted
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated tree is obtained after absorption
Fat and adsorption tail liquid.
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and pouring
Wash qualifying liquid；Described eluent is NaCl and NaHCO3Mixed solution, wherein NaCl's is dense
Degree control is in 90g/L, NaHCO3Concentration control in 50g/L；
The adsorption tail liquid obtained to step (3) adds CO2And O2, it is configured to leaching solution return to step
(1) recycle, CO is added in adsorption tail liquid2And O2Concentration is controlled in 250mg/L, makes HCO3 -Content is in 2000~2600mg/L.
(5) Cl obtained after terminating to step (4) elution technique-The poor resin of type utilizes step (3)
Obtained adsorption tail liquid is made the transition, and is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining elution
Agent is flowed out, and is discharged into eluent with liquid pool；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin of type
The flow control of bed in 6BV/h, remove the debris remained between most of resin particle and eluent into
Point, it is 2BV to rinse adsorption tail liquid amount, and recoil waste water is discharged into evaporation tank；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through
Cl-The flow control of the poor resin bed of type is in 0.9BV/h, and the time is 40 hours；
(d) reverse-osmosis treated is taken to transition waste water, the counter-infiltration system rate of recovery is set to 75%,
Control Cl-Clearance reaches more than 95%, and concentrated water obtained by reverse-osmosis treated is discharged into evaporation tank, instead
Infiltration processing gained fresh water return to step (1) is prepared leaching solution and recycled.
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation,
When first addition hydrochloric acid is acidified to pH=5.0, stop adding hydrochloric acid；Add NaOH regulation pH
For 13, precipitated by the aging of 8h normal temperature, upper solution is containing Na2CO3, NaCl and NaOH
Mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry.To Na2U2O7The washing of precipitation slurry,
Filtering, drying is that can obtain uranium product.Na will be contained2CO3, NaCl and NaOH upper strata precipitation
Eluent is prepared in mother liquor reuse, i.e., NaCl and NaHCO is added into the mother liquor of precipitation of ammonium3, regulation
Chemical analysis is the scope required by eluent, and return to step (4) is recycled.
Claims (3)
1. add CO in a kind of Bicarbonatetypegroundwater2And O2Ground soaks and leaches liquid processing method, and its feature exists
In the process comprises the following steps：
(1) leaching solution adds CO2And O2Underground Leaching Uranium is injected, Uranium extraction liquid is obtained；Described CO2
Addition is controlled in 100~300mg/L, O2Addition is controlled in 100~300mg/L, and leaching solution is
Adsorption tail liquid obtained by underground water or step (3)；
(2) CO is added in the Uranium extraction liquid obtained to step (1)2Uranium extraction liquid pH value is adjusted, then
Mechanical filter；Described CO2Addition is controlled in 100~300mg/L, CO2Stress control 0.2~
0.7MPa, adjusts the pH value of Uranium extraction liquid 6.0~8.5；
(3) ion exchange absorption is carried out to Uranium extraction liquid obtained by step (2) in adsorption tower, use
Resin is macropore polystyrene strong-base anion-exchange resin, and saturated resin and absorption tail are obtained after absorption
Liquid；
(4) saturated resin obtained by step (3) is eluted, obtains Cl-The poor resin of type and elution are closed
Lattice liquid；The eluent used is NaCl and NaHCO3Mixed solution, wherein NaCl concentration control
In 50~100g/L, NaHCO3Concentration control in 10~50g/L；
(5) Cl obtained to step (4)-The adsorption tail liquid that the poor resin of type is obtained using step (3) enters
Row transition, is comprised the following steps that：
(a) with compressed air by Cl in adsorption tower-The poor resin bed drying of type so that remaining eluent stream
Go out；
(b) with adsorption tail liquid recoil Cl-The poor resin bed of type, adsorption tail liquid passes through Cl-The poor resin bed of type
Flow control removes the debris and eluent composition remained between most of resin particle, punching in 4~6BV/h
Adsorption tail liquid amount is washed for 1~2BV；
(c) Cl is passed through at a slow speed with adsorption tail liquid-The poor resin bed transition resin of type, adsorption tail liquid passes through Cl-
The flow control of the poor resin bed of type is in 0.5~1BV/h, and the time is 40~20 hours；
(d) reverse-osmosis treated is taken to transition waste water, controls Cl-Clearance reaches more than 95%, instead
Infiltration processing gained concentrated water is discharged into evaporation tank, and fresh water return to step (1) is prepared obtained by reverse-osmosis treated
Leaching solution is recycled；
(6) the elution qualifying liquid obtained to step (4) carries out acidifying plus alkali normal temperature aging precipitation, first adds
When entering hydrochloric acid and being acidified to pH=4.0~5.0, stop adding hydrochloric acid；Adding NaOH regulation pH is
11~13, precipitated by the aging of 6~12h normal temperature, upper solution is containing Na2CO3, NaCl and NaOH
Mother liquor of precipitation of ammonium, lower floor obtains Na2U2O7Precipitate slurry；To Na2U2O7Precipitate slurry washing, filtering,
Dry and can obtain uranium product.
2. add CO in a kind of Bicarbonatetypegroundwater according to claim 12And O2Soak and soak in ground
Go out liquid processing method, it is characterised in that：The adsorption tail liquid obtained to step (3) adds CO2And O2,
It is configured in leaching solution return to step (1) recycling, adsorption tail liquid plus CO2And O2Concentration is controlled
In 100~300mg/L.
3. add CO in a kind of Bicarbonatetypegroundwater according to claim 1 or 22And O2Soak on ground
With leaching liquid processing method, it is characterised in that：Contain Na by what step (6) was obtained2CO3, NaCl and
Eluent is prepared in NaOH upper strata mother liquor of precipitation of ammonium reuse, i.e., added into the mother liquor of precipitation of ammonium NaCl with
NaHCO3, regulation chemical analysis is the scope required by eluent, and return to step (4) is recycled.
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106507867B true CN106507867B (en) | 2014-01-08 |
Family
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Cited By (8)
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| CN106927539A (en) * | 2015-12-31 | 2017-07-07 | 中核四○四有限公司 | A kind of UF6Produce the processing method of tail gas leacheate |
| CN109577940A (en) * | 2018-12-26 | 2019-04-05 | 核工业北京化工冶金研究院 | A kind of ground-dipping uranium extraction gas control system and method |
| CN110684907A (en) * | 2019-10-23 | 2020-01-14 | 核工业北京化工冶金研究院 | In-situ leaching uranium extraction leaching method for high-mineralization-degree underground water uranium ore |
| CN110773011A (en) * | 2019-10-23 | 2020-02-11 | 核工业北京化工冶金研究院 | Gas-liquid mixing method for in-situ leaching uranium mining |
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| CN106927539A (en) * | 2015-12-31 | 2017-07-07 | 中核四○四有限公司 | A kind of UF6Produce the processing method of tail gas leacheate |
| CN109577940A (en) * | 2018-12-26 | 2019-04-05 | 核工业北京化工冶金研究院 | A kind of ground-dipping uranium extraction gas control system and method |
| CN109577940B (en) * | 2018-12-26 | 2021-04-13 | 核工业北京化工冶金研究院 | In-situ leaching uranium mining gas control system and method |
| CN110684907A (en) * | 2019-10-23 | 2020-01-14 | 核工业北京化工冶金研究院 | In-situ leaching uranium extraction leaching method for high-mineralization-degree underground water uranium ore |
| CN110773011A (en) * | 2019-10-23 | 2020-02-11 | 核工业北京化工冶金研究院 | Gas-liquid mixing method for in-situ leaching uranium mining |
| CN110684907B (en) * | 2019-10-23 | 2021-08-17 | 核工业北京化工冶金研究院 | In-situ leaching uranium extraction leaching method for high-mineralization-degree underground water uranium ore |
| CN110777272A (en) * | 2019-11-12 | 2020-02-11 | 核工业北京化工冶金研究院 | Use method of organic chlorine oxidant in neutral in-situ leaching uranium mining |
| CN112853127A (en) * | 2019-11-12 | 2021-05-28 | 核工业北京化工冶金研究院 | Use method of organic chlorine oxidant in acid leaching uranium mining |
| CN112853127B (en) * | 2019-11-12 | 2022-08-19 | 核工业北京化工冶金研究院 | Use method of organic chlorine oxidant in acid leaching uranium mining |
| CN114291925A (en) * | 2021-12-09 | 2022-04-08 | 中核内蒙古矿业有限公司 | Method for treating strong-basicity silicon-rich uranium-containing solution |
| CN114291925B (en) * | 2021-12-09 | 2024-01-16 | 中核内蒙古矿业有限公司 | Treatment method of strong-alkalinity silicon-rich uranium-containing solution |
| CN117265300A (en) * | 2023-11-23 | 2023-12-22 | 核工业北京化工冶金研究院 | Method for improving reaction rate of neutral in-situ leaching uranium mining |
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