CN117265300A - Method for improving reaction rate of neutral in-situ leaching uranium mining - Google Patents
Method for improving reaction rate of neutral in-situ leaching uranium mining Download PDFInfo
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- 238000002386 leaching Methods 0.000 title claims abstract description 150
- 229910052770 Uranium Inorganic materials 0.000 title claims abstract description 83
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000007935 neutral effect Effects 0.000 title claims abstract description 22
- 238000011065 in-situ storage Methods 0.000 title claims abstract description 17
- 238000005065 mining Methods 0.000 title claims abstract description 10
- 239000003054 catalyst Substances 0.000 claims abstract description 88
- 239000007788 liquid Substances 0.000 claims abstract description 66
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000001301 oxygen Substances 0.000 claims abstract description 46
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 46
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 44
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 42
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000001179 sorption measurement Methods 0.000 claims abstract description 30
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 21
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 21
- 238000005342 ion exchange Methods 0.000 claims abstract description 8
- 239000000243 solution Substances 0.000 claims description 41
- 238000002347 injection Methods 0.000 claims description 15
- 239000007924 injection Substances 0.000 claims description 15
- 239000011259 mixed solution Substances 0.000 claims description 7
- 230000003647 oxidation Effects 0.000 abstract description 6
- 238000007254 oxidation reaction Methods 0.000 abstract description 6
- 238000004904 shortening Methods 0.000 abstract description 3
- 241000695274 Processa Species 0.000 abstract 1
- 238000005086 pumping Methods 0.000 abstract 1
- 238000012360 testing method Methods 0.000 description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 230000000694 effects Effects 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 239000003957 anion exchange resin Substances 0.000 description 4
- 150000001450 anions Chemical class 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000012795 verification Methods 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- -1 uranyl ions Chemical class 0.000 description 1
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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
- C22B60/0221—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes by leaching
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
- C22B3/24—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition by adsorption on solid substances, e.g. by extraction with solid resins
-
- 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
- C22B60/0265—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries extraction by solid resins
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- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Manufacturing & Machinery (AREA)
- Environmental & Geological Engineering (AREA)
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Abstract
The invention provides a method for improving the reaction rate of neutral in-situ leaching uranium mining, and relates to the technical field of in-situ leaching uranium mining. The method provided by the invention comprises the following steps: (1) Injecting a catalyst into a leaching agent for enhanced leaching to obtain uranium-containing leaching solution; the catalyst comprises NaNO 2 One or more of KI and citric acid; (2) Carrying out ion exchange adsorption treatment on the uranium-containing leaching solution to obtain adsorption tail liquid; and (3) introducing oxygen and carbon dioxide into the adsorption tail liquid, and returning the obtained mixed liquid as a leaching agent to the step (1). The method provided by the invention enhances the oxygen oxidation performance through the catalyst in neutral leaching uranium, thereby improving the uranium leaching reaction rate, improving the uranium concentration by more than 10%, shortening the uranium leaching reaction process, and avoiding blockage affecting the pumping and injecting liquid quantity of a well site in the reaction processA plug.
Description
Technical Field
The invention relates to the technical field of in-situ leaching uranium mining, in particular to a method for improving the reaction rate of neutral in-situ leaching uranium mining.
Background
The neutral in-situ leaching uranium is suitable for sandstone uranium deposit with higher carbonate content, has the advantages of low leaching cost, high uranium concentration of leaching liquid, green environmental protection and the like, and is mainly applied to in-situ leaching production in China and the United states.
Neutral leaching is a uranium mining process which is more environment-friendly than acid leaching, and has been industrially applied to a plurality of uranium mines such as Xinjiang Mongolian Golgi, inner Mongolian Tongli, inner Mongolian Karsch and the like in China. Neutral leaching mine use O in China 2 As an oxidant, under the standard condition, the oxygen density is 1.429g/L, and the following problems exist in the use process of neutral leaching uranium: the solubility of oxygen in water is small, the oxygen is difficult to mix with underground water, and the solubility is limited by the pressure-bearing water head of the underground water, so that the oxidation performance of the oxygen is affected. Neutral leaching has been found to suffer from the same problems as alkaline leaching in industrial production over many years, i.e. it has not been as efficient as acid leaching, especially in the middle and late stages of uranium production. At present, a plurality of large-scale uranium ores in China face the current situation of collaborative exploitation of mineral resources, and technical means for realizing rapid and efficient exploitation of the uranium ores are needed. Several researches are made for improving the efficiency of neutral in-situ leaching uranium extraction, shortening the leaching period and improving the utilization rate of uranium resources in domestic and foreign in-situ leaching industries. The early stage intensified leaching is mainly based on the aspects of changing the adding amount, adding mode and the like of the reagent, and enters from the leaching reactionThe intensified leaching of hands is less studied.
Disclosure of Invention
The invention aims to provide a method for improving the reaction rate of neutral in-situ leaching uranium extraction, which can overcome the defect of low oxidation performance of the neutral leaching uranium extraction by using oxygen as an oxidant, effectively oxidize tetravalent uranium in ores, improve the reaction rate of uranium leaching, shorten the leaching period of the ores, and avoid adverse effects such as secondary precipitation of uranyl ions, gas blockage and the like.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a method for improving the reaction rate of neutral in-situ leaching uranium mining, which comprises the following steps:
(1) Injecting a catalyst into a leaching agent for enhanced leaching to obtain uranium-containing leaching solution; the catalyst comprises NaNO 2 One or more of KI and citric acid;
(2) Carrying out ion exchange adsorption treatment on the uranium-containing leaching solution to obtain adsorption tail liquid; and (3) introducing oxygen and carbon dioxide into the adsorption tail liquid, and returning the obtained mixed liquid as a leaching agent to the step (1).
Preferably, the concentration of the catalyst in the leaching agent is 100-600 mg/L.
Preferably, the catalyst is added as a concentrated solution of the catalyst; controlling the flow rate of the catalyst injected into the leaching agent according to formula I;
c2 =v1×c1/(v1+v2) formula I;
in the formula I, c2 is the concentration of the catalyst in the leaching agent, and the unit is mg/L; v1 is the flow rate of the leaching agent before adding the catalyst, and the unit is L; c1 is the concentration of the catalyst concentrated solution, and the unit is mg/L; v2 is the flow rate of the catalyst into the leaching agent in L.
Preferably, after the intensified leaching operation is carried out for a period of time, detecting the concentration of the catalyst in the mixed liquor; and stopping injecting the catalyst when the concentration of the catalyst in the mixed solution is more than or equal to the concentration of the catalyst in the leaching agent.
Preferably, oxygen and carbon dioxide are introduced into the adsorption tail liquid, and the method for taking the obtained mixed liquid as the leaching agent comprises the following steps:
introducing oxygen into the adsorption tail liquid, injecting the obtained oxygen-enriched liquid into an underground ore-bearing aquifer through a liquid injection pipeline, leaching, and detecting the residual oxygen concentration in the leaching liquid;
and when the residual oxygen concentration is more than 5mg/L, introducing carbon dioxide into the adsorption tail liquid, and controlling the pH value of the mixed liquid to be 6.0-7.5, wherein the obtained mixed liquid is used as a leaching agent.
Preferably, the concentration of oxygen in the oxygen-enriched liquid is 200-400 mg/L.
Preferably, the carbon dioxide is introduced in an amount of 200-600 mg/L.
The invention provides a method for improving the reaction rate of neutral in-situ leaching uranium, which enhances the oxidation performance of oxygen through a catalyst in the neutral in-situ leaching uranium, thereby improving the uranium leaching reaction rate, improving the uranium concentration by more than 10%, shortening the uranium leaching reaction process, and avoiding blockage affecting the liquid extraction and injection amount of a well site in the reaction process. According to the invention, oxygen and carbon dioxide are introduced into the adsorption tail liquid, and the obtained mixed liquid is used as a leaching agent, so that the adsorption tail liquid can be reused, and the cycle of the leaching process is realized.
Drawings
FIG. 1 is a process flow diagram for improving the reaction rate of neutral leaching uranium provided by the invention;
fig. 2 is a graph of uranium concentration over time for the leaching process in an example.
Detailed Description
The invention provides a method for improving the reaction rate of neutral in-situ leaching uranium mining, which comprises the following steps:
(1) Injecting a catalyst into a leaching agent for enhanced leaching to obtain uranium-containing leaching solution; the catalyst comprises NaNO 2 One or more of KI and citric acid;
(2) Carrying out ion exchange adsorption treatment on the uranium-containing leaching solution to obtain adsorption tail liquid; and (3) introducing oxygen and carbon dioxide into the adsorption tail liquid, and returning the obtained mixed liquid as a leaching agent to the step (1).
The invention willAnd (3) injecting a catalyst into the leaching agent, and carrying out intensified leaching to obtain uranium-containing leaching liquid. In the present invention, the catalyst comprises NaNO 2 One or more of KI and citric acid, more preferably NaNO 2 And KI or a combination of citric acid and KI. In a specific embodiment of the present invention, the NaNO 2 And NaNO in KI composition 2 And the mass ratio of KI is preferably 1:1. In the invention, the mass ratio of the citric acid to the KI in the composition of the citric acid and the KI is preferably 1:1.
In the invention, the concentration of the catalyst in the leaching agent is preferably 100-600 mg/L, more preferably 200-300 mg/L.
In the present invention, the catalyst is preferably added in the form of a concentrated catalyst solution; controlling the flow rate of the catalyst injected into the leaching agent according to formula I;
c2 =v1×c1/(v1+v2) formula I;
in the formula I, c2 is the concentration of the catalyst in the leaching agent, and the unit is mg/L; v1 is the flow rate of the leaching agent before adding the catalyst, and the unit is L; c1 is the concentration of the catalyst concentrated solution, and the unit is mg/L; v2 is the flow rate of the catalyst into the leaching agent in L. The concentration of the catalyst concentrated solution is not particularly required, and the catalyst can be injected into the liquid injection pipeline.
The method is characterized by detecting the concentration of the catalyst in the mixed solution after the intensified leaching operation is carried out for a period of time; and stopping injecting the catalyst when the concentration of the catalyst in the mixed solution is more than or equal to the concentration of the catalyst in the leaching agent. In the present invention, the period of time is preferably 7 to 10 days. In the present invention, the mixed liquid refers to a mixed liquid obtained by introducing oxygen and carbon dioxide into the adsorption tail liquid.
In the present invention, the method for introducing oxygen and carbon dioxide into the adsorption tail liquid to obtain the mixed liquid as the leaching agent preferably comprises the following steps:
introducing oxygen into the adsorption tail liquid, injecting the obtained oxygen-enriched liquid into an underground ore-bearing aquifer through a liquid injection pipeline, leaching, and detecting the residual oxygen concentration in the leaching liquid;
and when the residual oxygen concentration is more than 5mg/L, introducing carbon dioxide into the adsorption tail liquid, and controlling the pH value of the mixed liquid to be 6.0-7.5, wherein the obtained mixed liquid is used as a leaching agent.
In the invention, the concentration of oxygen in the oxygen-enriched liquid is preferably 200-400 mg/L.
In the invention, the carbon dioxide is preferably introduced in an amount of 200-600 mg/L.
In the present invention, when neutral leaching of uranium is just started, the preparation method of the leaching agent preferably includes: introducing oxygen into the underground water containing hydrogen carbonate, injecting the obtained solution into an underground ore-bearing aquifer through a liquid injection pipeline, leaching, and detecting the residual oxygen concentration in the leaching liquid; and when the residual oxygen concentration is more than 5mg/L, introducing carbon dioxide into the liquid injection pipeline to obtain the leaching agent, and controlling the pH value of the leaching agent to be 6.0-7.5. In the invention, the concentration of bicarbonate in the groundwater containing the bicarbonate is preferably more than or equal to 800mg/L. In the invention, the concentration of oxygen in the solution is preferably 200-400 mg/L. In the invention, the carbon dioxide is preferably introduced in an amount of 200-600 mg/L. In the invention, the pH of the leaching agent is preferably 6.5-7.0.
In the present invention, the ion exchange adsorption treatment preferably employs a strongly basic anion exchange resin to treat the uranium-containing leaching solution. In the present invention, the strongly basic anion exchange resin preferably includes D231YT, D261 or 201×7.
In the invention, saturated resin is preferably obtained after the ion exchange adsorption treatment; the saturated resin is transferred to a rinsing process.
The method provided by the invention can enhance the oxidation performance of the system, obviously improve the oxidation effect of tetravalent uranium in ores, and further improve the uranium leaching reaction rate.
The technical solutions of the present invention will be clearly and completely described in the following in connection with the embodiments of the present invention. It will be apparent that the described embodiments are only some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1
The ore body of certain uranium deposit in inner Mongolia is mainly plate-shaped, the average thickness of the ore body is 6.79m, the average grade is 0.052%, and the average uranium content is 4.93kg/m 2 The average content of carbonate is 2.58%, and a neutral leaching process is suitable for use.
1. Indoor verification test
And taking the core sample of the ore deposit sandstone uranium deposit, crushing the core sample to 0.2-5 mm, uniformly mixing the core sample and carrying out a test for improving the uranium leaching reaction rate by catalysis. Crushing and uniformly mixing, dividing a core sample into three equal parts, adding stratum water of an ore-bearing water-bearing layer of the ore deposit in a liquid-solid ratio of 5:1 (the dosage ratio of stratum water to the core sample is 5mL:1 g), and adopting a three-phase reaction kettle as a reaction container; 3 groups of parallel tests are carried out to judge the effect of the catalyst on improving the uranium reaction rate.
Group 1 test: 400mg/L CO is introduced into the reaction kettle 2 After stirring and reacting for 1h, stopping, and then introducing 250mg/L O into a reaction kettle 2 . Taking liquid samples from 1 day, 3 days, 5 days and 7 days respectively to analyze uranium in the liquid samples; in the process of emptying and sampling the reaction kettle, 400mg/L CO is repeatedly introduced 2 250mg/L O 2 And (3) operating steps.
Group 2 test: adding NaNO into a reaction kettle 2 As a catalyst, the concentration is 100mg/L; 400mg/L CO is introduced 2 After stirring and reacting for 1h, stopping, and then introducing 250mg/L O into a reaction kettle 2 . Taking liquid samples from 1 day, 3 days, 5 days and 7 days respectively to analyze the uranium and the catalyst concentration; in the process of emptying and sampling the reaction kettle, 400mg/L CO is repeatedly introduced 2 250mg/L O 2 The operation steps are carried out without adding catalyst.
Group 3 test: adding NaNO into a reaction kettle 2 As a catalyst, the catalyst concentration was made 200mg/L; 400mg/L CO is introduced 2 After stirring and reacting for 1h, stopping, and then introducing 250mg/L O into a reaction kettle 2 . Taking liquid samples from 1 day, 3 days, 5 days and 7 days respectively to analyze the uranium and the catalyst concentration; in the process of emptying and sampling the reaction kettle, 400mg/L CO is repeatedly introduced 2 250mg/L O 2 The operation steps are carried out without adding catalyst.
Group 4 test: substantially the same as in run 3, except that the catalyst was adjusted to a 1:1 mass ratio of NaNO 2 And KI.
Group 5 test: substantially the same as in the test set 3, except that the catalyst was adjusted to a mass ratio of 1:1 of citric acid to KI.
The enhanced leaching effect of the catalyst is shown in Table 1 and FIG. 2, wherein "no catalyst" in FIG. 2 indicates the test of group 1, "catalyst-200" indicates the test of group 3, and "catalyst-100" indicates the test of group 2.
Table 1 comparison of enhanced leaching effects of catalysts
As can be seen from table 1, in the 5 groups of tests, the uranium concentration in the leachate increases with the increase of the reaction time. Compared with leaching reaction without adding a catalyst, the catalyst can be added to improve the concentration of uranium in the leaching solution and the leaching rate of final uranium. Comparing the tests in the group 5, when the adding amount of the catalyst is 100mg/L, the uranium concentration in the leaching solution after 1 day of reaction is 78.1mg/L and is more than 77.9mg/L when no catalyst is added for 3 days of reaction; when the adding amount of the catalyst is 200mg/L, after leaching reaction is carried out for 1 day, the uranium concentration of the leaching solution is 83.1mg/L, which is higher than the uranium concentration of the leaching solution which is not added with the catalyst and is reacted for 7 days, which is 82.8mg/L. Meanwhile, according to the reaction rate definition, the leaching reaction rate of uranium can be characterized as: the slope of the uranium concentration curve with time, Δv (U) = Δc (U)/. DELTA.t, can characterize the leaching reaction rate of uranium. As can be seen from fig. 2, the addition of the catalyst can effectively increase the uranium leaching reaction rate, and the higher the catalyst concentration, the greater the chemical reaction rate.
As can be seen from comparing the leaching rate of uranium in the test of group 5, the leaching rate of uranium is improved from 49.8% to 68.6% when the catalyst is added to 200mg/L compared with the leaching rate of uranium without the catalyst. Therefore, the catalyst is added, the leaching reaction rate of uranium can be obviously improved, and the intensified leaching of uranium is realized.
2. In-situ implementation verification
Tests of the catalyst to increase the uranium leaching reaction rate were conducted at the test site as shown in figure 1.
Step (1): pre-oxidizing the ore layer. Leaching solution with O 2 Mixing and injecting into underground mineral water-bearing layer through liquid injection pipeline, the flow rate of liquid injection is 1.5m 3 And/h, wherein the oxygen concentration in the mixed solution is 300mg/L; detecting the residual oxygen concentration in the leaching solution in the leaching process;
step (2): after 7 days, the residual oxygen concentration is more than 5mg/L, 400mg/L carbon dioxide gas is added into the leaching solution in the step (1), and the pH value of the solution is 6.5;
step (3): injecting the leaching solution obtained in the step (2) into a stirring tank, and adding NaNO with the mass ratio of 1:1 2 And KI, formulated at a concentration of 20kg/m 3 Injecting the catalyst solution into a liquid injection pipeline by using a metering pump, and controlling the adding concentration of the catalyst to be 300mg/L; detecting the uranium concentration and the catalyst concentration in the leaching solution; the result shows that after 25 days, the uranium concentration is increased from 15.6mg/L to 43.2mg/L and the uranium concentration is in an upward trend;
step (4): introducing the leaching solution obtained in the step (3) into an ion exchange adsorption tower, introducing 300mg/L oxygen and 400mg/L carbon dioxide into the adsorption tail solution treated by the strong-alkaline anion exchange resin 201 multiplied by 7 to prepare a leaching agent, injecting the leaching agent into a liquid injection hole, monitoring the concentration of free catalyst anions in the leaching agent, and stopping adding the catalyst when the concentration reaches 300mg/L; if the concentration of the catalyst anions is reduced, the replenishing is continued to ensure the high efficiency of uranium leaching.
Example 2
The ore bodies of certain uranium deposit in Xinjiang are distributed in a strip shape, the average thickness of the ore bodies is 7.58m, the average grade is 0.061%, and the average uranium content is 5.15kg/m 2 The average content of carbonate is 2.67%, and the neutral leaching technology is suitable for use.
Tests of the catalyst to increase the uranium leaching reaction rate were conducted at the test site as shown in figure 1.
Step (1): pre-oxidizing the ore layer. Leaching solution with O 2 Mixing and injecting into underground mineral water-bearing layer through liquid injection pipeline, the flow rate of liquid injection is 1.8m 3 And/h, wherein the oxygen concentration in the mixed solution is 350mg/L; detecting the residual oxygen concentration in the leaching solution in the leaching process;
step (2): after 7 days, the residual oxygen concentration is more than 5mg/L, 400mg/L carbon dioxide gas is added into the leaching solution in the step (1), and the pH value of the solution is 6.6;
step (3): injecting the leaching solution obtained in the step (2) into a stirring tank, and adding citric acid and KI with the mass ratio of 1:1 to prepare the concentration of 20kg/m 3 Injecting the catalyst solution into a liquid injection pipeline by using a metering pump, and controlling the adding concentration of the catalyst to be 350mg/L; detecting the uranium concentration and the catalyst concentration in the leaching solution; the result shows that the uranium concentration rises from 14.2mg/L to 39.2mg/L after 22 days, and the uranium concentration rises;
step (4): introducing the leaching solution obtained in the step (3) into an ion exchange adsorption tower, introducing 350mg/L oxygen and 400mg/L carbon dioxide into the adsorption tail solution treated by the strong-alkaline anion exchange resin D231YT to prepare a leaching agent, injecting the leaching agent into a liquid injection hole, monitoring the concentration of free catalyst anions in the leaching agent, and stopping adding the catalyst when the concentration reaches 350mg/L; if the concentration of the catalyst anions is reduced, the replenishing is continued to ensure the high efficiency of uranium leaching.
The foregoing is merely a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention, which are intended to be comprehended within the scope of the present invention.
Claims (7)
1. A method for improving the reaction rate of neutral in-situ leaching uranium mining, which is characterized by comprising the following steps:
(1) Injecting a catalyst into a leaching agent for enhanced leaching to obtain uranium-containing leaching solution; the catalyst comprises NaNO 2 One or more of KI and citric acid;
(2) Carrying out ion exchange adsorption treatment on the uranium-containing leaching solution to obtain adsorption tail liquid; and (3) introducing oxygen and carbon dioxide into the adsorption tail liquid, and returning the obtained mixed liquid as a leaching agent to the step (1).
2. The method of claim 1, wherein the concentration of the catalyst in the leaching agent is 100-600 mg/L.
3. The process according to claim 1 or 2, wherein the catalyst is added in the form of a concentrated catalyst solution; controlling the flow rate of the catalyst injected into the leaching agent according to formula I;
c2 =v1×c1/(v1+v2) formula I;
in the formula I, c2 is the concentration of the catalyst in the leaching agent, and the unit is mg/L; v1 is the flow rate of the leaching agent before adding the catalyst, and the unit is L; c1 is the concentration of the catalyst concentrated solution, and the unit is mg/L; v2 is the flow rate of the catalyst into the leaching agent in L.
4. The method of claim 1, wherein the concentration of catalyst in the mixed liquor is detected after a period of time of the enhanced leaching operation; and stopping injecting the catalyst when the concentration of the catalyst in the mixed solution is more than or equal to the concentration of the catalyst in the leaching agent.
5. The method according to claim 1, wherein oxygen and carbon dioxide are introduced into the adsorption tail solution, and the obtained mixed solution is used as a leaching agent, and the method comprises the following steps:
introducing oxygen into the adsorption tail liquid, injecting the obtained oxygen-enriched liquid into an underground ore-bearing aquifer through a liquid injection pipeline, leaching, and detecting the residual oxygen concentration in the leaching liquid;
and when the residual oxygen concentration is more than 5mg/L, introducing carbon dioxide into the adsorption tail liquid, and controlling the pH value of the mixed liquid to be 6.0-7.5, wherein the obtained mixed liquid is used as a leaching agent.
6. The method of claim 5, wherein the concentration of oxygen in the oxygen-enriched liquid is 200-400 mg/L.
7. The method of claim 5, wherein the carbon dioxide is introduced in an amount of 200-600 mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311566442.8A CN117265300A (en) | 2023-11-23 | 2023-11-23 | Method for improving reaction rate of neutral in-situ leaching uranium mining |
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