阅读说明：本技术 一种提高三脂肪胺淋萃提铀流程效益的方法 (Method for improving flow benefit of uranium extraction by triple-fatty amine leaching ) 是由 周志全 曹令华 任燕 牛玉清 张永明 赵凤岐 舒祖骏 曹笑豪 叶开凯 于 2020-09-07 设计创作，主要内容包括：本发明属于铀矿水冶技术领域,具体涉及一种提高三脂肪胺淋萃提铀流程效益的方法,通过工艺溶液循环方法和参数控制方法,提高了三脂肪胺淋萃提铀流程中有机相中铀浓度,降低了硫酸和氨的消耗量,减少了硫酸铵的排放量。通过本方法,可以降低三脂肪胺淋萃提铀流程硫酸消耗量、氨消耗量以及硫酸铵的产生量,提高经济性,并程达到减排效果。(The invention belongs to the technical field of uranium hydrometallurgy of uranium ores, and particularly relates to a method for improving benefits of a process of uranium leaching extraction by using tri-aliphatic amine. By the method, the sulfuric acid consumption, the ammonia consumption and the ammonium sulfate generation amount in the uranium leaching process of the tri-aliphatic amine can be reduced, the economy is improved, and the emission reduction effect is achieved.)

1. A method for improving flow benefit of uranium extraction by triple fatty amine leaching is characterized by comprising the following steps:

step 1, leaching broken and ground ore by adopting sulfuric acid, setting acid consumption as Q and unit as kg/t ore, leaching in situ to obtain uranium with unit as kg/kg, and leaching liquor with uranium concentration as C₁In units of g/L, the sulfuric acid concentration is C_H1The unit is g/L, 1t ore, or 1kg uranium in the leaching liquid leached in situ, and the volume of the leaching liquid is V₁The unit is L;

step 2, adsorbing the leaching solution by using strong basic resin to obtain saturated resin, wherein the volume of the adsorption tail solution is V₂The unit is L, and then high-concentration sulfuric acid is adopted for leaching, and the concentration of the sulfuric acid is C_HF3In units of g/L, C_HF3Not less than 80 g/L; obtaining leached qualified liquid with the uranium concentration of C₃In units of g/L, the sulfuric acid concentration is C_H2In g/L, the volume of the leaching solution is V₂The unit is L;

step 3, setting the volume as V_2-2The unit is L, the absorption tail liquid and the eluted qualified liquid are mixed, the extraction stock solution is adjusted, and the uranium concentration of the adjusted extraction stock solution is C₄In units of g/L, the sulfuric acid concentration is C_H4In g/L, the volume of the leaching solution is V₄Diluting the uranium concentration in the leached qualified liquid by the adsorption tail liquid with the unit of L, wherein the dilution multiple is DR;

dilution factor DR ═ V₄/V₃＝(V_2-2+V₃)/V₃＝V_2-2/V₃+1；

Step 4, carrying out multi-stage countercurrent extraction on the adjusted extraction stock solution by using tri-aliphatic amine to obtain a saturated organic phase with the uranium concentration of C_OIn units of g/L, the sulfuric acid concentration is C_HOThe unit is g/L, and the volume of the loaded organic phase is V_OThe unit is L, stripping is removed;

step 5, the uranium concentration of the raffinate obtained by the multi-stage countercurrent extraction is C₅In units of g/L, the sulfuric acid concentration is C_H5In g/L, the volume of the leaching solution is V₅In the unit of L, wherein V_5-1Unit is L, return eluent preparation, V_5-2The unit is L, and the leaching agent is returned for preparation;

step 6, the preparation of the back extractant meets the following conditions, and the sulfuric acid is supplemented in the preparation process to ensure that the concentration of the sulfuric acid reaches C_HF1；V_5-2Need to satisfy V_2-2≤V_5-2The conditions of (a);

step 7, carrying out multi-stage counter-current back extraction on the loaded organic phase, wherein the back extraction agents are ammonium sulfate and ammonia, and controlling the pH of each stage to be 3.8-5 to obtain a back extraction liquid;

step 8, adding ammonia into the back extraction liquid to precipitate ADU, and performing solid-liquid separation to obtain a product ADU and a mother liquid, wherein the mother liquid contains ammonium sulfate and the volume of the mother liquid is V₇In the unit of L, wherein V_7-1In the unit L, as stripping agent back to trans, V_7-2The unit is L, and the waste liquid is discharged and treated;

step (ii) of9 when C is present_H5×V₅When the Q value is more than or equal to 1000Q,

it should satisfy:

or

Wherein zeta is 1-1.2;

wherein C is_H5 ^*When DR is 1, i.e. V_2-20 or V_2-BC when equal to 0_H5；

Step 10, when C_H5×V₅When the frequency is less than 1000Q,

it should satisfy:

2. the method for improving the efficiency of the uranium leaching process of the tri-aliphatic amine according to claim 1, wherein the method comprises the following steps: in the step 1, the broken and ground ore is leached in situ by adopting sulfuric acid.

3. The method for improving the efficiency of the uranium leaching process of the tri-aliphatic amine according to claim 1, wherein the method comprises the following steps: in the step 3, DR is 1.2-4.

4. The method for improving the efficiency of the uranium leaching process of the tri-aliphatic amine according to claim 1, wherein the method comprises the following steps: in said step 3, DR >1 is controlled.

5. The method for improving the efficiency of the uranium leaching process of the tri-aliphatic amine according to claim 1, wherein the method comprises the following steps: in said step 3, V_2-2>0。

6. The method for improving the efficiency of the uranium leaching process of the tri-aliphatic amine according to claim 1, wherein the method comprises the following steps: and in the step 3, water is distributed through a public pool, so that the water balance and DR >1 are realized.

7. The method for improving the efficiency of the uranium leaching process of the tri-aliphatic amine according to claim 1, wherein the method comprises the following steps: in step 9, ζ was 1.08.

Technical Field

The invention belongs to the technical field of uranium ore hydrometallurgy, and particularly relates to a method for improving flow benefit of uranium extraction by triple aliphatic amine leaching.

Background

Ion exchange and solvent extraction are the main methods for extracting uranium from a uranium leach solution, and both have application characteristics. In one aspect, the ion exchange method is more suitable for systems with lower uranium concentrations, and the solvent extraction method is more suitable for systems with higher uranium concentrations. For leachate with lower uranium concentration, an ion exchange adsorption-leaching-solvent extraction method, namely a leaching extraction process, can be adopted to carry out ion exchange adsorption on uranium from a system with lower uranium concentration to obtain leached qualified liquid with higher concentration, and then solvent extraction is carried out. The method conforms to the adaptation characteristics of ion exchange and solvent extraction to high and low uranium concentrations on one hand, and on the other hand, the problem of conversion from a sodium system to an ammonium system of a solution system after single ion exchange is solved, and uranium ammonium salt is prepared after solvent extraction so as to prepare uranium oxide.

In the leaching and extraction process, high-concentration sulfuric acid is generally adopted to leach the loaded resin to obtain leached qualified liquid, the uranium in the leached qualified liquid is extracted, and then back extraction is performed to obtain back extraction liquid, so that a uranium product is prepared. The extractant is generally acidic cation extractant, such as D2EHPA, and can also be hydrogen ion association type weakly alkaline tri-fatty amine extractant, such as N235.

The uranium-loaded tri-aliphatic amine organic phase can be subjected to sodium carbonate back extraction, ammonium carbonate back extraction or ammonium sulfate back extraction. Compared with other back extraction methods, the ammonium sulfate back extraction method has low cost, is beneficial to preparing the ammonium salt product of uranium, is the main back extraction method at present, and adopts a multistage countercurrent process, takes ammonium sulfate and ammonia water as back extraction agents, generates the ammonium sulfate through the reaction of the ammonia and sulfuric acid in an organic phase under a proper pH condition, realizes the deprotonation process of the organic phase, and loses the extraction capacity, thereby achieving the purpose of back extraction of uranium.

The tri-fatty amine extractant has the advantages of good uranium selectivity, and the tri-fatty amine extractant has the defects that (1) the extraction capacity is seriously influenced by acidity, and the extraction capacity is lower under the condition of high-concentration sulfuric acid. The disadvantage (2) is that it can extract a large amount of sulphuric acid when extracting uranium, and then the sulphuric acid and ammonia water are subjected to acid-base reaction when back extracting to generate ammonium sulfate which needs to be disposed. The problems of low uranium concentration, high sulfuric acid consumption, high ammonia consumption, high ammonium sulfate generation amount and treatment need are the problems of the existing triple-fatty amine leaching process, and the method aims at solving or improving the problem and improving the economic benefit.

Disclosure of Invention

In view of the above disadvantages, the main object of the present invention is to provide a method for improving the benefit of a uranium leaching process with tri-aliphatic amine, which can reduce the consumption of sulfuric acid, the consumption of ammonia, and the generation of ammonium sulfate in the uranium leaching process with tri-aliphatic amine, improve the economy, and achieve the effect of emission reduction.

The technical scheme of the invention is as follows:

a method for improving flow benefit of uranium extraction by leaching tri-aliphatic amine comprises the step 1 of leaching crushed ore by sulfuric acid, setting acid consumption as Q and unit as kg/t ore, leaching in situ by taking unit as kg/kg uranium, and obtaining leachate with uranium concentration as C₁In units of g/L, the sulfuric acid concentration is C_H1The unit is g/L, 1t ore, or 1kg uranium in the leaching liquid leached in situ, and the volume of the leaching liquid is V₁The unit is L;

step 2, adsorbing the leaching solution by using strong basic resin to obtain saturated resin, wherein the volume of the adsorption tail solution is V₂The unit is L, and then high-concentration sulfuric acid is adopted for leaching, and the concentration of the sulfuric acid is C_HF3In units of g/L, C_HF3Not less than 80 g/L; obtaining leached qualified liquid with the uranium concentration of C₃In units of g/L, the sulfuric acid concentration is C_H2In g/L, the volume of the leaching solution is V₂The unit is L;

step 3, setting the volume as V_2-2The unit is L, the absorption tail liquid and the qualified leaching liquid are mixed, and the extraction stock solution is adjusted and adjustedThe uranium concentration of the later extraction stock solution is C₄In units of g/L, the sulfuric acid concentration is C_H4In g/L, the volume of the leaching solution is V₄Diluting the uranium concentration in the leached qualified liquid by the adsorption tail liquid with the unit of L, wherein the dilution multiple is DR;

dilution factor DR ═ V₄/V₃＝(V_2-2+V₃)/V₃＝V_2-2/V₃+1；

Step 4, carrying out multi-stage countercurrent extraction on the adjusted extraction stock solution by using tri-aliphatic amine to obtain a saturated organic phase with the uranium concentration of C_OIn units of g/L, the sulfuric acid concentration is C_HOThe unit is g/L, and the volume of the loaded organic phase is V_OThe unit is L, stripping is removed;

step 5, the uranium concentration of the raffinate obtained by the multi-stage countercurrent extraction is C₅In units of g/L, the sulfuric acid concentration is C_H5In g/L, the volume of the leaching solution is V₅In the unit of L, wherein V_5-1Unit is L, return eluent preparation, V_5-2The unit is L, and the leaching agent is returned for preparation;

step 6, the preparation of the back extractant meets the following conditions, and the sulfuric acid is supplemented in the preparation process to ensure that the concentration of the sulfuric acid reaches C_HF1；V_5-2Need to satisfy V_2-2≤V_5-2The conditions of (a);

step 7, carrying out multi-stage counter-current back extraction on the loaded organic phase, wherein the back extraction agents are ammonium sulfate and ammonia, and controlling the pH of each stage to be 3.8-5 to obtain a back extraction liquid;

step 8, adding ammonia into the back extraction liquid to precipitate ADU, and performing solid-liquid separation to obtain a product ADU and a mother liquid, wherein the mother liquid contains ammonium sulfate and the volume of the mother liquid is V₇In the unit of L, wherein V_7-1In the unit L, as stripping agent back to trans, V_7-2The unit is L, and the waste liquid is discharged and treated;

step 9, when C_H5×V₅When the Q value is more than or equal to 1000Q,

it should satisfy:

or

Wherein zeta is 1-1.2;

wherein C is_H5 ^*When DR is 1, i.e. V_2-20 or V_2-BC when equal to 0_H5；

Step 10, when C_H5×V₅When the frequency is less than 1000Q,

it should satisfy:

in the step 1, the broken and ground ore is leached in situ by adopting sulfuric acid.

In the step 3, DR is 1.2-4.

In said step 3, DR >1 is controlled.

In said step 3, V_2-2>0。

And in the step 3, water is distributed through a public pool, so that the water balance and DR >1 are realized.

In step 9, ζ was 1.08.

The invention has the beneficial effects that:

(1) when DR is more than 1, the qualified leaching solution is doped with other solutions, but the selectivity of the tri-fatty ammonium is good, so that the product quality is not obviously reduced compared with that when DR is 1, and an ADU product with equivalent quality can still be obtained.

(2) After DR is increased (DR is more than or equal to 1), the uranium concentration in the extracted organic phase is obviously increased, and the acid concentration is reduced. The organic phase treatment capacity is reduced, and the production pressure of the back extraction equipment is reduced.

(3)DR>1 and selecting proper parameters, the consumption of the sulfuric acid is 1-7 t/t less than that of the sulfuric acid with DR equal to 1, and ammonia (100% NH)₃Measured) consumption is 1-5 t/t less than that when DR is 1, and the amount of waste ammonium sulfate generated is 2-10 t/t less than that when DR is 1. The benefit is obvious, and the specific data are changed according to system parameters.

(4) When the parameter flow with DR >1 is adopted, the reconstruction and operation cost is not obviously increased compared with DR equal to 1.

Drawings

Fig. 1 is a flow chart 1 of a method for improving flow benefit of uranium leaching by using tri-aliphatic amine according to the present invention.

Fig. 2 is a flow chart of a method for improving the flow benefit of the uranium leaching process of tri-aliphatic amine according to the present invention 2.

In the figure: c_{Number of}Denotes the uranium concentration, C_{H number}Denotes the sulfuric acid concentration, V_{Number of}Denotes volume, C_ODenotes the concentration of uranium, C, in the organic phase_HODenotes the concentration of sulfuric acid in the organic phase, V_OIndicating the volume of the organic phase.

Detailed Description

The invention is described in further detail below with reference to the figures and the embodiments.

Example 1:

a method for improving flow benefit of uranium extraction by leaching tri-aliphatic amine comprises the step 1 of leaching crushed ore by sulfuric acid, setting acid consumption as Q and unit as kg/t ore, leaching in situ by taking unit as kg/kg uranium, and obtaining leachate with uranium concentration as C₁In units of g/L, the sulfuric acid concentration is C_H1The unit is g/L, 1t ore, or 1kg uranium in the leaching liquid leached in situ, and the volume of the leaching liquid is V₁The unit is L;

step 2, adsorbing the leaching solution by using strong basic resin to obtain saturated resin, wherein the volume of the adsorption tail solution is V₂The unit is L, and then high-concentration sulfuric acid is adopted for leaching, and the concentration of the sulfuric acid is C_HF3In units of g/L, C_HF3Not less than 80 g/L; obtaining leached qualified liquid with the uranium concentration of C₃In units of g/L, the sulfuric acid concentration is C_H2In g/L, the volume of the leaching solution is V₂The unit is L;

step 3, setting the volume as V_2-2The unit is L, the absorption tail liquid and the eluted qualified liquid are mixed, the extraction stock solution is adjusted, and the uranium concentration of the adjusted extraction stock solution is C₄In units of g/L, the sulfuric acid concentration is C_H4In g/L, the volume of the leaching solution is V₄Unit ofL, diluting the uranium concentration in the qualified leaching solution by using the tail absorption solution, wherein the dilution multiple is DR;

dilution factor DR ═ V₄/V₃＝(V_2-2+V₃)/V₃＝V_2-2/V₃+1；

Step 4, carrying out multi-stage countercurrent extraction on the adjusted extraction stock solution by using tri-aliphatic amine to obtain a saturated organic phase with the uranium concentration of C_OIn units of g/L, the sulfuric acid concentration is C_HOThe unit is g/L, and the volume of the loaded organic phase is V_OThe unit is L, stripping is removed;

step 5, the uranium concentration of the raffinate obtained by the multi-stage countercurrent extraction is C₅In units of g/L, the sulfuric acid concentration is C_H5In g/L, the volume of the leaching solution is V₅In the unit of L, wherein V_5-1Unit is L, return eluent preparation, V_5-2The unit is L, and the leaching agent is returned for preparation;

step 6, the preparation of the back extractant meets the following conditions, and the sulfuric acid is supplemented in the preparation process to ensure that the concentration of the sulfuric acid reaches C_HF1；V_5-2Need to satisfy V_2-2≤V_5-2The conditions of (a);

step 7, carrying out multi-stage counter-current back extraction on the loaded organic phase, wherein the back extraction agents are ammonium sulfate and ammonia, and controlling the pH of each stage to be 3.8-5 to obtain a back extraction liquid;

step 8, adding ammonia into the back extraction liquid to precipitate ADU, and performing solid-liquid separation to obtain a product ADU and a mother liquid, wherein the mother liquid contains ammonium sulfate and the volume of the mother liquid is V₇In the unit of L, wherein V_7-1In the unit L, as stripping agent back to trans, V_7-2The unit is L, and the waste liquid is discharged and treated;

step 9, when C_H5×V₅When the Q value is more than or equal to 1000Q,

it should satisfy:

or

Wherein zeta is 1-1.2;

wherein C is_H5 ^*When DR is 1, i.e. V_2-20 or V_2-BC when equal to 0_H5；

Step 10, when C_H5×V₅When the frequency is less than 1000Q,

it should satisfy:

in the step 1, the broken and ground ore is leached in situ by adopting sulfuric acid.

In the step 3, DR is 1.2-4.

In said step 3, DR >1 is controlled.

In said step 3, V_2-2>0。

And in the step 3, water is distributed through a public pool, so that the water balance and DR >1 are realized.

In step 9, ζ was 1.08.

Example 2:

the uranium grade of a uranium ore is 0.117 percent, and the uranium ore is stirred and leached by adopting conventional sulfuric acid. The acid consumption was 30kg/t ore. The solid ratio of the leaching solution is 2L/kg. Uranium in the leachate is adsorbed by adopting a density of 201 multiplied by 7, and 50mg/ml of saturated resin is obtained. And leaching the saturated resin by using 100g/L sulfuric acid, wherein the volume of the leaching solution is 25BV, the uranium concentration of the leached qualified solution is 2.02g/L, and the sulfuric acid concentration is 99.2 g/L.

When DR is 1, N235 organic phase relative leaching qualified liquid is used for extraction, the saturated uranium concentration is 1.95g/L, 54.3% of extraction residue is returned to be leached (the volume accounts for 13.8% of the leaching agent, the extraction return sulfuric acid is 25kg/t ore), and 45.7% is returned to be eluted with the eluent for preparation (the volume accounts for 45.7% of the eluent, and the sulfuric acid accounts for 41.6% of the eluent). And (3) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 5.85g/L, adding ammonia to precipitate ADU, returning a mother liquid to the back extraction preparation, treating and discharging part of the mother liquid, wherein the discharge amount of ammonium sulfate is 6.2t/t uranium.

When DR is 2, diluting and leaching with adsorption tail liquidAnd extracting the liquid by adopting N235 organic phase-to-leached qualified liquid to obtain saturated uranium with the concentration of 3g/L, wherein the raffinate is 51.6 percent returned to be leached (the volume accounts for 26.5 percent of the leaching agent, and the extracted returned sulfuric acid is 25kg/t ore), and 48.4 percent returned to be prepared by the leaching agent (the volume accounts for 96.8 percent of the leaching agent, and the sulfuric acid accounts for 45.7 percent of the leaching agent). And (2) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 6g/L, adding ammonia for precipitation to prepare ADU with the same quality, returning a mother solution for back extraction preparation, treating and discharging part of the mother solution, and discharging the ammonium sulfate with the discharge amount of 3.85t/t uranium. Saving 1.76t/t uranium sulfate and saving ammonia (by 100% NH) when DR is 2 to 1₃Metering) 1.22t/t uranium, less discharging 2.37t/t uranium ammonium sulfate and 38 percent of emission reduction rate.

Example 3:

the uranium grade of a uranium ore is 0.117 percent, and the uranium ore is stirred and leached by adopting conventional sulfuric acid. The acid consumption was 30kg/t ore. The solid ratio of the leaching solution is 2L/kg. Uranium in the leachate is adsorbed by adopting a density of 201 multiplied by 7, and 50mg/ml of saturated resin is obtained. And leaching the saturated resin by using 100g/L sulfuric acid, wherein the volume of the leaching solution is 25BV, the uranium concentration of the leached qualified solution is 2.04g/L, and the sulfuric acid concentration is 99.2 g/L.

When DR is 1, N235 organic phase relative leaching qualified liquid is used for extraction, the saturated uranium concentration is 1.95g/L, 21.9% of raffinate is returned to leaching (the volume accounts for 5.5% of the leaching agent, and the extraction return sulfuric acid is 10kg/t ore), and 78.1% is returned to leaching agent preparation (the volume accounts for 78.1% of the leaching agent, and the sulfuric acid accounts for 70.9% of the leaching agent). And (3) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 5.85g/L, adding ammonia to precipitate ADU, returning a mother liquid to the back extraction preparation, treating and discharging part of the mother liquid, wherein the discharge amount of ammonium sulfate is 6.2t/t uranium.

When ζ is 1.08, the DR maximum is calculated to be 2.53, and DR is taken to be 2.53. Diluting the qualified leaching solution with water in a public water tank, extracting the qualified leaching solution by adopting N235 organic phase to obtain saturated uranium with the concentration of 3.5g/L, returning and leaching 60.5% of raffinate (the volume accounts for 39.8% of the leaching agent, and the extraction return sulfuric acid accounts for 30kg/t ore), and preparing 39.5% of return eluent (the volume accounts for 99.9% of the eluent, and the sulfuric acid accounts for 37.7% of the eluent). Carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid6.3g/L, adding ammonia for precipitation to prepare ADU with the same quality, returning the mother liquor to back extraction preparation, treating and discharging part of the mother liquor, and discharging 3.22t/t of uranium by ammonium sulfate discharge amount. 2.23t/t uranium sulfate and ammonia (100% NH) can be saved when DR is 2.53 and DR is 1₃Calculated) 1.54t/t uranium, less discharge of 3.00t/t uranium ammonium sulfate and 48 percent of emission reduction rate.

Example 4:

the uranium grade of a uranium ore is 0.117%, and heap leaching is carried out by adopting sulfuric acid. The acid consumption was 30kg/t ore. The solid ratio of the leaching solution is 2L/kg. Uranium in the leachate is adsorbed by adopting a density of 201 multiplied by 7, and 50mg/ml of saturated resin is obtained. And leaching the saturated resin by using 100g/L sulfuric acid, wherein the volume of the leaching solution is 5BV, the uranium concentration of the leached qualified solution is 5.05g/L, and the sulfuric acid concentration is 97.94 g/L.

When DR is 1, N235 organic phase relative leaching qualified liquid is used for extraction, the saturated uranium concentration is 1.95g/L, the extraction residue is 6.06% returned to be leached (the volume accounts for 0.6% of the leaching agent, the extraction returned sulfuric acid is 1kg/t ore), and 93.9% returned to be leached to be prepared (the volume accounts for 93.9% of the leaching agent, and the sulfuric acid accounts for 77.5% of the leaching agent). And (3) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 7g/L, adding ammonia to precipitate ADU, returning a mother solution to the back extraction preparation, treating and discharging part of the mother solution, wherein the discharge amount of ammonium sulfate is 4.72t/t uranium.

When the value of zeta is 1.08, the maximum value of DR is calculated to be 11, and DR is taken to be 9. Diluting the qualified leaching solution with water in a public water tank, extracting the qualified leaching solution by adopting N235 organic phase to obtain saturated uranium with the concentration of 3.6g/L, returning and leaching 97.1% of raffinate (the volume accounts for 95.8% of the leaching agent, and the extraction return sulfuric acid is 19kg/t ore), and preparing 2.9% of return eluent (the volume accounts for 26.0% of the eluent, and the sulfuric acid accounts for 2.6% of the eluent). And (2) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 6.48g/L, adding ammonia for precipitation to prepare ADU with the same quality, returning a mother solution for back extraction preparation, treating and discharging part of the mother solution, and discharging the ammonium sulfate with the discharge amount of 3.11t/t uranium. The method saves 1.20t/t uranium sulfate and ammonia (100% NH) when DR is 9 to 1₃Calculated) 0.83t/t uranium, less discharge of 1.61t/t uranium ammonium sulfate and 34 percent of emission reduction rate.

Example 5:

some sulphuric acid process leach in situ. The acid consumption is 80t/t uranium. The uranium concentration of the leachate is 0.02 g/L. The uranium in the leachate was adsorbed by using a method of 201X 7 to obtain a saturated resin of 10 mg/ml. And (3) leaching the saturated resin by using 103g/L sulfuric acid, wherein the volume of the leaching solution is 10BV, the uranium concentration of the leached qualified solution is 1.04g/L, and the sulfuric acid concentration is 102 g/L.

When DR is 1, N235 organic phase relative leaching qualified liquid is used for extraction, the saturated uranium concentration is 1.45g/L, the extraction residue is 10.3% and returned to be leached (the volume accounts for 0.2% of the leaching agent, and the sulfuric acid accounts for 12.5% of the leaching agent), and 89.7% and returned to be the eluent preparation (the volume accounts for 89.7% of the eluent, and the sulfuric acid accounts for 84.2% of the eluent). And (3) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 4.35g/L, adding ammonia to precipitate ADU, returning a mother liquid to the back extraction preparation, treating and discharging part of the mother liquid, wherein the discharge amount of ammonium sulfate is 8.55t/t uranium.

When ζ is 1.08, the DR maximum is calculated to be 50.74, and DR is taken to be 2. Diluting the qualified leaching solution by using the tail adsorption solution, extracting by using N235 organic phase relative qualified leaching solution to obtain saturated uranium with the concentration of 2.05g/L, returning and leaching the extraction residue by 57.2% (the volume of the extraction residue is 2.4% of the leaching agent, and the sulfuric acid is 75% of the leaching agent), and preparing the 42.8% return eluting solution (the volume of the extraction residue is 85.6% of the eluting solution, and the sulfuric acid is 41.1% of the eluting solution). And (2) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 6.15g/L, adding ammonia for precipitation to prepare ADU with the same quality, returning mother liquor for back extraction preparation, treating and discharging part of the mother liquor, and discharging 5.88t/t uranium ammonium sulfate. When DR is 2 to 1, the method saves 1.97t/t uranium sulfate and ammonia (100% NH)₃Calculated) 1.38t/t uranium, less discharge of 2.66t/t uranium ammonium sulfate and 31 percent of emission reduction rate.

Example 6:

some sulphuric acid process leach in situ. The acid consumption is 80t/t uranium. The uranium concentration of the leachate is 0.02 g/L. The uranium in the leachate was adsorbed by using a method of 201X 7 to obtain a saturated resin of 10 mg/ml. And leaching the saturated resin by using 123g/L sulfuric acid, wherein the volume of the leaching solution is 10BV, the uranium concentration of the leached qualified solution is 1.05g/L, and the sulfuric acid concentration is 122.6 g/L.

When DR is 1, N235 organic phase relative leaching qualified liquid is used for extraction, the saturated uranium concentration is 0.95g/L, the extraction residue is 8.8% and returned to be leached (the volume accounts for 0.18% of the leaching agent, and the sulfuric acid accounts for 12.5% of the leaching agent), and 91.2% and returned to be eluted with the eluent for preparation (the volume accounts for 91.2% of the eluent, and the sulfuric acid accounts for 83.9% of the eluent). And (3) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 5.7g/L, adding ammonia to precipitate ADU, returning a mother liquid to the back extraction preparation, treating and discharging part of the mother liquid, wherein the discharge amount of ammonium sulfate is 13.3t/t uranium.

When ζ is 1.08, the DR maximum is calculated to be 50.78, and DR is taken to be 2.5. Diluting the qualified leaching solution by using adsorption tail solution, extracting by using N235 organic phase relative qualified leaching solution to obtain saturated uranium with the concentration of 2.83g/L, returning and leaching the extraction residue of 61.5% (the volume of the extraction residue is 3.3% of the leaching agent, and the sulfuric acid is 100% of the leaching agent), and preparing the 38.5% returned leaching agent (the volume of the extraction residue is 96.3% of the leaching agent, and the sulfuric acid is 37.6% of the leaching agent). And (2) carrying out back extraction on the saturated organic phase by adopting ammonia water and ammonium sulfate to obtain a back extraction liquid with the uranium concentration of 5.66g/L, adding ammonia for precipitation to prepare ADU with the same quality, returning a mother solution for back extraction preparation, treating and discharging part of the mother solution, and discharging the ammonium sulfate at a discharge amount of 4.10t/t uranium. Saving 6.85t/t uranium sulfate and saving ammonia (by 100% NH) when DR is 2.5 to 1₃Calculated) 4.76t/t uranium, less discharge of 9.23t/t uranium ammonium sulfate and 69 percent emission reduction.