CN106517253A - Technology of recycling sodium nitrate by leaching nitratine fine ore - Google Patents
Technology of recycling sodium nitrate by leaching nitratine fine ore Download PDFInfo
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- CN106517253A CN106517253A CN201611086760.4A CN201611086760A CN106517253A CN 106517253 A CN106517253 A CN 106517253A CN 201611086760 A CN201611086760 A CN 201611086760A CN 106517253 A CN106517253 A CN 106517253A
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- Prior art keywords
- leaching
- sodium nitrate
- fine ore
- nitratine
- heat exchange
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D9/00—Nitrates of sodium, potassium or alkali metals in general
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- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Agronomy & Crop Science (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a technology of recycling sodium nitrate by leaching nitratine fine ore. The technology comprises the following steps: leaching and dissolving fine ore in which the nitratine particle size is less than 5mm in water or light brine-circulating brine mixed liquid by use of a multi-stage continuous parallel-flow jacket heat exchange type suspension device, wherein the continuous leaching stage number of the parallel-flow jacket heat exchange type suspension device is 1-20, the leaching temperature is 20-60 DEG C, and the leaching time of each stage is 0.1-1h; and performing solid-liquid separation to obtain a sodium nitrate-containing nitrate brine solution and tailings, wherein one part of the nitrate brine solution is evaporated to obtain sodium nitrate, and the other part serves as circulating brine to participate in next cycle of nitratine fine ore leaching. The technology of recycling sodium nitrate by leaching nitratine fine ore, disclosed by the invention, can increase the sodium nitrate recovery rate of nitratine and has the characteristics of strong raw material adaptability, continuous operation, low cost, low energy consumption, low sodium nitrate content of tailings and the like.
Description
Technical field
The invention belongs to mine technical field of inorganic, particularly a kind of cubric niter fine ore leaching recovery sodium nitrate work
Skill.
Background technology
Known saliter stone ore is (typically containing NaNO3Fine ore of the substantial amounts of particle diameter less than 5mm is produced after 3-35%) crushing
(typically containing NaNO31-30%), due to very difficult with slag dehydration after great Chi leaching processes, take in actual production directly
Store up and abandon, therefore, cause the serious problems such as increase saliter stone ore and a large amount of wastes of production cost, resource.
The content of the invention
It is an object of the invention to provide sodium nitrate technique is reclaimed in a kind of cubric niter fine ore leaching, which can improve cubric niter
The sodium nitrate response rate, with adaptability to raw material it is strong, operation is continuous, cost and energy consumption is low, tailings low feature containing sodium nitrate.
For achieving the above object, the present invention takes technical scheme below：
Sodium nitrate technique is reclaimed in a kind of cubric niter fine ore leaching, utilizes many cascades with water or light halogen and circulation salt mixed liquor
Fine ore of the continuous cocurrent jacket heat exchange type suspension device leaching dissolving cubric niter particle diameter less than 5mm, cocurrent jacket heat exchange type suspension device connect
Continuous leaching series is 1-20 levels, and leaching temperature is 20-60 DEG C, leaching time 0.1-1 hours at different levels；Obtain containing nitre after solid-liquid separation
The nitre halogen solution of sour sodium and mine tailing, nitre halogen solution part evaporation sodium nitrate processed, under another part is participated in as circulation salt
One circulation leaching cubric niter fine ore.
Further, the fine ore contains NaNO31-30%, NaCl 15-25%, Na2SO44-7%.
Further, in the nitre halogen solution, each component content is NaNO3 10-600g/l、NaCl 300-30g/l、
Na2SO4 10-150g/l。
Further, the tailings contains NaNO30.5-1.0%, H2O 10-30%.
Further, Ore alternative can also be other soluble inorganic salt systems.
The invention has the beneficial effects as follows：Sodium nitrate technique is reclaimed in cubric niter fine ore leaching of the present invention, and which can improve saliter
The sodium nitrate response rate of stone, with adaptability to raw material it is strong, operation is continuous, cost and energy consumption is low, tailings low feature containing sodium nitrate.
Specific embodiment
Embodiment 1：Cubric niter particle diameter is taken less than 5mm fine ores (containing NaNO33%) 200 tons, with 60 tons of water and 340m3/ h is followed
Ring salt carries out continuous cocurrent jacket heat exchange type suspension device leaching, and suspension subsequent leaching series is 5 grades, and leaching temperature is 50 DEG C,
Leaching times at different levels are 0.2 hour, and the 400m containing compositions such as sodium nitrates is obtained after solid-liquid separation3/ h nitre halogen solution and mine tailing,
Nitre halogen solution component (NaNO3 100g/l、NaCl 230g/l、Na2SO460g/l), 38m3/ h nitre halogen solution is for evaporation production nitre
Sour sodium, 340m3/ h nitre halogen solution participates in the continuous cocurrent jacket heat exchange type suspension device of 5 grades of subsequent cycle as circulation salt and leaches sodium
Sal Nitri fine ore；218 tons of tailings (contain NaNO30.5%th, H2O is 10%).
Embodiment 2：Cubric niter particle diameter is taken less than 5mm fine ores (containing NaNO32%) 200 tons, with 40 tons of water and 360m3/ h is followed
Ring salt carries out continuous cocurrent jacket heat exchange type suspension device leaching, and suspension subsequent leaching series is 5 grades, and leaching temperature is 55 DEG C,
Leaching times at different levels are 0.3 hour, and the 400m containing compositions such as sodium nitrates is obtained after solid-liquid separation3/ h nitre halogen solution and mine tailing,
Nitre halogen solution component (NaNO3 100g/l、NaCl 230g/l、Na2SO460g/l), 18m3/ h nitre halogen solution is for evaporation production nitre
Sour sodium, 360m3/ h nitre halogen solution participates in the continuous cocurrent jacket heat exchange type suspension device of 5 grades of subsequent cycle as circulation salt and leaches sodium
Sal Nitri fine ore；218 tons of tailings (contain NaNO30.5%th, H2O is 10%).
Embodiment 3：Cubric niter particle diameter is taken less than 5mm fine ores (containing NaNO36%) 200 tons, with 120 tons of water and 280m3/ h is followed
Ring salt carries out continuous cocurrent jacket heat exchange type suspension device leaching, and suspension subsequent leaching series is 5 grades, and leaching temperature is 60 DEG C,
Leaching times at different levels are 0.5 hour, and the 400m containing compositions such as sodium nitrates is obtained after solid-liquid separation3/ h nitre halogen solution and mine tailing,
Nitre halogen solution component (NaNO3 100g/l、NaCl 230g/l、Na2SO460g/l), 87m3/ h nitre halogen solution is for evaporation production nitre
Sour sodium, 280m3/ h nitre halogen solution participates in the continuous cocurrent jacket heat exchange type suspension device of 5 grades of subsequent cycle as circulation salt and leaches sodium
Sal Nitri fine ore；221 tons of tailings (contain NaNO30.5%th, H2O is 15%).
Embodiment 4：Cubric niter particle diameter is taken less than 5mm fine ores (containing NaNO33%) 200 tons, use 60m3Light halogen (NaNO3
20g/l、NaCl 230g/l、Na2SO460g/l) and 340m3/ h circulation salt carries out continuous cocurrent jacket heat exchange type suspension device leaching
Take, suspension subsequent leaching series is 8 grades, leaching temperature is 40 DEG C, and leaching times at different levels are 0.2 hour, is obtained after solid-liquid separation
400m containing compositions such as sodium nitrates3/ h nitre halogen solution and mine tailing, nitre halogen solution component (NaNO3 120g/l、NaCl 215g/l、
Na2SO455g/l), 38m3/ h nitre halogen solution is for evaporation production sodium nitrate, 340m3Under/h nitre halogen solution is participated in as circulation salt
The one continuous cocurrent jacket heat exchange type suspension device of 8 grades of circulation leaches cubric niter fine ore；218 tons of tailings (contain NaNO30.5%th, H2O
10%).
Embodiment 5：Cubric niter particle diameter is taken less than 5mm fine ores (containing NaNO32%) 200 tons, use 40m3Light halogen (NaNO3
20g/l、NaCl 230g/l、Na2SO460g/l) and 360m3/ h circulation salt carries out continuous cocurrent jacket heat exchange type suspension device leaching
Take, suspension subsequent leaching series is 10 grades, leaching temperature is 35 DEG C, and leaching times at different levels are 0.3 hour, is obtained after solid-liquid separation
400m containing compositions such as sodium nitrates3/ h nitre halogen solution and mine tailing, nitre halogen solution component (NaNO3 120g/l、NaCl 215g/l、
Na2SO455g/l), 18m3/ h nitre halogen solution is for evaporation production sodium nitrate, 360m3Under/h nitre halogen solution is participated in as circulation salt
The one continuous cocurrent jacket heat exchange type suspension device of 10 grades of circulation leaches cubric niter fine ore；218 tons of tailings (contain NaNO30.5%th, H2O
10%).
Embodiment 6：Cubric niter particle diameter is taken less than 5mm fine ores (containing NaNO36%) 200 tons, use 120m3Light halogen (NaNO3
20g/l、NaCl 230g/l、Na2SO460g/l) and 280m3/ h circulation salt carries out continuous cocurrent jacket heat exchange type suspension device leaching
Take, suspension subsequent leaching series is 12 grades, leaching temperature is 20 DEG C, and leaching times at different levels are 1 hour, are contained after solid-liquid separation
The 400m of the compositions such as sodium nitrate3/ h nitre halogen solution and mine tailing, nitre halogen solution component (NaNO3 120g/l、NaCl 215g/l、
Na2SO455g/l), 87m3/ h nitre halogen solution is for evaporation production sodium nitrate, 280m3Under/h nitre halogen solution is participated in as circulation salt
The one continuous cocurrent jacket heat exchange type suspension device of 12 grades of circulation leaches cubric niter fine ore；221 tons of tailings (contain NaNO30.5%th, H2O
15%).
Claims (4)
1. sodium nitrate technique is reclaimed in a kind of cubric niter fine ore leaching, it is characterised in that：With water or light halogen and circulation salt mixed liquor
The fine ore of 5mm, cocurrent jacket for heat exchange are less than using multistage continuous cocurrent jacket heat exchange type suspension device leaching dissolving cubric niter particle diameter
Formula suspension device subsequent leaching series is 1-20 levels, and leaching temperature is 20-60 DEG C, leaching time 0.1-1 hours at different levels；Solid-liquid separation
The nitre halogen solution containing sodium nitrate and mine tailing are obtained afterwards, and a nitre halogen solution part evaporates sodium nitrate processed, and another part is used as circulation
Salt participates in subsequent cycle leaching cubric niter fine ore.
2. sodium nitrate technique is reclaimed in cubric niter fine ore leaching according to claim 1, it is characterised in that：The fine ore contains
NaNO31-13%, NaCl 15-25%, Na2SO44-7%.
3. sodium nitrate technique is reclaimed in cubric niter fine ore leaching according to claim 1, it is characterised in that：The nitre halogen solution
Middle each component content is NaNO3 10-600g/l、NaCl 300-30g/l、Na2SO4 10-150g/l。
4. sodium nitrate technique is reclaimed in cubric niter fine ore leaching according to claim 1, it is characterised in that：The tailings contains
NaNO30.5-1.0%, H2O 10-30%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611086760.4A CN106517253A (en) | 2016-12-01 | 2016-12-01 | Technology of recycling sodium nitrate by leaching nitratine fine ore |
Applications Claiming Priority (1)
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| CN201611086760.4A CN106517253A (en) | 2016-12-01 | 2016-12-01 | Technology of recycling sodium nitrate by leaching nitratine fine ore |
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| CN106517253A true CN106517253A (en) | 2017-03-22 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111892070A (en) * | 2020-09-07 | 2020-11-06 | 新疆硝石钾肥有限公司 | Powdery nitratine continuous halogen making system |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101343072A (en) * | 2008-08-20 | 2009-01-14 | 中蓝连海设计研究院 | Method for preparing sodium nitrate with soda niter |
| CN102167367A (en) * | 2010-12-28 | 2011-08-31 | 新疆安华矿业投资有限公司 | Process for producing high-concentration sodium nitrate brine through rotation dynamic leaching of nitratite ore |
| CN102689912A (en) * | 2012-06-18 | 2012-09-26 | 化工部长沙设计研究院 | Process for producing sodium nitrate from soda niter in size-fraction leaching manner |
-
2016
- 2016-12-01 CN CN201611086760.4A patent/CN106517253A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101343072A (en) * | 2008-08-20 | 2009-01-14 | 中蓝连海设计研究院 | Method for preparing sodium nitrate with soda niter |
| CN102167367A (en) * | 2010-12-28 | 2011-08-31 | 新疆安华矿业投资有限公司 | Process for producing high-concentration sodium nitrate brine through rotation dynamic leaching of nitratite ore |
| CN102689912A (en) * | 2012-06-18 | 2012-09-26 | 化工部长沙设计研究院 | Process for producing sodium nitrate from soda niter in size-fraction leaching manner |
Non-Patent Citations (1)
| Title |
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| 马茜茜等: ""钠硝石矿中硝酸钠水溶浸取过程研究"", 《无机盐工业》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111892070A (en) * | 2020-09-07 | 2020-11-06 | 新疆硝石钾肥有限公司 | Powdery nitratine continuous halogen making system |
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Application publication date: 20170322 |