CN216038730U - Tantalum-niobium extraction residual liquid treatment system - Google Patents
Tantalum-niobium extraction residual liquid treatment system Download PDFInfo
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Abstract
The utility model provides a tantalum-niobium raffinate treatment system which comprises an air compression bottle, a water saturation tower, a gas stripping tower, a first calcium hydroxide absorption tower, a second calcium hydroxide absorption tower and a third absorption tower, wherein the air compression bottle is connected with the water saturation tower through a first pipeline, a glass tube flowmeter is arranged on the first pipeline, the water saturation tower is connected with the gas stripping tower through a second pipeline, the gas stripping tower is connected with the first calcium hydroxide absorption tower through a third pipeline, a cooling assembly is arranged on the third pipeline, the first calcium hydroxide absorption tower is connected with the second calcium hydroxide absorption tower through a fourth pipeline, and the second calcium hydroxide absorption tower is connected with the third absorption tower. According to the tantalum-niobium raffinate treatment system, calcium fluoride solution with a certain concentration is obtained, the fluorine ions in the solution are recycled, and certain economic benefits are generated.
Description
Technical Field
The utility model belongs to the field of wastewater treatment, and particularly relates to a tantalum-niobium raffinate treatment system.
Background
A large amount of waste water is discharged every day from tantalum-niobium hydrometallurgy plants, and the waste water comprises extraction raffinate, tantalum and niobium hydroxide precipitation mother liquor, washing water, potassium fluotantalate crystallization mother liquor and the like. The wastewater contains fluorides and sulfates of W, Ti, Fe, Sb, etc. The common method for treating the wastewater in the market at present is to treat all the wastewater uniformly and adopt a precipitation method, namely adding lime to ensure that F < - >, SO in the wastewater4 2-Iso-formation of CaSO4、 CaF2And removing the precipitate. But not to CaSO4、CaF2And separating and recovering the solid.
F-SO in extraction raffinate4 2-The content is higher, and unified and other waste water are handled, not only cause the inventory to be too high, have also caused the wasting of resources.
Disclosure of Invention
In view of this, the present invention provides a system for treating raffinate of tantalum-niobium extraction, so as to solve the problems of high material input and resource waste.
In order to achieve the purpose, the technical scheme of the utility model is realized as follows:
the utility model provides a tantalum niobium raffinate processing system, including the air compression bottle, the water saturation tower, the gas blows and takes off the tower, first calcium hydroxide absorption tower, second calcium hydroxide absorption tower, the third absorption tower, the air compression bottle is connected with the water saturation tower through first pipeline, be equipped with the glass pipe flowmeter on the first pipeline, the water saturation tower is connected with the gas blow off tower through the second pipeline, the gas blows and takes off the tower and is connected with first calcium hydroxide absorption tower through the third pipeline, be equipped with cooling module on the third pipeline, first calcium hydroxide absorption tower is connected with the second calcium hydroxide absorption tower through the fourth pipeline, the second calcium hydroxide absorption tower is connected with the third absorption tower.
The bottom of gas stripping tower is equipped with first discharge gate, is equipped with the valve on the first discharge gate, is equipped with on the lateral wall of water saturation tower and adds waste water material funnel, and the lower part of water saturation tower is equipped with first gas distribution board, and the inside top of water saturation tower is equipped with first demister, and the interior bottom of water saturation tower is equipped with first plastic ball and packs, and the top of gas stripping tower is equipped with first thermometer. First demister can remove water to the hydrogen fluoride that blows off in the gas stripping tower, make hydrogen fluoride get into first calcium hydroxide and inhale, generate the calcium fluoride of certain concentration, produce certain economic benefits, first material ball filler can increase the area of contact of liquid and gas, the boiling point of hydrogen fluoride is 19 ℃, when the room temperature is higher than 19 ℃, the air contacts with the solution, hydrofluoric acid can become the state entering first calcium hydroxide absorption tower and second calcium hydroxide absorption tower of gas, can find out according to first thermometer whether the temperature in the gas stripping tower is higher than 19 ℃.
The bottom of water saturation tower is equipped with the second discharge gate, is equipped with the valve on the second discharge gate, is equipped with the funnel that adds water on the lateral wall of water saturation tower, and the lower part of water saturation tower is equipped with second gas distribution board, and the inside top of water saturation tower is equipped with the second demister, and the interior bottom of water saturation tower is equipped with second plastic ball filler, and the top of water saturation tower is equipped with the second thermometer. Be equipped with the water saturation tower behind the compressed air bottle, can carry out moist to compressed air to get rid of unnecessary moisture through the demister, make the gas air contact liquid earlier, carry out preliminary moist, then contact with waste water.
The cooling assembly comprises a cold bath tub which is arranged above the gas stripping tower. The cooling basin can cool hydrofluoric acid gas discharged from the gas stripping tower.
The third pipeline is connected with the upper part of the first calcium hydroxide absorption tower, the third pipeline stretches into the bottom of the first calcium hydroxide absorption tower, a first calcium hydroxide solution funnel is arranged on the side wall of the first calcium hydroxide absorption tower, a third discharge hole is formed in the bottom of the first calcium hydroxide absorption tower, a valve is arranged on the third discharge hole, and a third thermometer is arranged at the top of the first calcium hydroxide absorption tower.
The fourth pipeline is connected with the upper part of the second calcium hydroxide absorption tower, the fourth pipeline extends into the bottom of the second calcium hydroxide absorption tower, a second calcium hydroxide solution funnel is arranged on the side wall of the second calcium hydroxide absorption tower, a fourth discharge hole is formed in the bottom of the second calcium hydroxide absorption tower, a valve is arranged on the fourth discharge hole, and a fourth thermometer is arranged at the top of the second calcium hydroxide absorption tower.
The bottom is equipped with the active carbon in the third absorption tower, and the third absorption tower bottom is equipped with the fifth discharge gate, and the top of third absorption tower is equipped with the outlet duct. Further absorbing the gas by the active carbon, then releasing the gas and directly discharging the gas.
Compared with the prior art, the tantalum-niobium raffinate treatment system has the following beneficial effects:
1. the gas blowing tower can blow out hydrogen fluoride in the tantalum-niobium raffinate, the hydrogen fluoride respectively passes through the first calcium hydroxide absorption tower and the second calcium hydroxide absorption tower to obtain a calcium fluoride solution with a certain concentration, the reutilization of fluoride ions in the solution is realized, and certain economic benefits are generated.
2. Through using and first calcium hydroxide absorption tower and second calcium hydroxide absorption tower, can reduce the consumption of ammonia, and then reduce the production of waste water, reduce environmental protection running cost for the final waste residue volume that produces of tantalum niobium factory reduces in a large number.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate an embodiment of the utility model and, together with the description, serve to explain the utility model and not to limit the utility model. In the drawings:
FIG. 1 is a schematic diagram of a tantalum-niobium raffinate treatment system according to an embodiment of the present invention.
Description of reference numerals:
1-air compression bottle; 2-a water saturation column; 3-a gas stripping tower; 4-a first calcium hydroxide absorption tower; 5-a second calcium hydroxide absorption tower; 6-a third absorption column; 7-a first conduit; 8-glass tube flow meter; 9-a second conduit; 10-a third conduit; 11-a fourth conduit; 12-a fifth pipeline; 13-a first discharge port; 14-a waste water material feeding funnel; 15-a first gas distribution plate; 16-a first demister; 17-a first plastic ball filler; 18-a first thermometer; 19-a second discharge port; 20-a water adding funnel; 21-a second gas distribution plate; 22-a second demister; 23-a second plastic ball filler; 24-a second thermometer; 25-cold bath tub; 26-a first calcium hydroxide solution funnel; 27-a third discharge port; 28-a third thermometer; 29-second calcium hydroxide solution funnel; 30-a fourth discharge hole; 31-a fourth thermometer; 32-activated carbon; 33-a fifth discharge port; 34-an air outlet pipe.
Detailed Description
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
The utility model provides a tantalum niobium raffinate processing system, including air compression bottle 1, water saturation tower 2, gas blows tower 3, first calcium hydroxide absorption tower 4, second calcium hydroxide absorption tower 5, third absorption tower 6, air compression bottle 1 is connected with water saturation tower 2 through first pipeline 7, be equipped with glass pipe flowmeter 8 on the first pipeline 7, water saturation tower 2 is connected with gas blowing tower 3 through second pipeline 9, gas blows tower 3 and is connected with first calcium hydroxide absorption tower 4 through third pipeline 10, be equipped with cooling module on the third pipeline 10, first calcium hydroxide absorption tower 4 is connected with second calcium hydroxide absorption tower 5 through fourth pipeline 11, second calcium hydroxide absorption tower 5 is connected through fifth pipeline 12 with third absorption tower 6.
The bottom of gas stripping tower 3 is equipped with first discharge gate 13, is equipped with the valve on the first discharge gate 13, is equipped with on the lateral wall of water saturation tower 2 and adds useless water material funnel 14, and the lower part of water saturation tower 2 is equipped with first gas distribution board 15, and the inside top of water saturation tower 2 is equipped with first demister 16, and the interior bottom of water saturation tower 2 is equipped with the first plastic ball of a plurality of and packs 17, and the top of gas stripping tower 3 is equipped with first thermometer 18. The first demister 16 can remove water from the hydrogen fluoride blown off in the gas blowing tower 3, so that the hydrogen fluoride enters the first calcium hydroxide absorption tower to generate calcium fluoride with a certain concentration, certain economic benefits are generated, the contact area of liquid and gas can be increased by the first material ball packing, the boiling point of the hydrogen fluoride is 19 ℃, when the room temperature is higher than 19 ℃, air is in contact with the solution, hydrofluoric acid can enter the first calcium hydroxide absorption tower 4 and the second calcium hydroxide absorption tower 5 in a gas state, and whether the temperature in the gas blowing tower 3 is higher than 19 ℃ can be seen according to the first thermometer 18.
The bottom of water saturation tower 2 is equipped with second discharge gate 19, is equipped with the valve on the second discharge gate 19, is equipped with on the lateral wall of water saturation tower 2 and adds water funnel 20, and the lower part of water saturation tower 2 is equipped with second gas distribution board 21, and the inside top of water saturation tower 2 is equipped with second demister 22, and the interior bottom of water saturation tower 2 is equipped with a plurality of second plastic ball filler 23, and the top of water saturation tower 2 is equipped with second thermometer 24. Be equipped with water saturation tower 2 behind the compressed air bottle, can carry out moist to compressed air to get rid of unnecessary moisture through the demister, make the gas air contact liquid earlier, carry out preliminary moist, then contact with waste water.
The cooling assembly comprises a cold tub 25, the cold tub 25 being arranged above the gas stripping tower 3. The cooling basin can cool hydrofluoric acid gas discharged from the gas stripping tower 3.
The third pipeline 10 is connected with the upper part of the first calcium hydroxide absorption tower 4, the third pipeline 10 extends into the bottom of the first calcium hydroxide absorption tower 4, a first calcium hydroxide solution funnel 26 is arranged on the side wall of the first calcium hydroxide absorption tower 4, a third discharge hole 27 is arranged at the bottom of the first calcium hydroxide absorption tower 4, a valve is arranged on the third discharge hole 27, and a third thermometer 28 is arranged at the top of the first calcium hydroxide absorption tower 4.
The fourth pipeline 11 is connected with the upper part of the second calcium hydroxide absorption tower 5, the fourth pipeline 11 extends into the bottom of the second calcium hydroxide absorption tower 5, a second calcium hydroxide solution funnel 29 is arranged on the side wall of the second calcium hydroxide absorption tower 5, a fourth discharge hole 30 is arranged at the bottom of the second calcium hydroxide absorption tower 5, a valve is arranged on the fourth discharge hole 30, and a fourth thermometer 31 is arranged at the top of the second calcium hydroxide absorption tower 5.
The bottom in the third absorption tower 6 is provided with active carbon 32, the bottom of the third absorption tower 6 is provided with a fifth discharge hole 33, and the top of the third absorption tower 6 is provided with an air outlet pipe 34. The gas is further absorbed by the activated carbon 32 and then released to be directly discharged from a high place.
In the concrete use, at the funnel 20 of adding water of water saturation tower 2 and add the clear water, open the compressed air bottle, control compressed air's volume through glass flowmeter, make moist gas get into gas blow-off tower through the bottom, add waste water in the waste water funnel, waste water and gaseous full contact, and then generate hydrogen fluoride gas, hydrogen fluoride gas passes through first calcium hydrate absorption tower 4 and second calcium hydroxide absorption tower 5, then generate calcium fluoride, obtain the calcium fluoride solution of certain concentration, produce certain economic benefits. And the consumption of ammonia can be reduced, so that the generation of wastewater is reduced, the environment-friendly operation cost is reduced, and the amount of waste residues finally generated by a tantalum-niobium plant is greatly reduced.
The radioactive elements in the raw ore enter the raffinate. The dilute sulfuric acid produced in the technological process is recycled in a system, the enrichment of radioactive elements is produced, and the concentrated sulfuric acid can be treated in a targeted mode at regular intervals. Avoids the harm caused by the uncontrollable entering of radioactive elements into the waste residues and the huge amount of the waste residues.
The daily amount of wastewater treated was 48m3For example, HF and H in wastewater from a common commercial process2SO4All react with the added CaO to generate sediment, and the sediment is mixed with waste salt and radioactive substances in the waste water into the waste residues, and the generated waste residues are 31.5 to 48.8 tons/day. The scheme can reduce the generation of 31.5-48.8 tons of waste slag every day.
The daily amount of wastewater treated was 48m3For example, the content of hydrofluoric acid in the wastewater is 2-6mol/L, the content of total HF in the wastewater is 96-288mol, the recovery rate of the scheme is about 95%, and the recovery concentration is 10% -30%. The amount of recovered hydrofluoric acid solution is 9.1-27.4 tons/day calculated by 20% concentration, resulting in an economic value of 1.1-3.3 ten thousand yuan/day.
H in waste water2SO4The content of the sulfuric acid is 240-336mol, the recovery concentration is 40-60 percent, the amount of the recovered sulfuric acid solution is 30-50 tons/day calculated by 50 percent concentration, and the economic value is 0.6-1 ten thousand yuan per day. The specific data are as follows:
the daily amount of wastewater treated was 48m3For example. 96-288kmol of hydrofluoric acid is recovered every day, the usage amount of ammonia is reduced to 96-288kmol, and the cost is reduced to 6528 and 19584 yuan every day (calculated according to 4 yuan/kg of pure ammonia).
The part of ammonia enters a wastewater system, the consumption of the NaoH for ammonia distillation is 96-288kmol, and the cost is reduced by 7680 yuan and 23040 yuan (calculated according to pure NaoH: 2 yuan/kg) every day.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (7)
1. A tantalum niobium raffinate processing system which characterized in that: comprises an air compression bottle (1), a water saturation tower (2), a gas stripping tower (3), a first calcium hydroxide absorption tower (4), a second calcium hydroxide absorption tower (5) and a third absorption tower (6), air compression bottle (1) is connected with water saturation tower (2) through first pipeline (7), be equipped with glass pipe flowmeter (8) on first pipeline (7), water saturation tower (2) are connected with gas stripping tower (3) through second pipeline (9), gas stripping tower (3) are connected with first calcium hydroxide absorption tower (4) through third pipeline (10), be equipped with cooling module on third pipeline (10), first calcium hydroxide absorption tower (4) are connected with second calcium hydroxide absorption tower (5) through fourth pipeline (11), second calcium hydroxide absorption tower (5) are connected through fifth pipeline (12) with third absorption tower (6).
2. The tantalum-niobium raffinate processing system of claim 1, wherein: the bottom of gas stripping tower (3) is equipped with first discharge gate (13), is equipped with the valve on first discharge gate (13), is equipped with on the lateral wall of water saturation tower (2) and adds waste water material funnel (14), and the lower part of water saturation tower (2) is equipped with first gas distribution board (15), and the inside top of water saturation tower (2) is equipped with first demister (16), and the interior bottom of water saturation tower (2) is equipped with first plastic ball filler (17), and the top of gas stripping tower (3) is equipped with first thermometer (18).
3. The tantalum-niobium raffinate processing system of claim 1, wherein: the bottom of water saturation tower (2) is equipped with second discharge gate (19), is equipped with the valve on second discharge gate (19), is equipped with on the lateral wall of water saturation tower (2) and adds water funnel (20), and the lower part of water saturation tower (2) is equipped with second gas distribution board (21), and the inside top of water saturation tower (2) is equipped with second demister (22), and the interior bottom of water saturation tower (2) is equipped with second plastic ball filler (23), and the top of water saturation tower (2) is equipped with second thermometer (24).
4. The tantalum-niobium raffinate processing system of claim 1, wherein: the cooling assembly comprises a cold tub (25), and the cold tub (25) is arranged above the gas stripping tower (3).
5. The tantalum-niobium raffinate processing system of claim 1, wherein: third pipeline (10) are connected with the upper portion of first calcium hydroxide absorption tower (4), and third pipeline (10) stretch into first calcium hydroxide absorption tower (4) bottom, are equipped with first calcium hydroxide solution funnel (26) on the lateral wall of first calcium hydroxide absorption tower (4), and the bottom of first calcium hydroxide absorption tower (4) is equipped with third discharge gate (27), is equipped with the valve on third discharge gate (27), and the top of first calcium hydroxide absorption tower (4) is equipped with third thermometer (28).
6. The tantalum-niobium raffinate processing system of claim 1, wherein: fourth pipeline (11) are connected with the upper portion of second calcium hydroxide absorption tower (5), and fourth pipeline (11) stretch into second calcium hydroxide absorption tower (5) bottom, are equipped with second calcium hydroxide solution funnel (29) on the lateral wall of second calcium hydroxide absorption tower (5), and the bottom of second calcium hydroxide absorption tower (5) is equipped with fourth discharge gate (30), is equipped with the valve on fourth discharge gate (30), and the top of second calcium hydroxide absorption tower (5) is equipped with fourth thermometer (31).
7. The tantalum-niobium raffinate processing system of claim 1, wherein: the bottom is equipped with active carbon (32) in third absorption tower (6), and third absorption tower (6) bottom is equipped with fifth discharge gate (33), and the top of third absorption tower (6) is equipped with outlet duct (34).
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| CN202122372424.9U CN216038730U (en) | 2021-09-28 | 2021-09-28 | Tantalum-niobium extraction residual liquid treatment system |
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| CN202122372424.9U CN216038730U (en) | 2021-09-28 | 2021-09-28 | Tantalum-niobium extraction residual liquid treatment system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115852172A (en) * | 2023-02-13 | 2023-03-28 | 锦益创典(天津)科技有限责任公司 | System and method for decomposing tantalum-niobium slurry |
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2021
- 2021-09-28 CN CN202122372424.9U patent/CN216038730U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115852172A (en) * | 2023-02-13 | 2023-03-28 | 锦益创典(天津)科技有限责任公司 | System and method for decomposing tantalum-niobium slurry |
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