CN210710758U - Wet-process phosphoric acid purification deep defluorination device - Google Patents
Wet-process phosphoric acid purification deep defluorination device Download PDFInfo
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- CN210710758U CN210710758U CN201921528150.4U CN201921528150U CN210710758U CN 210710758 U CN210710758 U CN 210710758U CN 201921528150 U CN201921528150 U CN 201921528150U CN 210710758 U CN210710758 U CN 210710758U
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Abstract
The utility model discloses a phosphoric acid purification degree of depth defluorination device by wet process, including defluorination reaction tank, filter equipment, concentrated flash distillation device and the strip tower that connects gradually, wherein defluorination reaction tank is connected with sodium hydroxide and adds the pipe and phosphoric acid adds the pipe, and concentrated flash distillation device's liquid outlet is connected with the feed inlet on strip tower upper portion, and the lower part of strip tower is equipped with the steam port, and the tower bottom of strip tower is connected with the phosphoric acid of purification discharging pipe, adopts the utility model discloses phosphoric acid and sodium hydroxide generate sodium fluosilicate after the full reaction in the defluorination reaction tank and deposit, get into concentrated flash distillation device through filtering and detach and deposit back liquid and carry out concentrated flash distillation, and most fluorine in the phosphoric acid is got rid of after twice flash distillation, after stripping defluorination once more on this basis, remaining fluorine is by thorough desorption.
Description
Technical Field
The utility model relates to a phosphoric acid production technical field, concretely relates to phosphoric acid purification degree of depth defluorination device of wet process.
Background
In the defluorination purification process of phosphoric acid, sodium hydroxide is added to react with acid, then sodium ions are combined with fluosilicic acid radical ions to generate sodium fluosilicate precipitate, and because sodium fluosilicate has certain solubility under an acidic condition, the aim of removing most of fluorine can be achieved, and the initial defluorination treatment can only control the fluorine content to be about 200 ppm. Technical grade 85% phosphoric acid has a high requirement for fluorine content, and food grade phosphoric acid has a higher requirement for fluorine content, about 20ppm or less. Thus, the phosphoric acid preliminarily defluorinated needs to be further defluorinated.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides a phosphoric acid purification degree of depth defluorination device of wet process.
The technical scheme is as follows: the utility model provides a phosphoric acid purification degree of depth defluorinating device of wet process which the key lies in: including defluorination reaction tank, filter equipment, concentrated flash distillation device and the strip tower that connects gradually, wherein defluorination reaction tank is connected with sodium hydroxide and adds the pipe and phosphoric acid and adds the pipe, concentrated flash distillation device's liquid outlet with the feed inlet on strip tower upper portion is connected, the lower part of strip tower is equipped with the steam port, the tower bottom of strip tower is connected with the phosphoric acid purification discharging pipe. By adopting the technical scheme, phosphoric acid and sodium hydroxide which need to be defluorinated are fully reacted in the defluorination reaction tank to generate sodium fluosilicate precipitate, the liquid after the precipitate is removed by the filtering device enters the concentration flash evaporation device for concentration flash evaporation, the liquid after flash evaporation enters the stripping tower, and the residual fluorine in the phosphoric acid is thoroughly removed under the action of steam.
Preferably, the method comprises the following steps:
above-mentioned concentrated flash distillation device is including the first concentrated heating jar, first flash distillation jar, the concentrated heating jar of second and the second flash distillation jar that connect gradually, filter equipment's liquid outlet with the feed inlet of first concentrated heating jar is connected, the liquid outlet of second flash distillation jar with the feed inlet of strip tower is connected. By adopting the structure, fluosilicic acid in phosphoric acid is heated and decomposed into gaseous silicon tetrafluoride and hydrogen fluoride, and then enters the flash tank for gas-liquid separation, the silicon tetrafluoride and the hydrogen fluoride gas overflow, and most of residual fluorine in the phosphoric acid is removed after twice concentration and flash evaporation.
Still be equipped with the decoloration tower between above-mentioned first flash tank and the concentrated heating jar of second, the liquid outlet of first flash tank with the feed inlet of decoloration tower is connected, the discharge gate of decoloration tower is connected with the collecting tank, the discharge gate of this collecting tank with the feed inlet of the concentrated heating jar of second is connected. By adopting the structure, the phosphoric acid after the first concentration flash evaporation is decolorized and then is subjected to the second concentration flash evaporation, so that the decolorizing effect is good, and the defluorination effect on the second concentration is favorably improved.
The first flash tank, the second flash tank exhaust port and the exhaust port at the top of the stripping tower are connected with the same absorption tower, the top of the absorption tower is connected with a desalted water feeding pipe, and the bottom of the absorption tower is connected with a fluosilicic acid discharge pipe. By adopting the structure, the silicon tetrafluoride and hydrogen fluoride gas overflowing from the flash tank and the stripping tower enter the absorption tower and are absorbed by desalted water to generate fluosilicic acid which can be used for other purposes.
The exhaust ports of the first concentrated heating tank and the second concentrated heating tank are respectively connected with a balance tank, and the liquid discharge ports of the balance tanks are connected with the same condensed water recovery tank. By adopting the structure, the water-steam mixture discharged by the two concentration heating tanks enters the balance tank, and after the balance tank discharges gas, the liquid is collected in the condensed water collecting tank and can be recycled.
The filtering device comprises a plate filter and a filtering acid tank which are connected with each other, wherein the liquid outlet of the defluorination reaction tank is connected with the feed inlet of the plate filter, and the liquid outlet of the filtering acid tank is connected with the feed inlet of the first concentration heating tank. By adopting the structure, after the heating concentration tank in the phosphoric acid is filtered, the phosphoric acid mother liquor is collected in the acid filtering tank, and the mixed gas is discharged at the place, so that the subsequent concentration flash evaporation is facilitated.
Compared with the prior art, the beneficial effects of the utility model are that: phosphoric acid and sodium hydroxide which need to be defluorinated are fully reacted in a defluorination reaction tank to generate sodium fluosilicate precipitate, liquid after the precipitate is removed by filtration enters a concentration flash evaporation device for concentration flash evaporation, most of fluorine in the phosphoric acid is removed after twice flash evaporation, and residual fluorine in the phosphoric acid is thoroughly removed after the phosphoric acid is subjected to steam stripping defluorination by a stripping tower on the basis.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
The present invention will be further described with reference to the following examples and accompanying drawings.
As shown in figure 1, a phosphoric acid purification degree of depth defluorination device by wet process, including defluorination reaction tank 1, filter equipment, concentration flash distillation device and strip tower 8 that connect gradually, wherein defluorination reaction tank 1 is connected with sodium hydroxide and adds pipe 13 and phosphoric acid and adds pipe 14, concentration flash distillation device's liquid outlet with the feed inlet on strip tower 8 upper portion is connected, strip tower 8's lower part is equipped with steam port 17, strip tower 8's the bottom of the tower is connected with and purifies phosphoric acid discharging pipe 11.
The filtering device comprises a plate filter 2 and a filtering acid tank 17 'which are connected with each other, the liquid outlet of the defluorination reaction tank 1 is connected with the feed inlet of the plate filter 2, and the filtering acid tank 17' is connected with the concentration flash device.
The concentration and flash evaporation device comprises a first concentration and heating tank 3, a first flash evaporation tank 4, a second concentration and heating tank 6 and a second flash evaporation tank 7 which are connected in sequence, a liquid outlet of the filtering acid tank 17' is connected with a feed inlet of the first concentration and heating tank 3 through a feed pump, a decoloring tower 5 is further arranged between the first flash evaporation tank 4 and the second concentration and heating tank 6, a liquid outlet of the first flash evaporation tank 4 is connected with a feed inlet of the decoloring tower 5, a discharge outlet of the decoloring tower 5 is connected with a liquid collecting tank 18, a discharge outlet of the liquid collecting tank 18 is connected with a feed inlet of the second concentration and heating tank 6 through a feed pump, a liquid outlet of the second flash evaporation tank 7 is connected with a feed inlet of the stripping tower 8, an exhaust port at the top of the first flash evaporation tank 4 and the second flash evaporation tank 7 and an exhaust port at the top of the stripping tower 8 are connected with the same absorption tower 9, the top of the absorption tower 9 is connected with a desalted water feeding pipe 15, and the bottom of the absorption tower 9 is connected with a fluosilicic acid discharge pipe 16.
The gas vent of first concentrated heating jar 3 and the concentrated heating jar 6 of second is connected with a compensating tank 10 respectively, be equipped with gas vent and leakage fluid dram on the compensating tank 10, all the leakage fluid dram of compensating tank 10 is connected with same condensate water recovery tank 12.
In this embodiment, first concentrated heating jar 3 is the same with the structure of the concentrated heating jar 6 of second, and the two is double-deck jacketed jar, including inner tank and outer jar, be equipped with the feed inlet on the inner tank, the liquid outlet of filtering acid groove 17' is connected with the feed inlet on the inner tank, and it has the heating steam pipe to coil between inner tank and the outer jar, is equipped with the gas vent on the outer jar, the exit end of heating steam pipe stretches out be connected with corresponding balance tank 10 behind the gas vent of outer jar.
As can be seen from the figure, stirrers are respectively arranged in the defluorination reaction tank 1 and the liquid collecting tank 18.
The working principle of the device is as follows:
phosphoric acid to be defluorinated is added into a defluorination reaction tank 1 through a phosphoric acid adding pipe 14, sodium hydroxide is added through a sodium hydroxide adding pipe 13 at the same time, sodium ions are combined with fluosilicic acid ions to generate sodium fluosilicate precipitates, the filtrate is concentrated into a filtering acid tank 17' after being filtered by a plate filter 12, gas in the filtrate escapes at the position, at the moment, because the filtrate is acidic, partial dissolved sodium fluosilicate is still mixed in the phosphoric acid, the phosphoric acid is continuously sent into a first concentration heating tank 3 to be heated and pressurized, fluosilicic acid in the phosphoric acid is gasified to generate silicon tetrafluoride and hydrogen fluoride, the silicon tetrafluoride and the hydrogen fluoride are sent into a first flash tank 4, gas and liquid are separated, the phosphoric acid after the first concentration flash is sent into a decolorization tower 5 to be decolorized, and then sent into a second concentration heating tank 6 and a second flash tank 7 to be subjected to second concentration flash, most of fluorine in the phosphoric acid is removed, and finally the phosphoric acid is, phosphoric acid is fully contacted with introduced steam in the stripping tower 8, residual fluorine is thoroughly removed through partial pressure stripping, and silicon tetrafluoride and hydrogen fluoride gas escaping from the first flash tank 4, the second flash tank 7 and the stripping tower 8 enter an absorption tower 9 and are absorbed by desalted water to obtain fluosilicic acid which can be used for other purposes.
Finally, it should be noted that the above description is only a preferred embodiment of the present invention, and those skilled in the art can make various similar representations without departing from the spirit and the scope of the present invention.
Claims (6)
1. The utility model provides a phosphoric acid purification degree of depth defluorinating device of wet process which characterized in that: including defluorination reaction tank (1), filter equipment, concentration flash distillation device and strip tower (8) that connect gradually, wherein defluorination reaction tank (1) is connected with sodium hydroxide and adds pipe (13) and phosphoric acid and adds pipe (14), the liquid outlet of concentration flash distillation device with the feed inlet on strip tower (8) upper portion is connected, the lower part of strip tower (8) is equipped with steam port (17), the tower bottom of strip tower (8) is connected with purification phosphoric acid discharging pipe (11).
2. The deep defluorination apparatus by wet phosphoric acid purification according to claim 1, characterized in that: the concentrated flash distillation device comprises a first concentrated heating tank (3), a first flash distillation tank (4), a second concentrated heating tank (6) and a second flash distillation tank (7) which are connected in sequence, a liquid outlet of the filtering device is connected with a feed inlet of the first concentrated heating tank (3), and a liquid outlet of the second flash distillation tank (7) is connected with a feed inlet of the stripping tower (8).
3. The deep defluorination apparatus by wet phosphoric acid purification according to claim 2, characterized in that: still be equipped with decoloration tower (5) between first flash tank (4) and the concentrated heating jar of second (6), the liquid outlet of first flash tank (4) with the feed inlet of decoloration tower (5) is connected, the discharge gate of decoloration tower (5) is connected with collecting tank (18), the discharge gate of this collecting tank (18) with the feed inlet of the concentrated heating jar of second (6) is connected.
4. The wet-process phosphoric acid purification deep defluorination device according to the claim 2 or 3, characterized in that: the utility model discloses a fluosilicic acid purification device, including first flash tank (4), second flash tank (7) gas vent and the gas vent at stripper (8) top is connected with same absorption tower (9), the top of absorption tower (9) is connected with demineralized water and adds pipe (15), the bottom of absorption tower (9) is connected with fluosilicic acid discharge pipe (16).
5. The deep defluorination apparatus by wet phosphoric acid purification according to claim 4, characterized in that: the exhaust ports of the first concentration heating tank (3) and the second concentration heating tank (6) are respectively connected with a balance tank (10), and the liquid discharge ports of the balance tanks (10) are connected with the same condensed water recovery tank (12).
6. The deep defluorination apparatus by wet phosphoric acid purification according to claim 4, characterized in that: the filtering device comprises a plate filter (2) and a filtering acid tank (17 ') which are connected with each other, the liquid outlet of the defluorination reaction tank (1) is connected with the feed inlet of the plate filter (2), and the liquid outlet of the filtering acid tank (17') is connected with the feed inlet of the first concentration heating tank (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921528150.4U CN210710758U (en) | 2019-09-12 | 2019-09-12 | Wet-process phosphoric acid purification deep defluorination device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921528150.4U CN210710758U (en) | 2019-09-12 | 2019-09-12 | Wet-process phosphoric acid purification deep defluorination device |
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| CN210710758U true CN210710758U (en) | 2020-06-09 |
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| CN201921528150.4U Active CN210710758U (en) | 2019-09-12 | 2019-09-12 | Wet-process phosphoric acid purification deep defluorination device |
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