CN101049920A - Method for absorbing and extracting phosphor and fluorin from phosphoric acid produced in kiln method - Google Patents
Method for absorbing and extracting phosphor and fluorin from phosphoric acid produced in kiln method Download PDFInfo
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- CN101049920A CN101049920A CN 200710052195 CN200710052195A CN101049920A CN 101049920 A CN101049920 A CN 101049920A CN 200710052195 CN200710052195 CN 200710052195 CN 200710052195 A CN200710052195 A CN 200710052195A CN 101049920 A CN101049920 A CN 101049920A
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Abstract
This invention discloses a method for separating phosphorus and fluorine of kiln process phosphoric acid by absorption. The method comprises: sending relatively high temperature phosphoric acid after hydration in primary and secondary hydration columns to a circulation tank for cooling, pumping into the hydration columns for circulation, sending gases after primary and secondary absorption to a Venturi absorber for re-absorption, collecting the residual acid mist by a collector, sending the absorbed gas and tail gas after fluorine absorption together to a chemical absorption column, and exhausting the tail gas. Besides, qualified fluosilicic acid can be obtained from the fluorine-containing diluted H3PO4 in the collector. The method utilizes the air with residual heat in the kiln, and has such advantages as no extra energy consumption, high phosphorus and fluorine separation efficiency, high concentration and low fluorine content in obtained H3PO4, and low P2O5 content in obtained fluosilicic acid. The obtained fluosilicic acid has a wide concentration range and a high purity, and is easy to utilize.
Description
Technical field
The present invention relates to the phosphorus fluorine method for absorbing and separating of a kind of method of tail gas absorption extraction, particularly a kind of kiln-process phosphoric acid.
Background technology
Inevitably contain fluorine element in the Rock Phosphate (72Min BPL), phosphorus-containing ore is produced the fluoro-gas that produces in the reduction process of yellow phosphorus and phosphoric acid and is had intensive toxicity and corrodibility, and human body and environment are all had huge harm.In thermal phosphoric acid and kiln-process phosphoric acid production process, fluorine element will be overflowed together with the phosphorus that restores in the Rock Phosphate (72Min BPL), and in the Vanadium Pentoxide in FLAKES hydro-combination process, fluoro-gas is dissolved in the water simultaneously, and hydrolysis generates silicofluoric acid (H
2SiF
6) wait fluorine-containing solution to coexist as in the phosphoric acid, have a strong impact on the quality product of phosphoric acid; In the wet method phosphoric acid manufacture process process, the fluorine element in the Rock Phosphate (72Min BPL) is silicofluoric acid (H by acidolysis
2SiF
6) wait fluorine-containing solution to coexist as in the phosphoric acid because concentration is lower, fluorine content wherein is more than the thermal phosphoric acid height, but because of main as production fertilizer, little to the phosphoric acid product quality influence; Along with the raising of phosphoric acid concentration, silicofluoric acid resolves into hydrogen fluoride and silicon tetrafluoride is overflowed from phosphoric acid in the gaseous state mode, and concentration of phosphoric acid and temperature are high more, and the fluorine content that retains in the phosphoric acid is low more; But direct heating mixing acid, energy consumption height not only, and cause absorb tolerance and strengthen, not high to the separation rate of phosphorus, fluorine, can not get the low hexafluorophosphoric acid of high density, and P in the silicofluoric acid
2O
5Content higher, the working load of fluorine absorption system is bigger.
Summary of the invention
It is little to the purpose of this invention is to provide a kind of energy consumption, to the separation rate height of phosphorus, fluorine, P in the silicofluoric acid that obtains
2O
5Content low, the phosphorus fluorine method for absorbing and separating of the kiln-process phosphoric acid that the working load of fluorine recovery system is little.
The object of the present invention is achieved like this: a kind of phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid,
To contain P
2O
5, SiF
4Introduce in the one-level absorption equipment with the kiln oil preparation phosphoric acid gas mixture of HF etc., lower the temperature, absorb, be cooled to 60-70 ℃ after the strong phosphoric acid heat exchange, carry out circulated sprinkling by cyclic acid pump through one-level phosphoric acid circulation groove through the spray recycled phosphoric acid; Move to the finished acid storage tank after simultaneously the part strong phosphoric acid being filtered;
Enter two-level absorption tower through the gas mixture after the first grade absorption tower cooling and absorbing and lower the temperature once more, absorb, circulation, process of cooling such as first grade absorption tower; Simultaneously the phosphoric acid in the part secondary circulation groove is added one-level circulation acid tank, keep the recycle acid concentration and the liquid level of first grade absorption tower;
Enter in three grades of absorption equipments through the gas mixture after the two-level absorption tower cooling and absorbing, to absorb remaining phosphoric acid acid mist and fluoro-gas, to form lower concentration phosphoric acid and silicofluoric acid mix acid liquor; The acid mist of failing on a small quantity to absorb enters multiple retaining collector again and captures, and the diluted acid of formation flows into keeps off in the circulation groove again; The part acid solution of keeping off circulation groove again adds secondary circulation acid tank after defluorinate, to keep the recycle acid concentration and the liquid level of two-level absorption tower, keeping off additional pure water in the acid tank again, make the phosphoric acid absorption system reach equilibrium state;
The tail gas that contains minute quantity phosphorus and fluorine at last enters the chemical absorption tower and carries out chemical absorption, makes its temperature be reduced to qualified discharge below 40 ℃;
Keep off the part diluted acid (w (H in the circulation groove again
3PO
4): 10-45%) be introduced in the defluorinate groove, dilute phosphoric acid is heated to 60-150 ℃ by the high temperature uncontaminated air, impels wherein fluorine to break away from acid solution with gaseous form and enters gas phase, is diffused in the uncontaminated air after the heat exchange, and enters the fluorine absorption system together;
Enter that most fluorine enters liquid phase and forms silicofluoric acid circulation acid solution in the gas of one-level fluorine absorber of fluorine absorption system, silicofluoric acid moves to silicofluoric acid finished product acid tank after reaching expection concentration;
The gas of process one-level fluorine absorber directly enters two-level absorption tower and absorbs once more, and the diluted acid of formation is carried out circulated sprinkling, and partly adds one-level fluorine circulation acid tank to keep one-level fluorine recycle acid concentration and liquid level;
Establish multiple retaining collector behind the secondary fluorine absorber, with the silicofluoric acid acid mist of carrying secretly in the capture tail gas, and flow into secondary fluorine circulation acid tank, tail gas is extracted the back out by induced draft fan and is entered chemical absorption tower qualified discharge after chemical absorption with the tail gas that phosphoric acid absorbs in the flow process.
Recycled phosphoric acid temperature in the one-level phosphoric acid absorption tower will remain on 80-120 ℃, and concentration remains on w (H
3PO
4): 75-115%.
Recycled phosphoric acid temperature in the secondary phosphoric acid absorption equipment will remain on 60-80 ℃, and concentration remains on w (H
3PO
4): 45-75%.
Three grades of fluorine-containing dilute phosphoric acid w (H that obtain that recycle acid equipment is interior
3PO
4): 10-45%, fluorine-containing w (F): 1-5%.
Introduce the defluorinate groove from the fluorine-containing dilute phosphoric acid of three grades of circulation acid tanks, feed temperature at 150-300 ℃ of air, bring fluorine into gas phase from liquid phase, heating simultaneously concentrates diluted acid to 60-120 ℃, and recovery obtains the silicofluoric acid that the phosphoric acid composition is reduced to the finished product requirement in the fluorine absorption system.
In the defluorinate groove by defluorinate and through heating spissated concentration at w (H
3PO
4): the phosphoric acid of 20-65% returns secondary phosphoric acid circulation acid tank, makes the phosphoric acid absorption system realize the circulation of continous-stable.
Three grades of absorption equipments adopt venturi tube.
The phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid provided by the invention, the phosphoric acid of the comparatively high temps after one-level, the hydration of secondary hydration tower enter separately circulation groove respectively lowers the temperature, and enters hydration tower circulated sprinkling by the phosphoric acid pump at last.Enter the venturi tube resorber through the gas after the two-stage absorption and absorb once more, and use and keep off the residual acid mist of collector capture again.Thereby entering the chemical absorption tower, the tail gas of the gas after the absorption after fluorine absorbs makes tail gas emptying up to standard.Also can from keep off the fluorine-containing dilute phosphoric acid the collector again, obtain qualified silicofluoric acid.The present invention only uses the waste heat air in the kiln, does not have other energy consumption, and is good to the separation rate of phosphorus, fluorine, can obtain the low hexafluorophosphoric acid of high density, also obtains P simultaneously
2O
5The silicofluoric acid that content is extremely low.The silicofluoric acid product concentration rank that obtains is wide, and the purity height is easy to utilize reprocessing.
Description of drawings
The invention will be further described below in conjunction with drawings and Examples.
Fig. 1 is a process flow sheet of the present invention.
Embodiment
Phosphoric acid absorbs flow process: the high-temperature kiln gas from kiln system enters one-level phosphoric acid absorption tower, high temperature circulation acid through one-level phosphoric acid interchanger in one-level phosphoric acid circulation groove by the cooling of low temperature soft water after, return one-level phosphoric acid absorption tower and absorb P in the kiln gas
2O
5And reduce the kiln gas temperature, telling a part of phosphoric acid simultaneously, to be filtered into the complex acid groove through filter be finished product; The cooling kiln gas introduce the absorption tower high temperature circulation acid of secondary phosphoric acid through secondary phosphoric acid interchanger in secondary phosphoric acid circulation groove by the cooling of low temperature soft water after, return secondary phosphoric acid absorption tower and absorb P in the kiln gas
2O
5And reduce the kiln gas temperature, tell a part of phosphoric acid simultaneously to one-level phosphoric acid circulation groove; The low temperature kiln gas is introduced the venturi tube resorber, and recycle acid enters three grades of phosphoric acid circulation grooves and returns three grades of P in the phosphoric acid resorbers absorption kiln gas
2O
5And reduce the kiln gas temperature, and tell a part of phosphoric acid simultaneously to the defluorinate tower, well water is mended as required into three grades of phosphoric acid circulation grooves in addition; The low levels kiln gas enters phosphoric acid fluorine retaining, and isolating phosphoric acid is introduced in three grades of phosphoric acid circulation grooves; Kiln gas after the demist is introduced the chemical absorption tower, and the chemical absorption tower adopts the alkali lye resorber, in the alkali lye that recycles and absorb a little P in the tail gas
2O
5With F after the induced draft fan qualified discharge.
Fluorine absorbs flow process: from the low temperature fluoric acid of phosphoric acid absorption system by from the high temperature air of kiln system at defluorinate tower internal heating, the phosphoric acid after the defluorinate returns secondary phosphoric acid circulation acid tank; Air after the heat exchange keeps off collection acid mist wherein again by fluoric acid, enters the one-level fluorine absorber again and absorbs fluorine, and circulating absorption solution is through entering the one-level fluorine absorber, and tells part and introduce finished product silicofluoric acid groove as byproduct; Draw gas and continue to absorb fluorine in the secondary fluorine absorber, circulating absorption solution enters the secondary fluorine absorber, and tells part and introduce the one-level fluorine absorber; Draw gas and after keeping off collector again, introduce the chemical absorption tower of phosphoric acid absorption system.Well water replenishes the secondary fluorine absorber.
The principle of work of chemical absorption tower is:
2H
3PO
4+3Ca(OH)
2→Ca
3(PO
4)
2↓+3H
2O
2HF+Ca(OH)
2→CaF
2↓+2H
2O
H
2SiF
6+Ca(OH)
2→CaSiF
6↓+2H
2O
Embodiment:
Temperature is 452 ℃, w (P
2O
5): 8.2% high-temperature kiln gas enters one-level phosphoric acid absorption tower, high temperature circulation acid in the one-level phosphoric acid circulation groove, 84 ℃ of temperature, w (H
3PO
4): 85.5%, one-level phosphoric acid interchanger by low temperature soft water cooling back temperature be 65 ℃ phosphoric acid to be filtered into the complex acid groove through filter be finished product, w (H
3PO
4): 85.5%, impurity: 0.0015%; The cooling kiln gas, 145 ℃ of temperature, w (P
2O
5): 1.58% introduces secondary phosphoric acid absorption tower, and two inhale recycle acid, 75.2 ℃ of temperature, w (H
3PO
4): 55.4% through secondary phosphoric acid interchanger in secondary phosphoric acid circulation groove by phosphoric acid after the low temperature soft water cooling, 55.3 ℃ of temperature, w (H
3PO
4): 55.4% to one-level phosphoric acid circulation groove; The low temperature kiln gas, 78 ℃ of temperature, w (P
2O
5): 0.57% introduces venturi tube resorber, 55 ℃ of kiln gas temperature, w (P
2O
5): 0.2%, enter phosphoric acid fluorine retaining, isolating phosphoric acid is introduced in three grades of phosphoric acid circulation grooves; 55.4 ℃ of kiln gas temperature after the demist, w (P
2O
5): 0.24%, introducing the chemical absorption tower is the alkali lye resorber, the alkali lye that recycles is among the Ca:10.80% and absorb a little P in the tail gas
2O
5With F after induced draft fan is up to standard, 45.5 ℃ of temperature, w (P
2O
5): 0.009%, the F:0.008% discharging.Guide to three grades of recycled phosphoric acid of defluorinate tower, 44 ℃ of temperature, w (H
3PO
4): 25.4%, at the high temperature air of quilt from kiln system, T=223 ℃, at defluorinate tower internal heating, the phosphoric acid after the defluorinate, 64 ℃ of temperature, w (H
3PO
4): 56.4% returns secondary phosphoric acid circulation acid tank; Gas after the heat exchange, 65 ℃ of temperature, w (F): 5% keeps off collection acid mist wherein again by fluoric acid, enters the one-level fluorine absorber again and absorbs fluorine, and circulating absorption solution is told part and is introduced finished product silicofluoric acid groove as byproduct; Draw gas, 45.5 ℃ of temperature, w (F): 0.75% continues to absorb fluorine in the secondary fluorine absorber, circulating absorption solution is told part and introduced the one-level fluorine absorber; Draw 35.3 ℃ of gas temperatures, w (F): 0.24%, the chemical absorption tower of introducing the phosphoric acid absorption system after keeping off collector again is the alkali lye resorber.Well water replenishes the secondary fluorine absorber.
Set forth above embodiment reaches following index in process of production and can finish the present invention: the recycled phosphoric acid temperature in the one-level phosphoric acid absorption tower will remain on 80-120 ℃, and concentration remains on w (H
3PO
4): 75-115%; Recycled phosphoric acid temperature in the secondary phosphoric acid absorption equipment will remain on 60-80 ℃, and concentration remains on w (H
3PO
4): 45-75%. Three grades of fluorine-containing dilute phosphoric acid w (H that obtain that recycle acid equipment is interior
3PO
4): 10-45%, fluorine-containing 1-5%.
Claims (8)
1, a kind of phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid is characterized in that:
To contain P
2O
5, SiF
4Introduce in the one-level absorption equipment with the preparation phosphoric acid gas mixture of HF etc., lower the temperature, absorb, be cooled to 60-100 ℃ after the strong phosphoric acid heat exchange, carry out circulated sprinkling by cyclic acid pump through one-level phosphoric acid circulation groove through the spray recycled phosphoric acid; To move to the finished acid storage tank behind the part strong phosphoric acid cold filtration simultaneously;
Enter two-level absorption tower through the gas mixture after the first grade absorption tower cooling and absorbing and lower the temperature once more, absorb, circulation, process of cooling such as first grade absorption tower; Simultaneously the phosphoric acid in the part secondary circulation groove is added one-level circulation acid tank, keep the recycle acid concentration and the liquid level of first grade absorption tower;
Enter in three grades of absorption equipments through the gas mixture after the two-level absorption tower cooling and absorbing, to absorb remaining phosphoric acid acid mist and fluoro-gas, to form lower concentration phosphoric acid and silicofluoric acid mix acid liquor; The acid mist of failing on a small quantity to absorb enters multiple retaining collector again and captures, and the diluted acid of formation flows into keeps off in the circulation groove again; The part acid solution of keeping off circulation groove again adds secondary circulation acid tank after defluorinate, to keep the recycle acid concentration and the liquid level of two-level absorption tower, keeping off additional pure water in the acid tank again, make the phosphoric acid absorption system reach equilibrium state;
The tail gas that contains minute quantity phosphorus and fluorine at last enters the chemical absorption tower and carries out chemical absorption, makes its temperature be reduced to qualified discharge below 40 ℃;
Keep off the part diluted acid (w (H in the circulation groove again
3PO
4): 10-45%) be introduced in the defluorinate groove, dilute phosphoric acid is heated to 60-150 ℃ by the high temperature uncontaminated air, impels wherein fluorine to break away from acid solution with gaseous form and enters gas phase, is diffused in the uncontaminated air after the heat exchange, and enters the fluorine absorption system together;
Enter that most fluorine enters liquid phase and forms silicofluoric acid circulation acid solution in the gas of one-level fluorine absorber of fluorine absorption system, silicofluoric acid reaches expection concentration (w (H
3PO
4): 10-18%), move to silicofluoric acid finished product acid tank;
The gas of process one-level fluorine absorber directly enters two-level absorption tower and absorbs once more, and the diluted acid of formation is carried out circulated sprinkling, and partly adds one-level fluorine circulation acid tank to keep one-level fluorine recycle acid concentration and liquid level;
Establish multiple retaining collector behind the secondary fluorine absorber, to capture the silicofluoric acid acid mist of carrying secretly in the tail gas, and flowing into secondary fluorine circulation acid tank, tail gas is extracted the back out by induced draft fan and is entered chemical absorption tower (void tower) qualified discharge after the chemistry spray absorbs with the tail gas that phosphoric acid absorbs in the flow process.
2, the phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid according to claim 1 is characterized in that, the recycled phosphoric acid temperature in the one-level phosphoric acid absorption tower will remain on 80-120 ℃, and concentration remains on w (H
3PO
4): 75-115%.
3, the phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid according to claim 1 is characterized in that: the recycled phosphoric acid temperature in the secondary phosphoric acid absorption equipment will remain on 60-80 ℃, and concentration remains on w (H
3PO
4): 45-75%.
4, the phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid according to claim 1 is characterized in that: three grades of fluorine-containing dilute phosphoric acid w (H that obtain that recycle acid equipment is interior
3PO
4): 10-45%, fluorine-containing 1-5%.
5, according to the phosphorus fluorine method for absorbing and separating of claim 1 or 4 described kiln-process phosphoric acids, it is characterized in that: introduce the defluorinate groove from the fluorine-containing dilute phosphoric acid of three grades of circulation acid tanks, feed temperature at 150-300 ℃ of air, bring fluorine into gas phase from liquid phase, heating simultaneously concentrates diluted acid to 60-120 ℃, and recovery obtains the silicofluoric acid that the phosphoric acid composition is reduced to the finished product requirement in the fluorine absorption system.
6, the phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid according to claim 5 is characterized in that: in the defluorinate groove by defluorinate and through heating spissated concentration at w (H
3PO
4): the phosphoric acid of 20-65% returns secondary phosphoric acid circulation acid tank, makes the phosphoric acid absorption system realize the circulation of continous-stable.
7, the phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid according to claim 1 is characterized in that: three grades of absorption equipments adopt venturi tube.
8, the phosphorus fluorine method for absorbing and separating of kiln-process phosphoric acid according to claim 1, it is characterized in that: keeping off collector again is one group and equipment with keeping off circulation groove again, keep off the acid mist that collector is used for capturing gas phase again, and its inflow is kept off in the circulation groove again, keep off diluted acid in the circulation groove again as the circulated sprinkling liquid of three grades of absorptions.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100521954A CN100424007C (en) | 2007-05-14 | 2007-05-14 | Method for absorbing and extracting phosphor and fluorin from phosphoric acid produced in kiln method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100521954A CN100424007C (en) | 2007-05-14 | 2007-05-14 | Method for absorbing and extracting phosphor and fluorin from phosphoric acid produced in kiln method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101049920A true CN101049920A (en) | 2007-10-10 |
| CN100424007C CN100424007C (en) | 2008-10-08 |
Family
ID=38781558
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007100521954A Expired - Fee Related CN100424007C (en) | 2007-05-14 | 2007-05-14 | Method for absorbing and extracting phosphor and fluorin from phosphoric acid produced in kiln method |
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| CN1071097A (en) * | 1991-09-28 | 1993-04-21 | 云南昆明磷肥厂 | Handle the method for waste gas containing fluoride |
| CN1182053A (en) * | 1996-11-12 | 1998-05-20 | 湖南化工研究院 | Production technology of tricalcium phosphate defluorinated in kiln |
| CN1162322C (en) * | 2000-05-16 | 2004-08-18 | 单光渝 | Process of preparing defluorinated phosphate and purifying fluoric tail gas |
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| CN104445118A (en) * | 2014-12-01 | 2015-03-25 | 四川玖长科技有限公司 | Process for preparing phosphoric acid from drawing smoke of kiln method phosphoric acid process |
| WO2016086826A1 (en) * | 2014-12-01 | 2016-06-09 | 四川玖长科技有限公司 | Improved device for preparing phosphoric acid from kiln egression flue gas of phosphoric acid process of kiln method, and phosphoric acid preparing process |
| CN105536474B (en) * | 2015-12-24 | 2018-03-27 | 浙江埃森化学有限公司 | A kind of device and its implementation that hydrogen fluoride in tail gas is removed using dynamic wave |
| CN105536474A (en) * | 2015-12-24 | 2016-05-04 | 浙江埃森化学有限公司 | Device for removing hydrogen fluoride from tail gas by virtue of dynamic waves and implementation method for device |
| CN106268180A (en) * | 2016-08-31 | 2017-01-04 | 贵州开磷集团股份有限公司 | A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant and method |
| CN110240164A (en) * | 2019-06-26 | 2019-09-17 | 威海恒邦化工有限公司 | The method and device of fluosilicic acid concentration |
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| CN100424007C (en) | 2008-10-08 |
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