CN1062512A - Tower Wet-process Phosphoric Acid Production method and apparatus - Google Patents
Tower Wet-process Phosphoric Acid Production method and apparatus Download PDFInfo
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- CN1062512A CN1062512A CN 91108059 CN91108059A CN1062512A CN 1062512 A CN1062512 A CN 1062512A CN 91108059 CN91108059 CN 91108059 CN 91108059 A CN91108059 A CN 91108059A CN 1062512 A CN1062512 A CN 1062512A
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Abstract
The invention provides a kind of pre-production method and equipment of tower phosphoric acid by wet process, its chemical reaction is to carry out in tempering tank and extraction tower, or in the extraction tower of band premixer, carry out, reaction slurry mixes with meeting from two water thing crystal seeds at the bottom of the tower at Ta Nei, carry out hydration reaction, and through conical distributor and grid shape divider, slip is stirred and the mass transfer heat exchange by the pressurized air that enters at the bottom of the tower.The present invention can be with mid low grade phosphate rock (P
2O
5〉=25%) make raw material, the phosphorus ore percentage extraction is more than 99%, P
2O
5Total yield can directly make 32%P more than 97%
2O
5Phosphoric acid, the by-product phosphogypsum can directly be used as the raw material of cement, gypsum wallboard.
Description
The invention belongs to the phosphoric acid process industry, be used for the production of the phosphoric acid by wet process of ground phosphate rock and sulfuric acid reaction.
Phosphoric acid by wet process is one of important means of producing phosphoric acid, and at present, industrial production mainly adopts two water thing methods and half water thing-two water thing method.Traditional technology is that ground phosphate rock or ore pulp, sulfuric acid, circulation dilute phosphoric acid are added in the extraction tank simultaneously, (dilute phosphoric acid that ground phosphate rock is circulated that has adds one earlier and gives mixing tank, and extraction tank is advanced in overflow again, and the volume that gives mixing tank is very little, there is not whipping appts, do not have essential different with direct adding extraction tank), rely on machinery (stirring arm) to stir air or vacuum cooling, make slip, isolate phosphoric acid and phosphogypsum again, the problem of existence is to rely on mechanical stirring, and stirring intensity is restricted.Be difficult to avoid local material SO
-2 4, Ca
+ 2, Ca10(PO
4)
6F
2Deng excessive concentration, be easy to generate CaSO
4NH
2O is to the topped and HPO of phosphorus ore particle
-2 4Replace SO
-2 4Effect, influence the decomposition percentage extraction of phosphorus ore; It two is modes of air cooling or vacuum cooling, and the slip in the same extraction tank almost is in one and waits temperature state.CaSO
4NH
2The O crystalline forms and grows up and can not get ideal control, adds that the mechanical friction of stirring arm makes the crystal fretting corrosion and splits, and is difficult to form the CaSO that particle is thick, strainability is good
4NH
2The O crystal makes P
2O
5Washing loss increase, reduce the quality of phosphogypsum; It three is that to stir gearing many, influences Housing Starts, and maintenance cost is big; It four makes the ammonium phosphate solid fertilizer because phosphoric acid by wet process is mainly used in, and then needs could satisfy than the phosphorus ore of higher-grade the need of industrial production of solid phosphorus ammonium by above-mentioned technology, and the phosphorus ore of China be based in low-grade." in and slurry concentrated process " novel process (being called for short Yin Shanfa) of the common development of silver mountain phosphate fertilizer plant and Chengdu Univ. of Science ﹠ Technology, employing be two traditional water thing methods, the 22%P that produces with the mid low grade phosphate rock powder
2O
5The phosphoric acid solution of concentration and gas ammonia neutralization make the monoammonium phosphate dilute solution, concentrate through economic benefits and social benefits, and spraying drying makes powder ammonium phosphate.The problem that exists is: the phosphoric acid concentration that 1. makes is low, and is lower by 10% than the phosphoric acid concentration of producing the monoammonium phosphate defined, and the rare phosphor ammonium slurry that makes with this lower concentration phosphoric acid will concentrate through economic benefits and social benefits, just can make solid phosphorus ammonium, has increased power, consumption of heat energy.2. P
2O
5Total yield low, only below 90%, the raw materials consumption quota is high.3. phosphogypsum is phosphorous (contains P
2O
5＞1.0% contains wet (H
2O ≈ 28%) amount is big, can not directly be used as the raw material of cement, gypsum wallboard.Store up for a long time, take a large amount of soils, contaminate environment.Though this technology has solved the problem of utilizing of low-grade phosphate ore stone, on the manufacturing process of phosphoric acid, do not have new breakthrough.
The objective of the invention is to overcome the above-mentioned deficiency of prior art and a kind of employing mid low grade phosphate rock (P is provided
2O
5〉=25%) direct production goes out 32%P
2O
5Phosphoric acid, P
2O
5The total yield height, phosphogypsum phosphorus content water capacity is low, starting material power and heat energy consumption is low, pollute Wet-process Phosphoric Acid Production method and apparatus low, that comprehensive benefit is good.
Technology implementation scheme of the present invention is: one, extraction tower+mixing slot type Wet-process Phosphoric Acid Production method, ground phosphate rock and circulation dilute phosphoric acid are mixed in tempering tank fully, and carry out the first step chemical reaction:
With pump mixed slurry is input into extraction tower, adds the vitriol oil simultaneously, in tower, under the air violent stirring, mix immediately, and carry out the second step chemical reaction:
Half water thing CaSO
41/2 H
2The O slip from up to down slowly moves in extraction tower, has a large amount of two water thing CaSO in the tower middle and upper part with by what the cycle stock stock pump was carried at the bottom of tower
42H
2The low temperature slip of O crystal seed meets, mixes, and temperature drops to 70～75 ℃, half water thing CaSO
41/2 H
2O carries out hydration reaction, generates two water thing CaSO
42H
2The O gypsum in extraction tower, the silicon-dioxide in the slip, metal silicate and hydrogen fluoride reaction:
The part silicofluoric acid decomposes the effusion silicon tetrafluoride gas
Because the low temperature slurry circulation has been brought a large amount of two water thing CaSO into
42H
2The O crystal seed keeps with suitable temperature the hydration reaction district, and makes two water thing CaSO
42H
2O crystalline growth and crystal seed keep certain proportion, the two water thing CaSO that hydration reaction generates
42H
2The O solute keeps suitable degree of supersaturation.Under this degree of supersaturation, two water thing CaSO
42H
2The two water thing CaSO that the generation of O nucleus and crystal are grown up and exhausted
42H
2The summation amount of O solute just can be offset the two water thing CaSO that hydration reaction generates
42H
2The amount of O solute forms crystalline and grows up to obtain the control of appropriateness.The pressurized air that at the bottom of extraction tower, adds, through conical distributor and grid shape divider, from bottom to top with the reaction slurry countercurrent movement, slip is played the violent stirring effect, slip is mixed all the time, and and the heat exchange of slip mass transfer, make reaction slurry be gradually the temperature curve that reduces by 50～55 ℃ of 70～75 ℃ → bottoms, 95～98 ℃ → middle and upper part, top, help decomposing extractive reaction and half water thing CaSO
41/2 H
2The hydration reaction of O is carried out, and helps two water thing CaSO
42H
2The formation of O gypsum crystal and growing up, it is thick to form particle, the gypsum crystal that strainability is good, obtaining water capacity, phosphogypsum that phosphorus content is lower, because pressurized air contacts with the reaction slurry bubbling, the exhaust gas body saturation ratio height that wets, the moisture vapor amount is big, and slip is played inspissated.
Said tempering tank is the cylindrical enclosure device in the above-mentioned technology, a stirring arm is housed, step-down gear and electric motor are arranged on the stirring arm, mixing tank is given in the side on the cell body, giving mixing tank is cylindrical housings, and the ground phosphate rock opening for feed is arranged at its top, and the fast setter of material is housed on the opening for feed, side has the import of circulation dilute phosphoric acid, and the mixed slurry shower nozzle that stretches in the tempering tank is arranged at the bottom.3 temperature test points and 3 liquid level test point are arranged in the device.
Said extraction tower, tower body is cylindrical, the mixed slurry inlet of band shower nozzle and the vitriol oil enter the mouth respectively on the top of tower body, circulation slip inlet is in the middle and upper part of tower body, the taking-up slurry outlet is arranged at the tower body bottom, the circulation slurry outlet, compressed air inlet, top of tower has pneumatic outlet, according to 2～5 layers of conical distributor are set in the industrial scale tower, 4～8 layers of grid shape divider, pressurized air is made countercurrent movement from bottom to up with by the reaction slurry under the tower body top by conical distributor and grid shape divider, make reaction slurry uniform mixing fully, and regulate temperature in the tower.7 temperature test points and 7 liquid level test point also are set, so that observing tower internal reaction state is regulated in the tower.
Two, the tower Wet-process Phosphoric Acid Production method of extraction
The employed extraction tower of this technology, mixing tank is given at top at tower, giving mixing tank is cylindrical housings, the ground phosphate rock opening for feed is arranged at its top, the fast setter of material is housed on the opening for feed, the housing side has the import of circulation dilute phosphoric acid, and housing bottom has and stretches into the intravital mixed slurry shower nozzle of tower and at the top of extraction tower side pneumatic outlet is arranged, said extraction tower in the same extraction tower of other construction and device in the tower+mixing slot type phosphorus method phosphoric acid method.
Ground phosphate rock, circulation dilute phosphoric acid are added the extraction tower top simultaneously give mixing tank, flow in the extraction tower through shower nozzle, simultaneously, with the vitriol oil in shower nozzle adds extraction tower.Enter at the bottom of by tower under the compressed-air actuated violent stirring in the tower, mix immediately.Carry out following main chemical reactions
Half water thing CaSO
41/2 H
2The O slip slowly moves in extraction tower from top to bottom, has a large amount of two water thing CaSO what tower middle and upper part and cycle stock stock pump were carried at the bottom of tower
42H
2The low temperature slip of O crystal seed meets, mixing, temperature are reduced to 70～75 ℃, half water thing CaSO
41/2 H
2O carries out hydration reaction, generates two water things:
The same extraction tower of the growth control state+mixing slot type production method of slurry reaction, circulation and crystal seed in the tower.
The prepared slip of above-mentioned two methods is sent filter to and is filtered, washs and obtain phosphoric acid and phosphogypsum by taking out shurry pump.
Adopt above-mentioned phosphoric acid by wet process technology, with mid low grade phosphate rock (P
2O
5〉=25%) make raw material, phosphorus ore resolution ratio is more than 99%, P
2O
5Total yield is more than 97%, and can directly make 32%P
2O
5Phosphorus simultaneously, is paid the product phosphogypsum and is contained wet (H
2O).Phosphorus (P
2O
5) amount is low, can directly be used as the raw material of cement, gypsum wallboard, also can make sulfuric acid, the raw material of ammonium sulfate production.
The present invention compared with prior art has following advantage: 1. the main economic and technical indices of remarkable in economical benefits, the present invention and Yin Shanfa is as follows: (the average composition of phosphorus ore is: P
2O
526.8%, CaO38.36%, Fe
2O
31.36%, Al
2O
32.18% MgO1.04%, SO
30.36%, F3.0%, CO
23.47%, bright mistake 4.58%, acid non-soluble substance 18.7%).
The present invention and Yin Shan method phosphoric acid main economic and technical indices synopsis
| Index name | Unit | The present invention | Yin Shanfa | Remarks |
| The phosphorus ore grade | P?O?％ | 26.8 | 26.8 | The hubei baokang phosphorus ore |
| Supplies consumption | ||||
| Phosphorus ore | t/TP 2O 5 | 3.847 | 4.431 | |
| Sulfuric acid (98%) | .. | 3.033 | 3.174 | |
| Steam (0.4MPa) | .. | / | 3.789 | Being used for phosphor ammonium slurry concentrates |
| P 2O 5Total yield | ％ | ≥97 | 84.22 | |
| Product acid concentration | ％P 2O 5 | 32 | 23 | |
| The phosphogypsum quality | ||||
| CaO | ％ | 26.83 | 27.07 | |
| Full phosphorus (P 2O 5) | ％ | 0.34 | 1.12 | |
| Water-soluble phosphorus (P 2O 5） | ％ | 0.15 | / | |
| Water capacity (H 2O） | ％ | 15～20 | ～28 |
From last table as seen, P per ton
2O
5Product (phosphorus ammonium) is saved 0.584 ton of phosphorus ore, 0.141 ton in sulfuric acid than Yin Shanfa, and 3.789 tons of steam are pressed 100 yuan/ton in ground phosphate rock, (98%) 200 yuan/ton in sulfuric acid, 23 yuan of/ton meters of steam, 1.3 ten thousand tons of/year P of universal design
2O
5Phosphoric acid, 30,000 tons of/year phosphorus ammonium scales then can reduce by 225.87 ten thousand yuan of raw material energy expensess in 1 year.The product phosphogypsum is phosphorous, water capacity all reaches international most advanced level owing to pay.Can replace the plaster of paris.Paid 8.614 ten thousand tons of product phosphogypsums in 1 year by above-mentioned scale, by 29 yuan/ton, income then reaches 249.81 ten thousand yuan.Two totals can increase by 492.91 ten thousand yuan of economic benefits.
Social benefit, the present invention make a large amount of in low-grade phosphorus ore used, reduced the waste of phosphate rock resource, compare with Yin Shanfa, use P
2O
5〉=25% phosphorus ore directly expects to produce the phosphoric acid of 32% concentration, is used for the manufacturing of phosphorus ammonium, can cancel the slip enrichment process and reduce the scale that heat supply (vapour) is installed, and saves about 1,000,000 yuan of one-time investments.
3. environmental benefit.The present invention pays the product phosphogypsum can directly be used as cement, the raw material of gypsum wallboard.Phosphogypsum slag becomes a pair product and sells.1.3 ten thousand tons of/year P
2O
5Phosphoric acid plant can be saved phosphogypsum every year and push away 2.58 mu of land occupations and (high 20 meters " three wastes " environmental pollution is administered by average heap at all.Simultaneously, because slot type Wet-process Phosphoric Acid Production 32%P
2O
5The desired phosphorus ore grade of phosphoric acid has reduced by 5 percentage points, a large amount of mid low grade phosphate rock stone is directly used without ore dressing, thereby reduced the pollution of flotation of phosphate rock field waste residue to environment.
Fig. 1 mixes slot type phosphoric acid by wet process one embodiment production method schema for extraction tower adds;
Fig. 2 is the tower phosphoric acid by wet process one embodiment production method schema of extraction;
Fig. 3 is the structure iron of extraction tower one embodiment;
Fig. 4 is the structure iron of another embodiment of extraction tower;
Fig. 5 is the structural representation of tempering tank;
Fig. 6 gives the extraction tower structural representation of mixing tank for band;
Fig. 7 gives another embodiment of the extraction tower of mixing tank for band.
The invention will be further described below in conjunction with accompanying drawing.
Among Fig. 1, (100 order 95%) ground phosphate rock of sending here by material process, mixing tank 10 is given in the input of metering back, simultaneously, the circulation dilute phosphoric acid enters and gives mixing tank 10 and ground phosphate rock and give after the mixing together that overflow enters tempering tank 1, be delivered into extraction tower 5 through stirring complete mixed slip by shurry pump 2, simultaneously, by sulfuric acid pump 4 vitriol oil in the sulfuric acid storage tank 3 is input into extraction tower 5, through the air violent stirring of countercurrent movement in the tower, the mixed slurry and the vitriol oil mix immediately, and react, the big calorimetric of emitting remains in 95～98 scopes reaction slurry temperature, mainly generates things such as half water thing gypsum and phosphate aqueous solution.Reaction slurry constantly moves from top to bottom lentamente, has two water thing CaSO in the tower middle and upper part with by cycle stock stock pump 6 from what tower bottom was carried into
42H
2The low temperature of O crystal seed＜50～55 ℃) circulation slip meets, mix, temperature is reduced to about 70～75 ℃, half water thing gypsum begins to carry out hydration reaction, generates two water thing gypsum, and reaction slurry continues to move down, temperature reduces gradually, react sophisticated slurry temperature and reduce in 50～55 ℃ of scopes, a part of slip is sent filter to by taking-up shurry pump 7 and is filtered, washs, and obtains phosphogypsum and phosphoric acid.Another part slip is sent back in the extraction tower by cycle stock stock pump 6 and is circulated.The pressurized air of sending by air compressor 9, after water cooler 8 coolings, enter in the tower through extraction tower 5 bottom conical distributors again, move with tower internal reaction slip adverse current from bottom to top, play stirring, mass transfer, heat exchange effect, the waste gas that produces with reaction is derived by top of tower together and is entered the device that defluorinate is handled then.In air-cooler 8, delivered to hot water tank by the water coolant after the warm air beating, use for the filter washing.
Among Fig. 2, what (the 100 order 95%) ground phosphate rock after the metering was sent into extraction tower 13 tops gives mixing tank 18, in giving mixing tank 18, give and mixing with the circulation dilute phosphoric acid, advance in the extraction tower 13 through shower nozzle, simultaneously by sulfuric acid pump 12 with the vitriol oil in the sulfuric acid storage tank 11 in shower nozzle is sent extraction tower 13 to, in tower, under the violent stirring of the air of countercurrent movement, mix immediately, a large amount of heat is emitted in reaction, makes slurry temperature remain on the main CaSO of generation in 95～98 ℃ of scopes
41/2 H
2O phosphoric acid and overflow CO
2, SiF gas etc.Reaction slurry constantly moves from top to bottom lentamente, passes on the CaSO that has that comes from tower 13 bottoms in the tower middle and upper part with by cycle stock stock pump 14
42H
2The circulation slip of the low temperature of O crystal seed (50～55 ℃) meets, mixes, and temperature is reduced to about 75 ℃, CaSO
41/2 H
2O begins to carry out hydration reaction, generates CaSO
42H
2O, reaction slurry continue to move down, and temperature reduces gradually, CaSO
42H
2The O gypsum crystal is grown up gradually.At the bottom of tower, reacting sophisticated slurry temperature reduces in 50～55 ℃ of scopes, part slip is sent filter to by taking-up shurry pump 15 and is filtered, washs, obtain phosphoric acid and phosphogypsum, another part slip is sent extraction tower 13 internal recycle back to by cycle stock stock pump 14, through conical distributor and grid shape divider reaction slurry is stirred heat exchange by entering in the tower through extraction tower 13 bottoms through water cooler 16 refrigerative pressurized air of sending of air compressor 17; Waste gas is derived by top of tower and is entered the defluorinate processing.
Among Fig. 3, waste gas outlet 20 is arranged at 19 tops for cylindrical extraction tower housing, housing 19, and the mixed slurry inlet 21 and the vitriol oil inlet 22 of band shower nozzle arranged at top, and there is the circulation slip inlet 23 of band shower nozzle the middle and upper part, 24,6 layers of grid shape of 4 layers of conical distributor divider 25 is arranged in the tower; Take out slurry outlet 26, circulation slurry outlet 27, compressed air inlet 28 are contained in the bottom of extraction tower respectively.
Among Fig. 4, conical shell 29 is divided into extractive reaction section 31 and hydration reaction section 32 by dividing plate 30.Mixed slurry inlet 33 is arranged on extractive reaction section 31 tops, waste gas outlet 35 is arranged at the vitriol oil 34 tops that enter the mouth, 2 layers of conical distributor 36 are arranged in the tower body, 3 layers of grid shape divider 37, half water material slurry outlet 38 is arranged at the bottom, compressed air inlet 39, half water material slurry inlet 40 is arranged, circulation slip inlet 41, hydration reaction pneumatic outlet 42 on hydration reaction section 32 tops, 2 layers of conical distributor 43 are arranged in the tower body, 4 layers of grid shape divider 44, compressed air inlet 45 is arranged at the bottom, takes out slurry outlet 46, circulation slurry outlet 47, all material inlets all have shower nozzle.
Among Fig. 5, the cell body 48 of tempering tank 1 is cylindrical, stirring arm 49, speed reduction unit 50, electric motor 51 are housed, mixing tank 52 is given on cell body top, and opposite side has pneumatic outlet 53, and mixed slurry outlet 54 is arranged at the cell body bottom, give mixing tank 52 by conical shell 55, ground phosphate rock feed-pipe 56, circulation dilute phosphoric acid import 57, the fast setter 58 of material, mixed slurry shower nozzle 59 is formed.
Among Fig. 6, mixing tank 18 is given at the top of cylindrical tower body 60, gives mixing tank 18 by conical shell 62, ground phosphate rock feed-pipe 63, and fast setter 65 is expected in circulation dilute phosphoric acid import 64, mixed slurry shower nozzle 66 is formed; The top of tower body 60 also has waste gas outlet 67, vitriol oil inlet 68 is arranged at tower body 60 tops, the middle and upper part has circulation slip 69 bottoms that enter the mouth that compressed air inlet 70 is arranged, take out slurry outlet 72, circulation slurry outlet 71,73,8 layers of grid shape of the conical distributor divider 74 that is of five storeys in the tower body 60, all material inlets all have shower nozzle.
Among Fig. 7, cylindrical tower body 75 is divided into extractive reaction section 77 and hydration reaction section 78 by dividing plate 76, give mixing tank 61 and pneumatic outlet 83 at 77 li tops of tower of extractive reaction section, give mixing tank 61 ground phosphate rock feed-pipe 79 is arranged, circulation dilute phosphoric acid import 80, expect fast setter 81 and mixed slurry shower nozzle 82, vitriol oil inlet 84 is arranged at extractive reaction section 77 tops, compressed air inlet 85, half water materials slurry outlet 86 is arranged at the bottom, and there are 2 layers of conical distributor 87 inside, 3 layers of grid shape divider 88,78 li of hydration reaction sections, waste gas outlet 89, half water material slurry inlets 90 are arranged at top, cycle stock slurry inlet 91, compressed air inlet 92 is arranged at the bottom, takes out slurry outlet 93, circulation slurry outlet 94,95,2 layers of conical distributor 96 of 2 layers of grid shape divider are arranged in the tower.All material inlets all have shower nozzle.
Aforesaid device material of main part is: OCr18Ni12MO2Ti, 1Cr18Ni12MO2TiOCr18Ni12MO3Ti, 1Cr18Ni12MO3Ti, A3 Steel Lining rubber or other acid corrosion-resistant material.
Claims (8)
1, a kind of tower Wet-process Phosphoric Acid Production method.Comprise ground phosphate rock and dilute phosphoric acid.Sulfuric acid reaction obtain phosphoric acid and phosphogypsum reaction slurry more after filtration, washing, it is characterized in that ground phosphate rock and dilute phosphoric acid mix earlier, carry out the first step chemical reaction in tempering tank 1
Above-mentioned slip input extraction tower 5 tops are mixed with the vitriol oil, carry out the second step chemical reaction:
Reaction slurry meets, mixes in the tower middle and upper part with from the circulation low temperature slip that has a large amount of two water thing crystal seeds at the bottom of the tower, and temperature is reduced to 70～75 ℃, CaSO by 95～98 ℃
41/2 H
2O carries out hydration reaction, generates CaSO
42H
2O.The pressurized air that at the bottom of tower, adds, through conical distributor and grid shape divider, from bottom to top with the reaction slurry countercurrent movement, make the slip uniform mixing, and and the heat exchange of slip mass transfer, reaction slurry keeps 50～55 ℃ of 70～75 ℃ → bottoms, 95～98 ℃ → middle and upper part, top, circulates to the tower middle and upper part as crystal seed from a slip part of taking out at the bottom of the tower, another part after filtration, the washing, obtain phosphoric acid and phosphogypsum.
2, equipment in the production method according to claim 1, it is characterized in that tempering tank 1 is the cylindrical seal device, one stirring arm 49 is arranged, the side has a taper shape to give mixing tank 52 on the cell body, ground phosphate rock feed-pipe 56 is arranged at its top, feed-pipe 56 is equipped with the fast setter 58 of material, and its side has circulation dilute phosphoric acid import 57, and giving the mixing tank bottom has the mixed slurry shower nozzle 59 that stretches in the tempering tank; Said extraction tower 5 tower bodies are cylindrical, the mixed slurry inlet 21 and vitriol oil inlet 22 tops at tower body of waste gas outlet 20 band shower nozzles are arranged at the top, circulation slip inlet 23 middle and upper parts at tower body, compressed air inlet 28 is arranged at the tower body bottom, take out slurry outlet 26 and circulation slurry outlet 27,24,4～8 layers of grid shape of 2～5 layers of conical distributor divider 25 is arranged in the tower.
3, equipment as claimed in claim 2 is characterized in that one deck dividing plate 30 can be adorned in the middle part of said extraction tower.
4, as claim 2,3 described equipment, it is characterized in that being provided with in the tempering tank 3 temperature test points, 3 liquid level test point are provided with 7 temperature test points, 7 liquid level test point in the extraction tower.
5, a kind of production method of tower phosphoric acid by wet process, comprise ground phosphate rock and dilute phosphoric acid, sulfuric acid reaction obtain phosphoric acid and gypsum as cement retarder slip more after filtration, washing, it is characterized in that ground phosphate rock and dilute phosphoric acid enter extraction tower and carry out following reaction with the vitriol oil after giving of extraction tower top mixed in the mixing tank:
The half water material slurry that obtains carries out hydration reaction as claimed in claim 1, circulation, crystalline growth and other process in extraction tower, obtain phosphoric acid and phosphogypsum.
6, give the extraction tower 13 of mixing tank as the band in the method as described in the claim 5, its tower body part extraction tower structure as claimed in claim 2, the top that it is characterized in that this extraction tower 13 has a taper shape to give mixing tank 18, give mixing tank 18 tops ground phosphate rock feed-pipe 663 is arranged, the fast setter 65 of material is housed on the feed-pipe 63, the side that gives mixing tank has circulation dilute phosphoric acid import 64, and the intravital mixed slurry shower nozzle 66 of extraction tower is stretched in the bottom.
7, band as claimed in claim 6 gives the extraction tower of mixing tank, it is characterized in that can adorning one deck division board 76 at the tower body middle part.
8, as claim 6,7 described equipment, it is characterized in that giving that 3 temperature test points being set in the tempering tank, 7 temperature test points are set, 7 liquid level test point in the extraction tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 91108059 CN1029517C (en) | 1991-10-24 | 1991-10-24 | Process and equipment for tower-type wet production of phosphoric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 91108059 CN1029517C (en) | 1991-10-24 | 1991-10-24 | Process and equipment for tower-type wet production of phosphoric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1062512A true CN1062512A (en) | 1992-07-08 |
| CN1029517C CN1029517C (en) | 1995-08-16 |
Family
ID=4908995
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 91108059 Expired - Fee Related CN1029517C (en) | 1991-10-24 | 1991-10-24 | Process and equipment for tower-type wet production of phosphoric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1029517C (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043521C (en) * | 1993-04-03 | 1999-06-02 | 刘传书 | Method and apparatus for tower wet production process of concentrated phosphoric acid |
| CN1055449C (en) * | 1996-01-05 | 2000-08-16 | 云南磷肥厂 | Out-reactor dilution of sulfuric acid in wet process producing phosphoric acid |
| CN1299976C (en) * | 2005-11-03 | 2007-02-14 | 华中师范大学 | Method of solvent extraction purification of wet method phosphoric acid produced from medium and low grade phosphosus ore |
| CN1317183C (en) * | 2005-12-23 | 2007-05-23 | 中国石化集团南京设计院 | Process for producing wet method phosphoric acid by medium low grade phosphorus mine |
| CN1321057C (en) * | 2005-02-01 | 2007-06-13 | 云南三环化工有限公司 | Improved wet dihydrate phosphoric acid producing process |
| CN101274755B (en) * | 2008-04-18 | 2010-10-13 | 侯炎学 | Device for wet phosphoric acid refining and high-purity ammonium molybdate preparation |
| CN102001636A (en) * | 2010-09-26 | 2011-04-06 | 四川大学 | Method for producing broad-concentration phosphoric acid and clean plaster by middle-low grade phosphorus ore wet process |
| CN102431980A (en) * | 2010-09-29 | 2012-05-02 | 朱寿连 | Method and equipment for preparing phosphoric acid |
| CN102534801A (en) * | 2012-02-23 | 2012-07-04 | 云南民族大学 | Method for improving quality of calcium sulfate whiskers |
| CN106927438A (en) * | 2017-04-18 | 2017-07-07 | 云南佳贝节能科技有限公司 | A kind of system of processing of phosphoric acid,diluted |
| CN112624175A (en) * | 2021-01-11 | 2021-04-09 | 宜都兴发化工有限公司 | Method for improving crystal form of phosphogypsum in wet-process phosphoric acid |
| CN115611260A (en) * | 2022-12-15 | 2023-01-17 | 中国科学院过程工程研究所 | Method for extracting micro-bubble reinforced phosphate rock acidolysis solution |
-
1991
- 1991-10-24 CN CN 91108059 patent/CN1029517C/en not_active Expired - Fee Related
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043521C (en) * | 1993-04-03 | 1999-06-02 | 刘传书 | Method and apparatus for tower wet production process of concentrated phosphoric acid |
| CN1055449C (en) * | 1996-01-05 | 2000-08-16 | 云南磷肥厂 | Out-reactor dilution of sulfuric acid in wet process producing phosphoric acid |
| CN1321057C (en) * | 2005-02-01 | 2007-06-13 | 云南三环化工有限公司 | Improved wet dihydrate phosphoric acid producing process |
| CN1299976C (en) * | 2005-11-03 | 2007-02-14 | 华中师范大学 | Method of solvent extraction purification of wet method phosphoric acid produced from medium and low grade phosphosus ore |
| CN1317183C (en) * | 2005-12-23 | 2007-05-23 | 中国石化集团南京设计院 | Process for producing wet method phosphoric acid by medium low grade phosphorus mine |
| CN101274755B (en) * | 2008-04-18 | 2010-10-13 | 侯炎学 | Device for wet phosphoric acid refining and high-purity ammonium molybdate preparation |
| CN102001636A (en) * | 2010-09-26 | 2011-04-06 | 四川大学 | Method for producing broad-concentration phosphoric acid and clean plaster by middle-low grade phosphorus ore wet process |
| CN102001636B (en) * | 2010-09-26 | 2012-07-25 | 四川大学 | Method for producing broad-concentration phosphoric acid and clean plaster by middle-low grade phosphorus ore wet process |
| CN102431980A (en) * | 2010-09-29 | 2012-05-02 | 朱寿连 | Method and equipment for preparing phosphoric acid |
| CN102431980B (en) * | 2010-09-29 | 2014-07-09 | 北京博大杰世环保节能技术服务有限公司 | Method and equipment for preparing phosphoric acid |
| CN102534801A (en) * | 2012-02-23 | 2012-07-04 | 云南民族大学 | Method for improving quality of calcium sulfate whiskers |
| CN106927438A (en) * | 2017-04-18 | 2017-07-07 | 云南佳贝节能科技有限公司 | A kind of system of processing of phosphoric acid,diluted |
| CN112624175A (en) * | 2021-01-11 | 2021-04-09 | 宜都兴发化工有限公司 | Method for improving crystal form of phosphogypsum in wet-process phosphoric acid |
| CN115611260A (en) * | 2022-12-15 | 2023-01-17 | 中国科学院过程工程研究所 | Method for extracting micro-bubble reinforced phosphate rock acidolysis solution |
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