CN107827114A - The method of phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid - Google Patents
The method of phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid Download PDFInfo
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- CN107827114A CN107827114A CN201711252756.5A CN201711252756A CN107827114A CN 107827114 A CN107827114 A CN 107827114A CN 201711252756 A CN201711252756 A CN 201711252756A CN 107827114 A CN107827114 A CN 107827114A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/08—Compounds containing halogen
- C01B33/10—Compounds containing silicon, fluorine, and other elements
- C01B33/103—Fluosilicic acid; Salts thereof
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/466—Conversion of one form of calcium sulfate to another
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- C—CHEMISTRY; METALLURGY
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Abstract
The present invention relates to phosphorous chemical industry technological development application field, specifically discloses a kind of method of the phosphorus co-production dihydrate gypsum reclaimed in wet-process phosphoric acid concentration slag acid and prodan, is added after wet-process phosphoric acid concentration slag acid is prepared in proportion with process water and turn brilliant groove；Crystal control agent will be turned again and a turn brilliant auxiliary agent is proportionally added into and turns the brilliant process of a brilliant groove progress semi-hydrated gypsum turn；Turn the slurry after crystalline substance terminates and enter the progress sedimentation separation of suspension separator；By suspension separator bottom discharge slurry is filtered, gypsum purifies, filtration washing obtains product dihydrate gypsum；By suspension separator top discharge slurry is filtered, prodan purifies, filtration washing obtains product prodan, gained filtrate can directly return to phosphorus ore extraction tank or phosphoric acid,diluted storage tank.The present invention realizes the value for phosphorus recovery and the comprehensive utilization of waste residue in wet-process phosphoric acid concentration slag acid, improving condensed slag acid, while technique is simple, and phosphorous recovery is high, and no waste residue produces, and economic benefit is obvious.
Description
The method of phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid.
Technical field
The present invention relates to phosphorous chemical industry technological development application field, and in particular to the phosphorus in recovery wet-process phosphoric acid concentration slag acid is simultaneously
The method of coproduction dihydrate gypsum and prodan.
Background technology
For Wet Processes of Phosphoric Acid mainly based on two water laws, phosphorus ore carries out dilute phosphorus of extractive reaction obtained 22~25% with sulfuric acid
Acid, then concentrated obtain 40~45% concentrated phosphoric acid.In concentration process, because the moisture in phosphoric acid,diluted is evaporated, phosphoric acid concentration carries
Height, cause to be dissolved in the supersaturation of the impurity in phosphoric acid and largely separate out, by the isolated concentrated phosphoric acid of natural subsidence and slag acid.Mesh
Before, slag acid amount is about the 10~15% of concentrated phosphoric acid yield caused by dihydrate wet phosphoric acid concentration process.The main component of slag acid is dense
Phosphoric acid, gypsum（Based on semi-hydrated gypsum）, villiaumite and a small amount of phosphate etc., solid content 40~60%, wherein liquid phase P2O5Content 40
~45%；Solid phase citric acid-soluble P2O5Content 2~4%, CaO content 20~25%, SO3Content 28~36%, Na2O contents 10~14%,
The contents 22~32% of SiF2- 6.
In phosphoric acid,diluted concentration process, not only dihydrate gypsum, which can be converted into, crystallizes tiny, a certain amount of intergranular phosphorus of entrainment（Solubility in citric acid
Phosphorus）Semi-hydrated gypsum, and the tiny villiaumite of crystal formation and phosphate can also separate out, cause in concentrated phosphoric acid solid phase settling efficiency it is low,
Slag acid yield is big, phosphoric acid loss is big, waste residue is difficult.
The purpose of the present invention is by after caused slag acid is handled by simple process during wet-process phosphoric acid concentration, reclaims phosphorus
Acid, acquisition crystallization is thick, uniform, is easy to the crystal of filtering or sedimentation separation, and reduces the intergranular phosphorus in crystal.Recovery
Phosphoric acid can be used for production high added value fine phosphate, the crystal of separation can be sold directly as product, so as to reduce
Influence caused by slag acid directly returns to Wet-process Phosphoric Acid Production system, improves device driving rate, improves the economic benefit of slag acid.
The content of the invention
It is an object of the invention to provide a kind of phosphorus co-production dihydrate gypsum and fluorine reclaimed in wet-process phosphoric acid concentration slag acid
The method of sodium metasilicate, in the prior art the method for slag acid treatment have：Slag acid is directly returned into rubble cream filtration system, easily blocked
Filter cloth, filtration system is caused to paralyse；Slag acid directly returns to phosphorus ore extraction tank, and temperature is in a slight decrease in course of conveying to separate out
Villiaumite so that induction system fouling severe obstruction；Slag acid filtration system is separately provided, but slag acid viscosity is big, solid phase crystal formation is thin
It is small, poor filtration effect；Using slag acid as raw material, produce other products such as chemical fertilizer, not only utilization rate is low and slag it is sour in impurity it is equal
It is enriched in fertilizer, is finally applied to soil, pollute environment.The purpose of the application is exactly to solve prior art processing phosphoric acid by wet process
The above mentioned problem run into during condensed slag acid.
To solve above-mentioned technical problem, the present invention uses following technical scheme：
A kind of method of the phosphorus co-production dihydrate gypsum reclaimed in wet-process phosphoric acid concentration slag acid and prodan, including：
Step a：Crystal modifier is added into the mixture of slag acid and water and carries out the brilliant process of semi-hydrated gypsum turn, obtains slurry A；
Step b：Sedimentation separation is carried out to slurry A using suspension separator, material is used as from the slurry of suspension separator bottom discharge
B is starched, the slurry discharged from suspension separator top is as slurry C；
Step c：Slurry B is filtered, carrying out gypsum to obtained filter residue D purifies to obtain dihydrate gypsum；The filtrate that will be obtained
Return to phosphorus ore extraction tank or phosphoric acid,diluted storage tank；
Step d：Slurry C is filtered, carrying out prodan to obtained filter residue E purifies to obtain prodan；By what is obtained
Filtrate returns to phosphorus ore extraction tank or phosphoric acid,diluted storage tank.
Slag acid includes liquid phase P in the present invention2O5, solid phase P2O5、CaO、Na2O content 10~14%, and SiF2- 6, in order to carry
The utilization rate of concentrated phosphoric acid in high slag acid, and the comprehensive utilization of waste residue is realized, no discarded object produces, and turns brilliant, waste residue by slag acid
Separation and purification production dihydrate gypsum and prodan, improve its added value.
As preferable, the mass ratio of slag acid and water is 1 in the mixture：0.5~1.5.
As preferable, the crystal modifier includes turning crystal control agent and turns a brilliant auxiliary agent.
Under the process water additional proportion of optimization, add and turn crystal control agent and turn brilliant auxiliary agent, compared with temperate condition
Realize this turn of brilliant process.
As preferable, the crystal control agent that turns is to account for 1.5~5.5% concentrated sulfuric acid of slag acid quality, account for slag acid quality
1~2% calcium sulphate dihydrate or the one or more accounted in 8~12% fluosilicic acid of slag acid quality.
During turning brilliant, sulfuric acid and calcium sulphate dihydrate turn crystal control agent as semi-hydrated gypsum, add sulfuric acid adjustment liquid phase
Sulfur trioxide concentration, suppresses the dissolving of dihydrate gypsum, and with the Ca in liquid phase2+With reference to generation dihydrate gypsum；Add a small amount of two water
Calcium sulfate promotes semi-hydrated gypsum to turn the brilliant dihydrate gypsum thick for particle diameter as crystal seed in the presence of brilliant auxiliary agent is turned, and
The phosphorus that eutectic substitutes in semi-hydrated gypsum is discharged, reduces the phosphorus content of product dihydrate gypsum.Fluosilicic acid presses down as crystal control agent is turned
The dissolving of prodan in slurry processed, reduce the content for returning to sodium oxide molybdena in filtrate.
It is Diammonium phosphate (DAP), DBSA triethanolamine, ethoxylation alkane as preferable, the described brilliant auxiliary agent that turns
One or more in base sodium sulfate salt, sodium sulfate of polyethenoxy ether of fatty alcohol salt, the described brilliant auxiliary agent that turns account for slag acid quality
0.005~0.01%.
As preferable, the brilliant temperature that turns that semi-hydrated gypsum turns brilliant process in step a is 55~65 DEG C, and stirring linear velocity is
0.6~0.9m/s, it is 90~120min to turn the brilliant time.
During turning brilliant, controlling reaction temperature, mixing speed and reaction time are needed, under the control condition of the present invention,
Dihydrate gypsum well-crystallized, is easily isolated.
As preferable, the charging aperture of the suspension separator is located in the middle part of guide shell, the position taper of suspension separator bottom
Or it is circular, agitating paddle is double-deck press-down type, and top discharge mouth uses overflow discharge.
As preferable, the stirring linear velocity during sedimentation separation is 0.5~0.7m/s, the residence time 120~
150min。
As preferable, the gypsum purification is by filter residue D and water in mass ratio 1：1~2 mixing, adds sulphur thereto
The pH value of one or more of regulation materials in acid, hydrochloric acid, nitric acid, phosphoric acid or fluosilicic acid is 3~7, in 60~90 DEG C of bars of temperature
30~60min is purified under part.
The present invention carries out separation of solid and liquid using flotation separator to turning brilliant slurry, because dihydrate gypsum crystallizes during turning brilliant
It is thick, after being mixed by the suspension separator upper back discharge filtered obtained filter residue of slurry with water, using sulfuric acid, hydrochloric acid, nitre
The pH value 3~7 of one kind and above regulation Gypsum slurry in acid, phosphoric acid, fluosilicic acid, it is miscellaneous that purification removes prodan therein
Matter, filtration washing can obtain dihydrate gypsum, and product purity can reach natural gypsum superfine standard.
As preferable, prodan purification is by filter residue E and water in mass ratio 1：1~4 mixing, add account for filter thereto
The cleanser of slag E mass 0.1~1%, 30~60min is then purified under the conditions of 60~90 DEG C of temperature, the cleanser is chlorination
One or more in ammonium, ammonium sulfate, MAP, Diammonium phosphate (DAP), ammonium acetate or ammonium hydrogen carbonate.
Separation of solid and liquid is carried out to turning brilliant slurry using flotation separator, because prodan crystal grain is tiny, by outstanding
After the floating separator upper back discharge filtered obtained filter residue of slurry mixes with water, addition ammonium chloride, ammonium sulfate, MAP,
One kind in Diammonium phosphate (DAP), ammonium acetate, ammonium hydrogen carbonate and more than, purification removes gypsum impurity therein, and filtration washing can obtain
To the prodan of certified products standard.
Compared with prior art, beneficial effects of the present invention are at least one of following：
（1）The present invention proposes the new method of the recovery of phosphorus and waste residue comprehensive utilization in a kind of wet-process phosphoric acid concentration slag acid, not only will
The phosphorus product of phosphoric acid remanufacture high added value in slag acid, and coproduction dihydrate gypsum and prodan, breach existing skill
Slag acid is used to produce the relatively low fertilizer of added value by art, and the objectionable impurities in slag acid can be also applied to soil with fertilizer,
Pollute the Nature.
（2）The phosphor resource in slag acid can be reclaimed using this method while produces dihydrate gypsum and prodan, it is main logical
Gypsum rotating crystal process in control slag acid is crossed, semi-hydrated gypsum can be converted into and crystallize thick dihydrate gypsum, and can be by gypsum
In solubility in citric acid intergranular phosphorus be converted into water-soluble phosphorus, reach improve slag acid in phosphorous recovery purpose.
（3）After turning brilliant, the crystal grain of solid content is thick in slag acid, improves the strainability of slurry.Two after purification
Water gypsum purity and whiteness exceed well over ardealite primary standard, can be as the raw material of production plaster of Paris；Prodan purity
Up to certified products standard, product can be used as to sell, increased economic efficiency.
（4）Technique provided by the invention mainly includes a turn brilliant, separation, purification can obtain product, and flow is short, equipment requirement
Simply, invest low with running cost.
（5）The present invention realizes the efficient utilization to wet phosphoric acid by dihydrate condensed slag acid, improves its added value, economy effect
It is beneficial obvious, and filtrate can be recycled with return system, and no waste residue, waste gas produce, and realize clean manufacturing.
Brief description of the drawings
Fig. 1 is the method for the phosphorus co-production dihydrate gypsum and prodan in present invention recovery wet-process phosphoric acid concentration slag acid
Flow chart.
Embodiment
In order to make the purpose , technical scheme and advantage of the present invention be clearer, it is right below in conjunction with drawings and Examples
The present invention is further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, and
It is not used in the restriction present invention.
Embodiment 1：
The composition of the raw material wet-process phosphoric acid concentration slag acid used in the present embodiment is as follows：
Wet-process phosphoric acid concentration slag acid and the water in mass ratio 1 of These parameters:0.5 prepares, and is added to and turns in brilliant groove.Then slag is added
The concentrated sulfuric acid, 1% calcium sulphate dihydrate, 8% fluosilicic acid of acid amount 1.5%, 0.005% Diammonium phosphate (DAP), turn brilliant 55 DEG C of temperature, stirring
Linear velocity 0.7m/s, turn the brilliant 120 minutes time.Turn after crystalline substance terminates, material enters suspension separator, and stirring linear velocity is 0.5m/
S, residence time of material 120 minutes.The filter residue for being separated by filtration to obtain by suspension separator bottom discharge slurry is with water by 1：1 is mixed
Close, Gypsum slurry pH most 3 is adjusted using sulfuric acid, purification temperature is 90 DEG C, and the clarification time is 60 minutes, and filtration washing is produced
Product dihydrate gypsum.The filter residue for being separated by filtration to obtain by suspension separator top discharge slurry is with water by 1：1 mixing, adds filter residue
The ammonium chloride of quality 0.1%, purification temperature are 60 DEG C, and the clarification time is 60 minutes, and filtration washing obtains product prodan.Two
Water gypsum purity 98.6%, P2O5Content 0.09%；Prodan purity 97.4%；Phosphrus reagent is 99.85%.
Embodiment 2
The composition of the raw material wet-process phosphoric acid concentration slag acid used in the present embodiment is as follows：
Wet-process phosphoric acid concentration slag acid and the water in mass ratio 1 of These parameters:1 prepares, and is added to and turns in brilliant groove.Then slag acid is added
The concentrated sulfuric acid, 2% calcium sulphate dihydrate, 12% fluosilicic acid of amount 3%, 0.005% ethoxylated alkyl sulfate salt, 0.01%
Sodium sulfate of polyethenoxy ether of fatty alcohol salt, turn brilliant temperature 60 C, stir linear velocity 0.8m/s, turn the brilliant 110 minutes time.Turn brilliant knot
Shu Hou, material enter suspension separator, and stirring linear velocity is 0.6m/s, residence time of material 140 minutes.By suspension separator bottom
The filter residue that portion's discharge slurry is separated by filtration to obtain is with water by 1：1.2 mixing, Gypsum slurry pH most 4 is adjusted using hydrochloric acid, only
It is 70 DEG C to change temperature, and the clarification time is 35 minutes, and filtration washing obtains product dihydrate gypsum.Discharged and expected by suspension separator top
The filter residue for being separated by filtration to obtain is starched with water by 1：2 mixing, add the ammonium sulfate of filter residue quality 1%, 0.5% MAP, purification
Temperature is 80 DEG C, and the clarification time is 50 minutes, and filtration washing obtains product prodan.Dihydrate gypsum purity 98.1%, P2O5Contain
Amount 0.07%；Prodan purity 97.3%；Phosphrus reagent is 99.88%.
Embodiment 3
The composition of the raw material wet-process phosphoric acid concentration slag acid used in the present embodiment is as follows：
Wet-process phosphoric acid concentration slag acid and the water in mass ratio 1 of These parameters:1.2 prepare, and are added to and turn in brilliant groove.Then slag is added
The concentrated sulfuric acid, 1.5% calcium sulphate dihydrate of acid amount 4%, 0.01% Diammonium phosphate (DAP), 0.01% ethanol of DBSA three
Amine, turn brilliant 55 DEG C of temperature, stir linear velocity 0.8m/s, turn the brilliant 100 minutes time.Turn after crystalline substance terminates, material, which enters to suspend, to be separated
Device, stirring linear velocity are 0.6m/s, residence time of material 130 minutes.It is separated by filtration by suspension separator bottom discharge slurry
Obtained filter residue is with water by 1：1.6 mixing, Gypsum slurry pH most 5 is adjusted using nitric acid, purification temperature is 85 DEG C, the clarification time
For 45 minutes, filtration washing obtained product dihydrate gypsum.The filter for being separated by filtration to obtain by suspension separator top discharge slurry
Slag presses 1 with water：3 mixing, the Diammonium phosphate (DAP) of filter residue quality 1%, 0.05% ammonium hydrogen carbonate are added, purification temperature is 40 DEG C, purification
Time is 60 minutes, and filtration washing obtains product prodan.Dihydrate gypsum purity 98.5%, P2O5Content 0.11%；Prodan
Purity 97.9%；Phosphrus reagent is 99.82%.
Embodiment 4
The composition of the raw material wet-process phosphoric acid concentration slag acid used in the present embodiment is as follows：
Wet-process phosphoric acid concentration slag acid and the water in mass ratio 1 of These parameters:1.5 prepare, and are added to and turn in brilliant groove.Then slag is added
The concentrated sulfuric acid of acid amount 5.5%, 0.01% DBSA triethanolamine, 0.01% ethoxylated alkyl sulfate salt,
0.01% sodium sulfate of polyethenoxy ether of fatty alcohol salt, turn brilliant 65 DEG C of temperature, stir linear velocity 0.9m/s, turn the brilliant 90 minutes time.
Turn after crystalline substance terminates, material enters suspension separator, and stirring linear velocity is 0.7m/s, residence time of material 150 minutes.Divided by suspending
The filter residue and water for being separated by filtration to obtain from device bottom discharge slurry are by 1：2 mixing, Gypsum slurry pH is adjusted most using phosphoric acid
6, purification temperature is 60 DEG C, and the clarification time is 30 minutes, and filtration washing obtains product dihydrate gypsum.Arranged by suspension separator top
Go out filter residue that slurry is separated by filtration to obtain with water by 1：4 mixing, add the ammonium acetate of filter residue quality 0.5%, 0.5% bicarbonate
Ammonium, purification temperature are 90 DEG C, and the clarification time is 30 minutes.Filtration washing obtains product prodan.Dihydrate gypsum purity
98.5%, P2O5Content 0.1%；Prodan purity 98.2%；Phosphrus reagent is 99.83%.
Although reference be made herein to invention has been described for multiple explanatory embodiments of the invention, however, it is to be understood that
Those skilled in the art can be designed that a lot of other modifications and embodiment, and these modifications and embodiment will fall in this Shen
Please be within disclosed spirit and spirit.More specifically, can in the range of disclosure, drawings and claims
A variety of variations and modifications are carried out with the building block to theme combination layout and/or layout.Except to building block and/or layout
Outside the modification and improvement of progress, to those skilled in the art, other purposes also will be apparent.
Claims (10)
1. a kind of method of phosphorus co-production dihydrate gypsum reclaimed in wet-process phosphoric acid concentration slag acid and prodan, its feature exist
In：Including：
Step a：Crystal modifier is added into the mixture of slag acid and water and carries out the brilliant process of semi-hydrated gypsum turn, obtains slurry A；
Step b：Sedimentation separation is carried out to slurry A using suspension separator, material is used as from the slurry of suspension separator bottom discharge
B is starched, the slurry discharged from suspension separator top is as slurry C；
Step c：Slurry B is filtered, carrying out gypsum to obtained filter residue D purifies to obtain dihydrate gypsum；The filtrate that will be obtained
Return to phosphorus ore extraction tank or phosphoric acid,diluted storage tank；
Step d：Slurry C is filtered, carrying out prodan to obtained filter residue E purifies to obtain prodan；By what is obtained
Filtrate returns to phosphorus ore extraction tank or phosphoric acid,diluted storage tank.
2. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that the mass ratio of slag acid and water is 1 in the mixture：0.5~1.5.
3. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that the crystal modifier includes turning crystal control agent and turns brilliant auxiliary agent.
4. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 3
Method, it is characterised in that it is described turn crystal control agent be account for 1.5~5.5% concentrated sulfuric acid of slag acid quality, account for slag acid quality 1~
2% calcium sulphate dihydrate or the one or more accounted in 8~12% fluosilicic acid of slag acid quality.
5. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 3
Method, it is characterised in that the described brilliant auxiliary agent that turns is Diammonium phosphate (DAP), DBSA triethanolamine, ethoxylated alkyl
One or more in sodium sulfate salt, sodium sulfate of polyethenoxy ether of fatty alcohol salt, the described brilliant auxiliary agent that turns account for slag acid quality
0.005~0.01%.
6. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that the brilliant temperature that turns that semi-hydrated gypsum turns brilliant process is 55~65 DEG C, and stirring linear velocity is 0.7~0.9m/s,
It is 90~120min to turn the brilliant time.
7. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that the charging aperture of the suspension separator is located in the middle part of guide shell, the position taper of suspension separator bottom or circle
Shape, agitating paddle are double-deck press-down type, and top discharge mouth uses overflow discharge.
8. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that the stirring linear velocity during sedimentation separation is 0.5~0.7m/s, 120~150min of residence time.
9. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that the gypsum purification is by filter residue D and water in mass ratio 1：1~2 mixing, adds sulfuric acid, salt thereto
The pH value of one or more of regulation materials in acid, nitric acid, phosphoric acid or fluosilicic acid are 3~7, net under the conditions of 60~90 DEG C of temperature
Change 30~60min.
10. phosphorus co-production dihydrate gypsum and prodan in recovery wet-process phosphoric acid concentration slag acid according to claim 1
Method, it is characterised in that prodan purification is by filter residue E and water in mass ratio 1：1~4 mixing, add account for filter thereto
The cleanser of slag E mass 0.1~1%, 30~60min is then purified under the conditions of 60~90 DEG C of temperature, the cleanser is chlorination
One or more in ammonium, ammonium sulfate, MAP, Diammonium phosphate (DAP), ammonium acetate or ammonium hydrogen carbonate.
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| CN109231863A (en) * | 2018-10-18 | 2019-01-18 | 洛阳理工学院 | A kind of compound crystal modifier being used to prepare alpha type high-strength gypsum |
| CN111689875A (en) * | 2020-07-07 | 2020-09-22 | 中化云龙有限公司 | Method for producing feed-grade urea phosphate by using wet-process phosphoric acid residues |
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| CN107140614A (en) * | 2017-05-16 | 2017-09-08 | 云南胜威化工有限公司 | Method to improve concentrator driving rate is pre-processed to wet dilute phosphoric acid |
| CN107140614B (en) * | 2017-05-16 | 2019-11-29 | 云南胜威化工有限公司 | Method to improve concentrator driving rate is pre-processed to wet dilute phosphoric acid |
| CN109231863A (en) * | 2018-10-18 | 2019-01-18 | 洛阳理工学院 | A kind of compound crystal modifier being used to prepare alpha type high-strength gypsum |
| CN109231863B (en) * | 2018-10-18 | 2021-10-01 | 洛阳理工学院 | Composite crystal transformation agent for preparing alpha-type high-strength gypsum |
| CN111689875A (en) * | 2020-07-07 | 2020-09-22 | 中化云龙有限公司 | Method for producing feed-grade urea phosphate by using wet-process phosphoric acid residues |
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