CN110371939A - A kind of preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate - Google Patents
A kind of preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate Download PDFInfo
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- CN110371939A CN110371939A CN201910684680.6A CN201910684680A CN110371939A CN 110371939 A CN110371939 A CN 110371939A CN 201910684680 A CN201910684680 A CN 201910684680A CN 110371939 A CN110371939 A CN 110371939A
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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
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/18—Phosphoric acid
- C01B25/234—Purification; Stabilisation; Concentration
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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
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/18—Phosphoric acid
- C01B25/234—Purification; Stabilisation; Concentration
- C01B25/237—Selective elimination of impurities
- C01B25/238—Cationic impurities, e.g. arsenic compounds
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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
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/28—Ammonium phosphates
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The present invention relates to a kind of preparation methods of Diammonium phosphate (DAP) based on phosphoric acid raffinate.Its technical solution is: by phosphoric acid raffinate: the mass ratio of water is 1: (0.1~0.3) adds water in phosphoric acid raffinate, stirs 0.5~1h, the phosphoric acid raffinate after being diluted；By urea: the mass ratio of the phosphoric acid raffinate after dilution is (0.5~2) ︰ 1, urea is added in the phosphoric acid raffinate after dilution, stirring to pH value is 6~7 under the conditions of 70~100 DEG C, is separated by solid-liquid separation to get purified phosphoric acid raffinate and removal of impurities slag；Removal of impurities slag is washed with water, the removal of impurities slag and washing water after being washed；Washing water return step one is for diluting phosphoric acid raffinate；The purified phosphoric acid raffinate is concentrated into P2O5Content is 40~50wt%, then passes to tubular reactor, and control degree of neutralization is 1.8~2.0, obtains the Diammonium phosphate (DAP) based on phosphoric acid raffinate.The present invention has the characteristics that good operational environment, easily filtering is low with dedoping step phosphorus loss late while not introducing new impurity.
Description
Technical field
The invention belongs to phosphoric acid raffinate technical fields.More particularly to a kind of system of Diammonium phosphate (DAP) based on phosphoric acid raffinate
Preparation Method.
Background technique
Wet-process phosphoric acid (WPPA) energy consumption is lower, and adaptability to raw material is strong, is widely used to the preparation of different phosphorus products.But wet
A large amount of impurity such as Fe, Al, Mg plasma enters leachate with phosphorus in method extraction process, leads to the phosphorus and foreign ion of subsequent technique
Separation is difficult.It is wide in recent years due to the advantage that the solvent extraction technology in Wet-process phosphoric acid (WPPA) is high-efficient with its, selectivity is good
The general preparation applied to high-purity phosphoric acid.Though the solvent extraction technology has significant economic benefit, there are still following two
A main problem: being enriched with first is that extraction process phosphorus is extracted with foreign ion, and phosphoric acid raffinate viscosity is very big, is occurred a large amount of
Gelatinous precipitate causes to filter extremely difficult；Second is that still containing certain density phosphorus in phosphoric acid raffinate, it is commonly used to produce agricultural
Monoammonium phosphate or Diammonium phosphate (DAP), but the impurity ion contents such as Fe, Al, Mg are very high, the phosphorus product for causing subsequent technique to prepare
Purity is not up to standard.
" the raffinate method that neutralisation prepares industrial grade monoammonium phosphate twice " (CN103896232 A) patented technology and old
Abiding by road etc., (the raffinate such as Chen Zunkui prepares the work of industrial grade monoammonium phosphate using ammonia neutralisation processing twice phosphoric acid raffinate
Skill optimizes [J], chemistry and bioengineering, 2015,32 (08), 63~66), PHOSPHORIC ACID TECH.GRADE one is finally prepared using crystallisation
Ammonium: high viscosity raffinate is diluted first；The phosphoric acid raffinate first time ammonia after dilution is neutralized again, first time ammonia
The terminal pH of neutralization is 3.4~3.6, is filtered after curing；Then second of ammonia neutralization, the terminal that second of ammonia neutralizes are carried out
PH is 4.4~4.6, is filtered after curing；Monoammonium phosphate is finally made using concentrated crystallization.The technique uses conventional nertralizer-
Ammonia handles phosphoric acid raffinate phosphoric acid, and impurity-eliminating effect is preferable, but there are still following three problems: first is that dedoping step generates a large amount of glue
Shape sediment is difficult to filter；Second is that phosphorus loss is big, 25~30% are commonly reached；Third is that being cleaned using ammonia, operating process is difficult to
Avoid ammonia from the evolution in reactor, laboratory and industry spot operating environment are poor.
" with the method for raffinate production industrial monoammonium phosphate coproduction fertilizer grade monoammonium phosphate " (102674284 A of CN) is special
Sharp technology, the technology first remove impurity using the ammonia precipitation method under the action of silicon fluoride, ammonium fluoride, then with purified raffinate
Acid preparation monoammonium phosphate.The technique introduces fluoride as precipitating reagent and removes impurity, but in addition fluoride ion removing impurity
New impurity fluorine is introduced simultaneously.In addition, the technique that there are phosphorus losses is big, operating environment is poor, gelatinous precipitate is difficult to filter and
Phosphorus is difficult to the shortcomings that recycling.
" utilizing the method for raffinate production granular monoammonium phosphate " (101891504 A of CN) patented technology, which will be high
The phosphoric acid by wet process of concentration is mixed with phosphoric acid raffinate, to reduce impurity ion content in phosphoric acid raffinate, final obtained qualification
Monoammonium phosphate.The technique needs to be incorporated to the restricted larger of raw material when impurity ion content increases in phosphoric acid raffinate
Phosphoric acid by wet process amount can also increase with it, and cause to prepare agricultural grade monoammonium phosphate, production with the phosphoric acid by wet process of a large amount of high added value
It is at high cost.
" with the method for the raffinate production Diammonium phosphate (DAP) of purifying phosphoric acid " (101613094 A of CN) patented technology, the technology
First the phosphoric acid by wet process of high concentration is mixed according to a certain percentage with phosphoric acid raffinate, and surfactant is added thereto to improve
The mobility of mixed acid reduces viscosity.According still further to conventional method, in ammonia and complex acid, Diammonium phosphate (DAP) is made.This technique is by table
Phosphoric acid by wet process is added in face activating agent, but the surfactant only has the function of reducing viscosity, sediment is made to be easier to filtering, and
Foreign ion cannot be removed.
In conclusion existing phosphoric acid raffinate processing technique is primarily present, operating environment is poor, the sad filter of sediment, phosphorus damage
Mistake rate height and there is new impurity the technological deficiencies such as to introduce.
Summary of the invention
The present invention is directed to overcome prior art defect, it is therefore an objective to provide a kind of good operational environment, sediment easily filters, phosphorus damage
Mistake rate is low and does not introduce the preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate of new impurity.
To achieve the above object, the technical solution adopted by the present invention comprises the concrete steps that:
Step 1: dilution
By phosphoric acid raffinate: the mass ratio of water is 1: (0.1~0.3) water is added in the phosphoric acid raffinate,
0.5~1h, the phosphoric acid raffinate after being diluted are stirred under normal temperature condition.
Step 2: precipitating
By urea: the mass ratio of the phosphoric acid raffinate after the dilution is that (0.5~2) ︰ 1, will be described in urea addition
In phosphoric acid raffinate after dilution, stirring to pH value is 6~7 under the conditions of 70~100 DEG C, is separated by solid-liquid separation to get purified
Phosphoric acid raffinate and removal of impurities slag.
Step 3: washing
The removal of impurities slag is used into water washing, removal of impurities slag and washing water after being washed；The washing water return step
One for diluting phosphoric acid raffinate.
Step 4: preparation Diammonium phosphate (DAP)
The purified phosphoric acid raffinate is concentrated into P2O5Content is 40~50wt%, then passes to tubular reactor,
Controlling degree of neutralization is 1.8~2.0, obtains the Diammonium phosphate (DAP) based on phosphoric acid raffinate.
The phosphoric acid raffinate: P2O5Content > 35wt%, content of MgO are 2~8wt%, Al2O3Content is 4~8wt%,
Fe2O3Content is 0.5~3wt%, CaO content < 0.05wt%, K2O content < 0.1wt%, Na2O content < 1.5wt%, solid content
For 4~8wt%, pH value is less than -0.8；The density of phosphoric acid raffinate clear liquid is greater than 1.6g/cm3。
Due to the adoption of the above technical scheme, the present invention has following good effect compared with prior art:
(1) urea is added at one time by the present invention, can be to the removal effect that various metals ion has had, wherein iron, aluminium
Impurities removing efficiency reaches 98% or more, and the impurities removing efficiency of magnesium reaches 90% or more；
(2) urea can effectively prevent co-precipitation as slow release precipitator, targetedly remove in phosphoric acid raffinate
Iron, aluminium, magnesium ion, it is therefore prevented that phosphorus is mingled with, and the sediment generated is in powdery, and it is gluey to avoid existing ammonium hydroxide purification process
The loss late of the generation of sediment, phosphorus can be reduced to 5% or less.
In the present invention, urea will be slow release ammonia being heated to 60 DEG C or more:
CO(NH2)2+H2O→CO2↑+2NH3
NH3+H2O→NH4 ++OH-
The obtained product NH of urea hydrothermal decomposition4 +It is the subsequent reactant for preparing ammonium phosphate salt product, and the reaction is raw
At OH-The promotion for then facilitating pH value of solution is finally reached the optimum PH range of contamination precipitation in phosphoric acid raffinate.In addition, control
Condition processed decomposes urea slowly, uniformly discharges OH in the solution-, can prevent conventional ammonium hydroxide from adjusting local ph mistake in pH method
Winding that is high and leading to phosphorus caused by the intense hydrolysis of the part Fe, Al.
The surface topography of removal of impurities slag of the invention and existing ammonium hydroxide removal of impurities slag surface topography are compared, as a result as schemed
Shown in 1 and Fig. 2.Fig. 1 is a kind of surface topography SEM figure of removal of impurities slag of the invention；Fig. 2 is the table of existing ammonium hydroxide removal of impurities product
Face pattern SEM figure.As shown in Figure 1, the present invention product that cleans is that flake stacks, structural integrity is consistent, it was demonstrated that urea precipitation
Product crystallinity is high；As shown in Figure 2, existing ammonium hydroxide removal of impurities product sheet granularity is smaller, in irregular shape, easily formation bulky grain
Reunite；By the comparison of Fig. 1 and Fig. 2 it is found that urea removal of impurities product of the invention is compared to existing ammonium hydroxide removal of impurities product, pattern is more
To be complete uniform, crystalline size is bigger, and useful element phosphorus is not easy to lose in Fe, Al, Mg precipitation process.
(3) process object of the invention is muddy phosphoric acid raffinate, directly cleans, is not required to muddy phosphoric acid raffinate
Gelatinous precipitate in filtering phosphoric acid raffinate is just able to achieve the purification to raffinate, the sediment knot generated on a microscopic level
Brilliant degree is high, and crystallite dimension is big, and in fine-powdered, (and the removal of impurities slag that existing removal of impurities mode obtains is in glue to particle on a macroscopic level
Shape), and the muddy object in phosphoric acid raffinate reacts in dedoping step with precipitating reagent, so that filter process is easier to carry out, shortens
Process flow.
(4) as described in this good effect (2), urea will be slow release ammonia being heated to 60 DEG C or more:
CO(NH2)2+H2O→CO2↑+2NH3
NH3+H2O→NH4 ++OH-
Urea, which decomposes, generates ammonia and carbon dioxide, will not introduce new impurity, Diammonium phosphate (DAP) obtained while removal of impurities
Product reaches the requirement of national standard " monoammonium phosphate, Diammonium phosphate (DAP) " (GB 10205-2009).
Therefore, the present invention has good operational environment, easily filters low with dedoping step phosphorus loss late while not introducing new impurity
The advantages of.
Detailed description of the invention
Fig. 1 is a kind of surface topography SEM figure of removal of impurities slag of the invention；
Fig. 2 is the surface topography SEM figure of the ammonium hydroxide removal of impurities product of the prior art.
Specific embodiment
The present invention will be further described With reference to embodiment, not to the limitation of its protection scope.
In present embodiment:
The phosphoric acid raffinate: P2O5Content > 35wt%, content of MgO are 2~8wt%, Al2O3Content is 4~8wt%,
Fe2O3Content is 0.5~3wt%, CaO content < 0.05wt%, K2O content < 0.1wt%, Na2O content < 1.5wt%, solid content
For 4~8wt%, pH value is less than -0.8；The density of phosphoric acid raffinate clear liquid is greater than 1.6g/cm3。
It is repeated no more in embodiment.
Embodiment 1
A kind of preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate.The present embodiment the method comprises the concrete steps that:
Step 1: dilution
By phosphoric acid raffinate: the mass ratio of water is 1: (0.1~0.15) water is added in the phosphoric acid raffinate,
0.5~0.7h, the phosphoric acid raffinate after being diluted are stirred under normal temperature conditions.
Step 2: precipitating
By urea: the mass ratio of the phosphoric acid raffinate after the dilution is that (0.5~1) ︰ 1, will be described in urea addition
In phosphoric acid raffinate after dilution, stirring to pH value is 6~6.4 under the conditions of 70~80 DEG C, is separated by solid-liquid separation to get purified
Phosphoric acid raffinate and removal of impurities slag.
Step 3: washing
The removal of impurities slag is used into water washing, removal of impurities slag and washing water after being washed；The washing water return step
One for diluting phosphoric acid raffinate.
Step 4: preparation Diammonium phosphate (DAP)
The purified phosphoric acid raffinate is concentrated into P2O5Content is 40~44wt%, then passes to tubular reactor,
Controlling degree of neutralization is 1.8~2.0, and the Diammonium phosphate (DAP) based on phosphoric acid raffinate is made.The obtained phosphorus based on phosphoric acid raffinate
Sour diammonium product reaches the requirement of national standard " monoammonium phosphate, Diammonium phosphate (DAP) " (GB 10205-2009).
Embodiment 2
A kind of preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate.The present embodiment the method comprises the concrete steps that:
Step 1: dilution
By phosphoric acid raffinate: the mass ratio of water is 1: (0.1~0.2) water is added in the phosphoric acid raffinate,
0.6~0.8h, the phosphoric acid raffinate after being diluted are stirred under normal temperature condition.
Step 2: precipitating
By urea: the mass ratio of the phosphoric acid raffinate after the dilution is that (1~1.5) ︰ 1, will be described in urea addition
In phosphoric acid raffinate after dilution, stirring to pH value is 6.2~6.6 under the conditions of 80~90 DEG C, after being separated by solid-liquid separation to get purification
Phosphoric acid raffinate and removal of impurities slag.
Step 3: washing
The removal of impurities slag is used into water washing, removal of impurities slag and washing water after being washed；The washing water return step
One for diluting phosphoric acid raffinate.
Step 4: preparation Diammonium phosphate (DAP)
The purified phosphoric acid raffinate is concentrated into P2O5Content is 43~47wt%, then passes to tubular reactor,
Controlling degree of neutralization is 1.8~2.0, and the Diammonium phosphate (DAP) based on phosphoric acid raffinate is made.The obtained phosphorus based on phosphoric acid raffinate
Sour diammonium product reaches the requirement of national standard " monoammonium phosphate, Diammonium phosphate (DAP) " (GB 10205-2009).
Embodiment 3
A kind of preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate.The present embodiment the method comprises the concrete steps that:
Step 1: dilution
By phosphoric acid raffinate: the mass ratio of water is 1: (0.2~0.3) water is added in the phosphoric acid raffinate,
0.8~1h, the phosphoric acid raffinate after being diluted are stirred under normal temperature condition.
Step 2: precipitating
By urea: the mass ratio of the phosphoric acid raffinate after the dilution is that (1.5~2) ︰ 1, will be described in urea addition
In phosphoric acid raffinate after dilution, stirring to pH value is 6.6~7 under the conditions of 90~100 DEG C, after being separated by solid-liquid separation to get purification
Phosphoric acid raffinate and removal of impurities slag.
Step 3: washing
The removal of impurities slag is used into water washing, removal of impurities slag and washing water after being washed；The washing water return step
One for diluting phosphoric acid raffinate.
Step 4: preparation Diammonium phosphate (DAP)
The purified phosphoric acid raffinate is concentrated into P2O5Content is 46~50wt%, then passes to tubular reactor,
Controlling degree of neutralization is 1.8~2.0, and the Diammonium phosphate (DAP) based on phosphoric acid raffinate is made.The obtained phosphorus based on phosphoric acid raffinate
Sour diammonium product reaches the requirement of national standard " monoammonium phosphate, Diammonium phosphate (DAP) " (GB 10205-2009).
Present embodiment has following good effect compared with prior art:
(1) urea is added at one time by present embodiment, to the removal effect that various metals ion has had,
In, iron, aluminium impurities removing efficiency are up to 98% or more, and the impurities removing efficiency of magnesium is up to 90% or more；
(2) urea can effectively prevent co-precipitation as slow release precipitator, targetedly remove in phosphoric acid raffinate
Iron, aluminium, magnesium ion, it is therefore prevented that phosphorus is mingled with, and the sediment generated is in powdery, and it is gluey to avoid existing ammonium hydroxide purification process
The loss late of the generation of sediment, phosphorus can be reduced to 5% or less.
In present embodiment, urea will be slow release ammonia being heated to 60 DEG C or more:
CO(NH2)2+H2O→CO2↑+2NH3
NH3+H2O→NH4 ++OH-
The obtained product NH of urea hydrothermal decomposition4 +It is the subsequent reactant for preparing ammonium phosphate salt product, and the reaction is raw
At OH-The promotion for then facilitating pH value of solution is finally reached the optimum PH range of contamination precipitation in phosphoric acid raffinate.In addition, control
Condition processed decomposes urea slowly, uniformly discharges OH in the solution-, can prevent conventional ammonium hydroxide from adjusting local ph mistake in pH method
Winding that is high and leading to phosphorus caused by the intense hydrolysis of the part Fe, Al.
The surface topography of the removal of impurities slag of present embodiment and existing ammonium hydroxide removal of impurities slag surface topography are compared,
As a result as depicted in figs. 1 and 2.Fig. 1 is a kind of surface topography SEM figure of removal of impurities slag of embodiment 2；Fig. 2 is that existing ammonium hydroxide removes
The surface topography SEM of miscellaneous product schemes.As shown in Figure 1, the removal of impurities slag object is that flake stacks, and structural integrity is consistent, it was demonstrated that
Urea precipitation product crystallinity is high；As shown in Figure 2, existing ammonium hydroxide removal of impurities product sheet granularity is smaller, in irregular shape, easy shape
Reunite at bulky grain；By the comparison of Fig. 1 and Fig. 2 it is found that the urea removal of impurities product of present embodiment is compared to existing ammonia
Water cleans product, and pattern is more complete uniform, and crystalline size is bigger, the useful element phosphorus not rapid wear in Fe, Al, Mg precipitation process
It loses.
(3) process object of present embodiment is muddy phosphoric acid raffinate, is directly cleaned to muddy phosphoric acid raffinate,
The gelatinous precipitate being not required in filtering phosphoric acid raffinate can realize the purification to raffinate, the precipitating generated on a microscopic level
Object crystallinity is high, and crystallite dimension is big, and in fine-powdered, (the removal of impurities slag that existing removal of impurities mode obtains is in glue to particle on a macroscopic level
Shape), and the muddy object in phosphoric acid raffinate reacts in dedoping step with precipitating reagent, so that filter process is easier to carry out, shortens
Process flow.
(4) as described in this good effect (2), urea will be slow release ammonia being heated to 60 DEG C or more:
CO(NH2)2+H2O→CO2↑+2NH3
NH3+H2O→NH4 ++OH-
Urea, which decomposes, generates ammonia and carbon dioxide, and new impurity will not be introduced while removal of impurities, obtained to be based on phosphoric acid
The diammonium phosphate product of raffinate reaches the requirement of national standard " monoammonium phosphate, Diammonium phosphate (DAP) " (GB 10205-2009).
Therefore, present embodiment has good operational environment, easily filters low with dedoping step phosphorus loss late while not drawing
The advantages of entering new impurity.
Claims (2)
1. a kind of preparation method of the Diammonium phosphate (DAP) based on phosphoric acid raffinate, it is characterised in that the method comprises the concrete steps that:
Step 1: dilution
By phosphoric acid raffinate: the mass ratio of water is 1: (0.1~0.3) water is added in the phosphoric acid raffinate, in room temperature
Under the conditions of stir 0.5~1h, the phosphoric acid raffinate after being diluted；
Step 2: precipitating
By urea: the mass ratio of the phosphoric acid raffinate after the dilution is that (dilution is added in the urea by 0.5~2) ︰ 1
In phosphoric acid raffinate afterwards, stirring to pH value is 6~7 under the conditions of 70~100 DEG C, is separated by solid-liquid separation to get purified phosphoric acid
Raffinate and removal of impurities slag；
Step 3: washing
The removal of impurities slag is used into water washing, removal of impurities slag and washing water after being washed；The washing water return step one is used
In dilution phosphoric acid raffinate；
Step 4: preparation Diammonium phosphate (DAP)
The purified phosphoric acid raffinate is concentrated into P2O5Content is 40~50wt%, then passes to tubular reactor, is controlled
Degree of neutralization is 1.8~2.0, obtains the Diammonium phosphate (DAP) based on phosphoric acid raffinate.
2. the preparation method of the Diammonium phosphate (DAP) according to claim 1 based on phosphoric acid raffinate, it is characterised in that the phosphoric acid
Raffinate: P2O5Content > 35wt%, content of MgO are 2~8wt%, Al2O3Content is 4~8wt%, Fe2O3Content be 0.5~
3wt%, CaO content < 0.05wt%, K2O content < 0.1wt%, Na2O content < 1.5wt%, solid content are 4~8wt%, pH value
Less than -0.8；The density of phosphoric acid raffinate clear liquid is greater than 1.6g/cm3。
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|---|---|---|---|---|
| US20030235622A1 (en) * | 2002-06-20 | 2003-12-25 | Merck Patent Gmbh | Method of preparing alpha-and-beta-tricalcium phosphate powders |
| CN101891504A (en) * | 2010-07-26 | 2010-11-24 | 瓮福（集团）有限责任公司 | Method for producing granular monoammonium phosphate with raffinate |
| CN102674284A (en) * | 2012-06-20 | 2012-09-19 | 瓮福（集团）有限责任公司 | Method for producing industrial monoammonium phosphate co-produced fertilizer grade monoammonium phosphate by extracted spent acid |
| CN104016322A (en) * | 2014-05-20 | 2014-09-03 | 贵阳中化开磷化肥有限公司 | Production method for diammonium hydrogen phosphate |
| CN107161967A (en) * | 2017-06-29 | 2017-09-15 | 宜都兴发化工有限公司 | It is a kind of to add the method and device that raffinate clear liquid produces high-class product diammonium phosphate product |
-
2019
- 2019-07-26 CN CN201910684680.6A patent/CN110371939B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030235622A1 (en) * | 2002-06-20 | 2003-12-25 | Merck Patent Gmbh | Method of preparing alpha-and-beta-tricalcium phosphate powders |
| CN101891504A (en) * | 2010-07-26 | 2010-11-24 | 瓮福（集团）有限责任公司 | Method for producing granular monoammonium phosphate with raffinate |
| CN102674284A (en) * | 2012-06-20 | 2012-09-19 | 瓮福（集团）有限责任公司 | Method for producing industrial monoammonium phosphate co-produced fertilizer grade monoammonium phosphate by extracted spent acid |
| CN104016322A (en) * | 2014-05-20 | 2014-09-03 | 贵阳中化开磷化肥有限公司 | Production method for diammonium hydrogen phosphate |
| CN107161967A (en) * | 2017-06-29 | 2017-09-15 | 宜都兴发化工有限公司 | It is a kind of to add the method and device that raffinate clear liquid produces high-class product diammonium phosphate product |
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