CN104261371B - A kind of method by high impurity phosphorus ore production diammonium phosphate - Google Patents

A kind of method by high impurity phosphorus ore production diammonium phosphate Download PDF

Info

Publication number
CN104261371B
CN104261371B CN201410440378.3A CN201410440378A CN104261371B CN 104261371 B CN104261371 B CN 104261371B CN 201410440378 A CN201410440378 A CN 201410440378A CN 104261371 B CN104261371 B CN 104261371B
Authority
CN
China
Prior art keywords
diammonium phosphate
high impurity
phosphorus
production
phosphoric acid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201410440378.3A
Other languages
Chinese (zh)
Other versions
CN104261371A (en
Inventor
师永林
韩喜超
彭明辉
李勇
薛河南
解忠勇
潘继斐
曹光玲
蔡昆林
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Yunnan Yuntianhua Co Ltd
Original Assignee
Yunnan Yth International Chemical Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Yunnan Yth International Chemical Co Ltd filed Critical Yunnan Yth International Chemical Co Ltd
Priority to CN201410440378.3A priority Critical patent/CN104261371B/en
Publication of CN104261371A publication Critical patent/CN104261371A/en
Application granted granted Critical
Publication of CN104261371B publication Critical patent/CN104261371B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

The invention discloses a kind of method by high impurity phosphorus ore production diammonium phosphate.Extract high impurity phosphorus ore by dihydrate wet phosphoric acid technique, in gained dilute phosphoric acid, logical ammonia carries out neutralization reaction, and gained phosphoric acid by wet process ammonification slip carries out natural subsidence in subsider, gets upper strata phosphorus ammonium clear liquid for subsequent use; Dilute phosphoric acid carries out concentrating, must clarifying gelled acid through clarification ageing; Upper strata phosphorus ammonium clear liquid is mixed with clarification gelled acid, more traditionally features of DAP production explained hereafter obtains diammonium phosphate product.This method can solve the continuous dilution along with phosphate rock resource, the problem that diammonium phosphate quality declines, and effectively ensure that the production of diammonium phosphate, to the strong adaptability of phosphorus ore, comparatively economical, is conducive to realizing large-scale industrial production.

Description

A kind of method by high impurity phosphorus ore production diammonium phosphate
Technical field
The invention belongs to features of DAP production technical field, specifically relate to a kind of method by high impurity phosphorus ore production diammonium phosphate.
Background technology
Traditional features of DAP production technique is by dilute phosphoric acid (about 25%P 2o 5) be concentrated into 46 ~ 50%P 2o 5, then carry out neutralization reaction with ammonia, controlled by degree of neutralization 1.5 ~ 1.7, granulation in ammoniation granulator, obtains diammonium phosphate product through roller drying.But along with the minimizing of phosphate rock resource in recent years, the continuous dilution of phosphorus ore quality, in phosphoric acid by wet process, the impurity such as Fe, Al, Mg raises gradually, and causing phosphoric acid by wet process impurity coefficient MER value, higher (MER value refers to Fe in phosphoric acid by wet process 2o 3, Al 2o 3, MgO mass percent sum and P 2o 5the ratio of mass percent, i.e. (Fe 2o 3+ Al 2o 3+ MgO)/P 2o 5), to the production of DAP product, particularly cause considerable influence to the production of total nutrient 64%DAP, product nitrogen content is on the low side, the more difficult requirement that is up to state standards, the more difficult specification of quality reached to diammonium phosphate product on world market.
At present, the research report producing DAP product about the dilution of reply phosphate rock resource is more, it mainly contains three kinds of methods: one is phosphorus ore pre-treatment, main employing phosphate rock floating technology and phosphorus ore de-magging technology etc., but the subject matter that this method exists is that phosphrus reagent is lower, mine tailing amount is large, is unfavorable for the comprehensive utilization of resource, in addition, a large amount of acid waste waters that phosphorus ore de-magging produces are difficult to the problems such as digestibility and utilization and all govern it and apply.Two is that phosphoric acid by wet process removes iron, magnesium, aluminium impurity, research report both at home and abroad about this one side is a lot, but mostly because economy is poor, cost cannot get through, up to the present, phosphoric acid by wet process is not also adopted to remove the report of method production high-quality DAP of iron, magnesium, aluminium impurity.Three is phosphoric acid by wet process ammonification impurity removal method, and this method, to the strong adaptability of phosphorus ore, is convenient to implement, and is also generally acknowledge comparatively economically viable method.At present, the research report about this method is a lot, and the present invention just belongs to phosphoric acid by wet process ammonification impurity removal method.
Chinese patent 201010181889.X discloses " a kind of method improving nitrogen content of diammonium phosphate product ".This method is heating and melting under being stirred in fusion tank by the urea of nitrogen content >=46%; again the urea through high temperature melting is squeezed into tablets press in proportion; inside tablets press, be coated with spray granulating together with diammonium phosphate, the massfraction obtaining nitrogen reaches the diammonium phosphate product of more than 18%.The subject matter that this method exists is the nitrogen in diammonium phosphate is ammonium nitrogen, and the nitrogen in urea is acyl state nitrogen, this is two kinds of multi-form nitrogen, its analysis determining method is all different, so strictly speaking, interpolation urea is not the nitrogen content that improve diammonium phosphate product truly.
Chinese patent 200610021182.6 discloses " adopting method and the secondary ammoniation reactor of acidic slurry concentration production diammonium phosphate ".This method is that adopt twice ammonification to produce DAP, the degree of neutralization of an ammonification is 0.5 ~ 1.0, this acidic slurry concentration to moisture 13 ~ 20% with the dilute phosphoric acid of two water wet production for raw material; Secondary ammoniation and preparation DAP adopt Traditional Method DAP technique to produce.The object of this method adopts slip to concentrate steam saving, do not solve the problem that DAP product nitrogen content that diluting phosphate rock causes is on the low side.
Chinese patent 200910191621.1 discloses " adopting semi-acidic slurry to concentrate method and the secondary ammoniation concentration integrated device of production diammonium phosphate ".This method be with two water wet method dilute phosphoric acids for raw material, be first concentrated into 30 ~ 40%P 2o 5, then carrying out settlement separate, bottom sludge sends to two water wet method dilute phosphoric acid subsiders, upper clear supernate adopts four aminating reactions, the degree of neutralization of an ammonification is 0.3 ~ 0.5, and the degree of neutralization of secondary ammoniation is 0.6 ~ 0.8, is then 15 ~ 20% by acidic slurry concentration to water content; Carry out third time, the 4th aminating reaction again, the rear obtained diammonium phosphate product of dry and screening.The object of this method adopts dilute phosphoric acid to concentrate settlement separately with strong phosphoric acid to reach the object removing partial impurities, but the effect of this method imurity-removal is very limited, also can not solve the problem that DAP product nitrogen content that diluting phosphate rock causes is on the low side.
Chinese patent 200810048758.7 discloses " technique of slurry concentrated process co-producing diammonium phosphate and monoammonium phosphate ".This method is the same with Chinese patent 200610021182.6 also adopts twice ammonification.One time ammonification degree of neutralization is 1.0 ~ 1.15, settlement separate after ammonification, the thick slurry in bottom with in concentrated together with slip after be used for producing monoammonium phosphate; Supernatant liquid secondary ammoniation after concentrated produces diammonium phosphate product.The subject matter that this method exists concentrates supernatant liquid; because supernatant liquid is phosphor ammonium slurry, in order to ensure that concentration process is non-crystallizable, its concentrated concentration is on the low side; simultaneously; carry out secondary ammoniation to enriching slurry, because this process reaction neutralization heat is less, reaction slurry moisture content is high; direct feeding spray granulating machine; its granulation has been difficult to, and very large to Influence of production, system moisture is difficult to balance.
Chinese patent 201210120131.4 discloses " method of diammonium phosphate and slow-release fertilizer prepared by a kind of high impurity phosphorus ore ".This method adopts high impurity phosphoric acid to be raw material, neutralize by alkaline substance, hierarchy of control degree of neutralization is 0.05 ~ 0.7, temperature is 30 ~ 130 DEG C, reaction times is 10 ~ 120 minutes, filters after reaction, and filter residue is used for producing raw material or the lapping of slow-release fertilizer or Bulk Blending Fertilizer or other slow-release fertilizer, filtrate concentrates, and the concentration controlling concentrated solution is 36 ~ 45%P 2o 5, concentrated solution adopts alkaline substance to continue neutralization, and controlling solution degree of neutralization is 1.3 ~ 1.6, and the slip after neutralization produces diammonium phosphate product traditionally.The subject matter that this method exists is in whole high impurity phosphoric acid by wet process and rear filter cleaner by alkaline substance, very large with filter cleaner load in certainly will causing, huge filter plant need be configured supporting with it, cause investment significantly to increase, the production requirement of the extensive DAP device of more difficult adaptation.
Summary of the invention
The object of the invention is to for the deficiencies in the prior art, a kind of method by high impurity phosphorus ore production diammonium phosphate is provided, to solve the problem of the diammonium phosphate product Quality Down caused due to phosphate rock resource dilution, ensure the suitability for industrialized production of diammonium phosphate product.
The present invention seeks to be achieved through the following technical solutions.
Except as otherwise noted, percentage ratio of the present invention is mass percent.
By a method for high impurity phosphorus ore production diammonium phosphate, comprise the following steps:
(1) extract high impurity phosphorus ore by dihydrate wet phosphoric acid technique, in gained two water wet method dilute phosphoric acid, pass into ammonia carry out neutralization reaction, being neutralized to slip pH value is 4.0 ~ 7.0;
(2) step (1) gained phosphoric acid by wet process ammonification slip is carried out natural subsidence in subsider, get upper strata phosphorus ammonium clear liquid for subsequent use; The phosphorus ammonium slag slurry of bottom is used for subsequent production agricultural type complex fertilizer product;
(3) the two water wet method dilute phosphoric acids got described in step (1) carry out concentrating, must clarifying gelled acid through clarification ageing;
(4) upper strata phosphorus ammonium clear liquid for subsequent use for step (2) is clarified gelled acid with step (3) gained to mix, the MER value of mixed slurry is 0.080 ~ 0.095, and the slip mixed is concentrated into 40 ~ 50%P 2o 5;
(5) step (4) gained is concentrated mixed slurry traditionally features of DAP production explained hereafter obtain diammonium phosphate product.
In step (1), the pH value of slip is preferably 5.0 ~ 6.0.
In step (4), the MER value of mixed slurry is preferably 0.080 ~ 0.085.
The slip mixed in step (4) is preferably concentrated into 44 ~ 47%P 2o 5.
In step (4), can first filter upper strata phosphorus ammonium clear liquid, the phosphorus ammonium clear liquid after filtration mixes with clarification gelled acid again.
In step (4), can first concentrate upper strata phosphorus ammonium clear liquid, enriched material mixes with clarification gelled acid again, and then traditionally features of DAP production explained hereafter obtains diammonium phosphate product.
Compared with prior art, its advantage is in the present invention:
(1) this method only carries out ammonification removal of impurities to part dilute phosphoric acid, and it accounts for 1/2 ~ 1/3 of total amount, greatly reduces the load of dilute phosphoric acid ammonification removal of impurities operation, can significantly reduce required separating power, reduces investment.
(2) filtration gained phosphorus ammonium filtrate and clarification gelled acid mix by this method in proportion, mixed slurry has comparatively strongly-acid, monoammonium phosphate is made to be difficult to crystallization in strong acidic environment, ensure that concentrated concentration, avoid the monoammonium phosphate crystallization that independent concentrated filtrate brings, mixed slurry concentration is difficult to the problem improved.
(3) investment of this method is less, only needs to transform a little existing features of DAP production system, and in addition, this method is to the strong adaptability of phosphorus ore, comparatively economical, is conducive to realizing large-scale industrial production.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the present invention is described in further detail, but drawings and Examples are not limited to the technical solution.
Embodiment 1
As shown in Figure 1,1000.0g wet method dilute phosphoric acid (24.37%P is got 2o 5), logical ammonia carries out neutralization reaction wherein, and being neutralized to slip pH is 4.0, in and slip after natural subsidence, gained supernatant liquid is used as the raw material of lower step production diammonium phosphate, and its analysis indexes is: P 2o 5%=23.47, Fe 2o 3%=0.18, Al 2o 3%=0.17, MgO%=0.65, MER=0.043.
Get 241.2g above-mentioned phosphorus ammonium clear liquid, clarify gelled acid (P with 258.8g 2o 5%=47.07, Fe 2o 3%=1.02, Al 2o 3%=2.00, MgO%=1.92, MER=0.105) mixing, mixed slurry MER value is 0.085, passes into ammonia and carries out neutralization reaction, is neutralized to slip pH value and is greater than 9.0, then drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=47.52, P 2o 5 is water-soluble%=43.26, water-soluble phosphorus/available phosphorus=91.04%, total N%=18.21, H 2o%=0.76.
Embodiment 2:
Get 1000.0g wet method dilute phosphoric acid (24.37%P 2o 5), logical ammonia carries out neutralization reaction wherein, and being neutralized to slip pH is 4.5, in and slip after natural subsidence, gained supernatant liquid is used as the raw material of lower step production diammonium phosphate after filtering, and its analysis indexes is: P 2o 5%=23.90, Fe 2o 3%=0.045, Al 2o 3%=0.024, MgO%=0.39, MER=0.020.
Get phosphorus ammonium filtrate after the above-mentioned filtration of 155.4g, clarify gelled acid (P with 344.6g 2o 5%=47.12, Fe 2o 3%=0.86, Al 2o 3%=1.92, MgO%=1.93, MER=0.100) mixing, mixed slurry MER value is 0.085, passes into ammonia and carries out neutralization reaction, is neutralized to slip pH value and is greater than 9.0, then drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=47.12, P 2o 5 is water-soluble%=43.41, water-soluble phosphorus/available phosphorus=92.13%, total N%=18.37, H 2o%=0.38.
Embodiment 3:
Get 1000.0g wet method dilute phosphoric acid (24.37%P 2o 5), pass into ammonia wherein and carry out neutralization reaction, being neutralized to slip pH is 5.0, in and slip after natural subsidence, gained supernatant liquid is used as the raw material of lower step production diammonium phosphate, and its analysis indexes is: P 2o 5%=24.18, Fe 2o 3%=0.031, Al 2o 3%=0.016, MgO%=0.31, MER=0.015.
Get 170.6g above-mentioned phosphorus ammonium clear liquid, clarify gelled acid (P with 329.4g 2o 5%=46.98, Fe 2o 3%=1.19, Al 2o 3%=2.08, MgO%=1.90, MER=0.110) mixing, mixed slurry MER value is 0.090, passes into ammonia and carries out neutralization reaction, is neutralized to slip pH value and is greater than 9.0, then drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=46.90, P 2o 5 is water-soluble%=42.91, water-soluble phosphorus/available phosphorus=91.50%, total N%=18.17, H 2o%=0.43.
Embodiment 4:
Get 1000.0g wet method dilute phosphoric acid (24.37%P 2o 5), pass into ammonia wherein and carry out neutralization reaction, being neutralized to slip pH is 6.0, in and slip after natural subsidence, gained supernatant liquid is used as the raw material of lower step production diammonium phosphate after filtering, and its analysis indexes is: P 2o 5%=22.87, Fe 2o 3%=0.026, Al 2o 3%=0.016, MgO%=0.20, MER=0.011.
Get phosphorus ammonium filtrate after the above-mentioned filtration of 270.7g, clarify gelled acid (P with 229.3g 2o 5%=46.85, Fe 2o 3%=1.52, Al 2o 3%=2.24, MgO%=1.86, MER=0.120) mixing, mixed slurry MER value is 0.080, passes into ammonia and carries out neutralization reaction, is neutralized to slip pH value and is greater than 9.0, then drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=47.65, P 2o 5 is water-soluble%=43.34, water-soluble phosphorus/available phosphorus=90.95%, total N%=18.57, H 2o%=0.57.
Embodiment 5:
Get 1000.0g wet method dilute phosphoric acid (24.37%P 2o 5), pass into ammonia wherein and carry out neutralization reaction, being neutralized to slip pH is 7.0, in and slip after natural subsidence, gained supernatant liquid is used as the raw material of lower step production diammonium phosphate, and its analysis indexes is: P 2o 5%=24.63, Fe 2o 3%=0.025, Al 2o 3%=0.016, MgO%=0.08, MER=0.005.
Get 212.0g above-mentioned phosphorus ammonium clear liquid, first after concentrated, then clarify gelled acid (P with 288.0g 2o 5%=46.71, Fe 2o 3%=1.84, Al 2o 3%=2.40, MgO%=1.83, MER=0.130) mixing, mixed slurry MER value is 0.095, passes into ammonia and carries out neutralization reaction, is neutralized to slip pH value and is greater than 9.0, then drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=46.51, P 2o 5 is water-soluble%=41.92, water-soluble phosphorus/available phosphorus=90.13%, total N%=17.73, H 2o%=0.84.
Embodiment 6:
Get 10000.0g wet method dilute phosphoric acid (24.37%P 2o 5), pass into ammonia wherein and carry out neutralization reaction, being neutralized to slip pH is 5.80, in and slip after natural subsidence, gained supernatant liquid is used as the raw material of lower step production diammonium phosphate, and its analysis indexes is: P 2o 5%=23.68, Fe 2o 3%=0.040, Al 2o 3%=0.017, MgO%=0.26, MER=0.013.
Get 714.0g above-mentioned phosphorus ammonium clear liquid, first after concentrated, then clarify gelled acid (P with 1286.0g 2o 5%=47.07, Fe 2o 3%=1.02, Al 2o 3%=2.00, MgO%=1.92, MER=0.105) mixing, make mixed slurry MER value be 0.085, be then 0.072MPa in vacuum tightness, temperature is carry out vacuum concentration at 85 DEG C, and being concentrated into mixed slurry concentration is 47.79%P 2o 5, pass into ammonia and carry out neutralization reaction, be neutralized to slip pH value and be greater than 9.0, then drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=47.58, P 2o 5 is water-soluble%=43.71, water-soluble phosphorus/available phosphorus=91.87%, total N%=18.42, H 2o%=1.03.
Embodiment 7:
Phosphorus ammonium clear liquid 684.0g in Example 6, clarifies gelled acid (P with 1316.0g 2o 5%=46.98, Fe 2o 3%=1.19, Al 2o 3%=2.08, MgO%=1.90, MER=0.110) mixing, making mixed slurry MER value be 0.090, is 0.072MPa in vacuum tightness, and temperature is carry out vacuum concentration at 85 DEG C, and being concentrated into mixed slurry concentration is 50.07%P 2o 5, pass into ammonia and carry out neutralization reaction, be neutralized to slip pH value and be greater than 9.0, drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is:
P2O 5 is effective%=47.36, P2O 5 is water-soluble%=43.12, water-soluble phosphorus/available phosphorus=91.05%, total N%=18.21, H 2o%=0.97.
Embodiment 8:
Phosphorus ammonium clear liquid 534.2g in Example 6, clarifies gelled acid (P with 1465.8g 2o 5%=46.98, Fe 2o 3%=1.19, Al 2o 3%=2.08, MgO%=1.90, MER=0.110) mixing, making mixed slurry MER value be 0.095, is 0.072MPa in vacuum tightness, and temperature is carry out vacuum concentration at 85 DEG C, and being concentrated into mixed slurry concentration is 42.07%P 2o 5, pass into ammonia and carry out neutralization reaction, be neutralized to slip pH value and be greater than 9.0, drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=46.62, P 2o 5 is water-soluble%=41.96, water-soluble phosphorus/available phosphorus=90.00%, total N%=17.86, H 2o%=1.50.
Embodiment 9:
Phosphorus ammonium clear liquid 1084.0g in Example 6, clarifies gelled acid (P with 916.0g 2o 5%=46.85, Fe 2o 3%=1.52, Al 2o 3%=2.24, MgO%=1.86, MER=0.120) mixing, making mixed slurry MER value be 0.080, is 0.072MPa in vacuum tightness, and temperature is carry out vacuum concentration at 85 DEG C, and being concentrated into mixed slurry concentration is 46.54%P 2o 5, pass into ammonia and carry out neutralization reaction, be neutralized to slip pH value and be greater than 9.0, drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=47.42, P 2o 5 is water-soluble%=42.96, water-soluble phosphorus/available phosphorus=90.59%, total N%=18.66, H 2o%=1.22.
Embodiment 10:
Phosphorus ammonium clear liquid 1107.4g in Example 6, clarifies gelled acid (P with 892.6g 2o 5%=46.71, Fe 2o 3%=1.84, Al 2o 3%=2.40, MgO%=1.83, MER=0.130) mixing, making mixed slurry MER value be 0.085, is 0.072MPa in vacuum tightness, and temperature is carry out vacuum concentration at 85 DEG C, and being concentrated into mixed slurry concentration is 49.87%P 2o 5, pass into ammonia and carry out neutralization reaction, be neutralized to slip pH value and be greater than 9.0, drying in the baking oven of 65 ~ 70 DEG C, after crushed obtained DAP sample, its analysis indexes is: P 2o 5 is effective%=47.91, P 2o 5 is water-soluble%=44.14, water-soluble phosphorus/available phosphorus=92.13%, total N%=18.37, H 2o%=1.84.

Claims (6)

1., by a method for high impurity phosphorus ore production diammonium phosphate, comprise the following steps:
(1) extract high impurity phosphorus ore by dihydrate wet phosphoric acid technique, in gained two water wet method dilute phosphoric acid, pass into ammonia carry out neutralization reaction, being neutralized to slip pH value is 4.0 ~ 7.0;
(2) step (1) gained phosphoric acid by wet process ammonification slip is carried out natural subsidence in subsider, get upper strata phosphorus ammonium clear liquid for subsequent use; The phosphorus ammonium slag slurry of bottom is used for subsequent production agricultural type complex fertilizer product;
(3) the two water wet method dilute phosphoric acids got described in step (1) carry out concentrating, must clarifying gelled acid through clarification ageing;
(4) upper strata phosphorus ammonium clear liquid for subsequent use for step (2) is clarified gelled acid with step (3) gained to mix, the MER value of mixed slurry is 0.080 ~ 0.095, and the slip mixed is concentrated into 40 ~ 50%P 2o 5;
(5) step (4) gained is concentrated mixed slurry traditionally features of DAP production explained hereafter obtain diammonium phosphate product.
2. the method by high impurity phosphorus ore production diammonium phosphate according to claim 1, is characterized in that: in step (1), the pH value of slip is preferably 5.0 ~ 6.0.
3. the method by high impurity phosphorus ore production diammonium phosphate according to claim 1, is characterized in that: in step (4), the MER value of mixed slurry is preferably 0.080 ~ 0.085.
4. the method by high impurity phosphorus ore production diammonium phosphate according to claim 1, is characterized in that: the slip mixed in step (4) is preferably concentrated into 44 ~ 47%P 2o 5.
5. the method by high impurity phosphorus ore production diammonium phosphate according to claim 1, is characterized in that: in step (4), first filters upper strata phosphorus ammonium clear liquid, and the phosphorus ammonium clear liquid after filtration mixes with clarification gelled acid again.
6. the method by high impurity phosphorus ore production diammonium phosphate according to claim 1, it is characterized in that: in step (4), first upper strata phosphorus ammonium clear liquid is concentrated, enriched material mixes with clarification gelled acid again, and then traditionally features of DAP production explained hereafter obtains diammonium phosphate product.
CN201410440378.3A 2014-09-01 2014-09-01 A kind of method by high impurity phosphorus ore production diammonium phosphate Active CN104261371B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410440378.3A CN104261371B (en) 2014-09-01 2014-09-01 A kind of method by high impurity phosphorus ore production diammonium phosphate

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410440378.3A CN104261371B (en) 2014-09-01 2014-09-01 A kind of method by high impurity phosphorus ore production diammonium phosphate

Publications (2)

Publication Number Publication Date
CN104261371A CN104261371A (en) 2015-01-07
CN104261371B true CN104261371B (en) 2016-04-20

Family

ID=52153001

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410440378.3A Active CN104261371B (en) 2014-09-01 2014-09-01 A kind of method by high impurity phosphorus ore production diammonium phosphate

Country Status (1)

Country Link
CN (1) CN104261371B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105257578B (en) * 2015-10-26 2017-07-21 衡阳师范学院 A kind of fan speed regulation method for dihydrate wet phosphoric acid extraction process
CN109019545A (en) * 2018-09-11 2018-12-18 湖北省黄麦岭磷化工有限责任公司 A kind of technique of phosphoric acid,diluted demetalization ion
CN113479859B (en) * 2021-06-11 2022-06-21 湖北宜化肥业有限公司 Method for producing diammonium phosphate from phosphorite with high impurity content

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1872669A (en) * 2006-06-16 2006-12-06 四川川大中德环保技术有限公司 Method for producing diammonium phosphate by concentrating acid slime, and secondary ammoniation reactor
RU2310630C1 (en) * 2006-08-01 2007-11-20 Открытое акционерное общество "Научно-исследовательский институт по удобрениям и инсектофунгицидам им. Я.В. Самойлова" Diammonium phosphate production process
CN102659454A (en) * 2012-04-23 2012-09-12 四川大学 Method for preparing diammonium phosphate and slow release fertilizer by using high-impurity phosphorite

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1872669A (en) * 2006-06-16 2006-12-06 四川川大中德环保技术有限公司 Method for producing diammonium phosphate by concentrating acid slime, and secondary ammoniation reactor
RU2310630C1 (en) * 2006-08-01 2007-11-20 Открытое акционерное общество "Научно-исследовательский институт по удобрениям и инсектофунгицидам им. Я.В. Самойлова" Diammonium phosphate production process
CN102659454A (en) * 2012-04-23 2012-09-12 四川大学 Method for preparing diammonium phosphate and slow release fertilizer by using high-impurity phosphorite

Also Published As

Publication number Publication date
CN104261371A (en) 2015-01-07

Similar Documents

Publication Publication Date Title
CN101891504B (en) Method for producing granular monoammonium phosphate with raffinate
CN101857213B (en) Method for preparing food-grade diammonium phosphate from wet-process phosphoric acid
CN104229764A (en) Method for continuously producing water-soluble monoammonium phosphate by using wet-process phosphoric acid
CN105600763B (en) A kind of method that fluoride salt method of purification produces industrial monoammonium phosphate
CN101857210B (en) Method for producing industrial grade diammonium phosphate from wet-process phosphoric acid
CN101708832A (en) Method for producing defluorinated ammonium phosphate
CN103466579B (en) The method of the complete water-soluble monoammonium phosphate of Wet-process Phosphoric Acid Production
CN104261371B (en) A kind of method by high impurity phosphorus ore production diammonium phosphate
CN104230448A (en) Method for preparing N-P-K (Nitrogen-Phosphorus-Potassium) compound fertilizer by using hydrochloric acid to decompose phosphorite acidified solution
CN104140088A (en) Method for producing fertilizer-level monoammonium phosphate through fertilizer-level calcium hydrophosphate
CN101734970A (en) Method for preparing urea ammonium phosphate by employing multi-level neutralization and acidic slurry concentration
CN107879321A (en) A kind of method of phosphorus ore de-magging co-production prodan and magnesium sulfate
CN105439646A (en) Method for producing phosphorus magnesia fertilizer by using wet phosphoric acid residues
CN102659454B (en) Method for preparing diammonium phosphate and slow release fertilizer by using high-impurity phosphorite
CN105000539A (en) Method for producing potassium dihydrogen phosphate and potassium-ammonium dihydrogen phosphate through wet process phosphoric acid
CN102874779B (en) New method for producing monoammonium phosphate by using middle and low-grade phosphate ore without discharging of solid waste
CN102674405A (en) Method for preparing potassium sulfate by using picromerite
CN105293459A (en) Method for producing fully water-soluble monoammonium phosphate and co-producing ammonium magnesium phosphate by wet process phosphoric acid
CN101293640B (en) Method for preparing ammonium phosphate salt with hydrochloric acid leaching deficient phosphorus ore
CN103435376A (en) Method and apparatus used for preparing ammonium phosphate fertilizer from phosphoric acid sediment
CN108117054A (en) A kind of method for preparing potassium dihydrogen phosphate coproduction ammonium potassium dihydrogen phosphate
CN105152716B (en) A kind for the treatment of process of the acid solution produced in phosphorus ore acid system ore dressing and ore dressing process and application
CN104326464A (en) Method for preparing high-quality calcium superphosphate in process of producing feed-grade calcium hydrophosphate
CN103539170B (en) Method for producing magnesium sulfate and industrial-grade monoammonium phosphate by using tail solution from refining of wet process phosphoric acid by solvent extraction method
CN106800284B (en) A kind of method of phosphorus ore de-magging phosphoric acid byproduct monoammonium

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
TR01 Transfer of patent right
TR01 Transfer of patent right

Effective date of registration: 20200903

Address after: 650228 No. 1417, Dianchi Road, Xishan District, Yunnan, Kunming

Patentee after: YUNNAN YUNTIANHUA Co.,Ltd.

Address before: 650228 No. 1417, Dianchi Road, Kunming, Yunnan

Patentee before: YUNNAN YUNTIANHUA INTERNATIONAL CHEMICAL Co.,Ltd.