CN104828799B - Process of producing feed-grade calcium dihydrogen phosphate through phosphoric acid circulation impurity removal method - Google Patents
Process of producing feed-grade calcium dihydrogen phosphate through phosphoric acid circulation impurity removal method Download PDFInfo
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Abstract
The invention discloses a process of producing feed-grade calcium dihydrogen phosphate through a phosphoric acid circulation impurity removal method, wherein the method comprises following steps: (a) decomposing acid mine; (b) maintaining the temperature and performing sedimentation to obtain a slurry material; (c) feeding the slurry material to a crystallization trough, cooling the slurry material to 30-60 DEG C and performing solid-liquid separation to obtain a filtrate and a filter residue; (d) adding water to the filter residue for making material slurry of which the specific gravity is 1.30-1.60; (e) maintaining the temperature and performing sedimentation to obtain a material slurry; (f) feeding the material slurry in the step (e) to a dryer with high-temperature gas flow to dry the material slurry, and adding an alkaline substance to a dried product to obtain the feed-grade calcium dihydrogen phosphate product; and (g) mixing a filtrate in the step (c) with phosphoric acid by wet process, and removing impurities to obtain an acid liquid used for decomposing the acid mine in the step (a). The process is good in adaptability of phosphorus ore, can ensure the product in the step (f) and heavy metals to meet a standard completely, can reduce discharge load of phosphogypsum and is good in application prospect.
Description
Technical field
The invention belongs to phosphate preparation field is and in particular to a kind of phosphoric acid circulation impurity removal method produces feed grade biphosphate
The technique of calcium.
Background technology
The demand of world's synthos is from the beginning of 1940, initially use meat meal tankage, low defluorinated phosphate rock.Feedstuff phosphorus now
Acid calcium salt mainly has 3 kinds of products：Calcium hydrogen phosphate (DCP)；Dalcium biphosphate (MCP)；Defluorinated calcium phosphate (DFP).Also exist in a large number
Calcium hydrogen phosphate and the intermediate species of dalcium biphosphate, this product by blending calcium hydrogen phosphate and dalcium biphosphate, or can given birth to
Obtain by proportion of composing reaction production during product, i.e. (MDCP).
According to investigations, the consumption of phosphorus substantially fertilizer in world wide（80%）, detergent（12%）, fodder calcium phosphate salt
（5%）, fine chemistry industry（3%）.Consumption in feedstuff for the fodder calcium phosphate salt is usually 1%-3%, is the representative of mineral feed.
Through continuous development and the technological change of decades, the production technology of fodder calcium phosphate salt is mainly with regional phosphorus ore
With sour resource classification.
（1）North America：Sulphuric acid and phosphorus ore extract phosphoric acid by wet process, and concentration defluorinating, agstone reaction produce MCP, DCP；Wet method
Phosphoric acid, phosphorus ore and soda calcination defluorinate produce DFP.
（2）Europe：Phosphoric acid by wet process is produced with Mannheim proeess potassium sulfate by-product salt acid extraction phosphorus ore, through precipitation defluorination, precipitates
Method produces the DCP of different cultivars, then with sedimentation method DCP and concentration defluorinating phosphoric acid production MCP（MDCP) or by North America mode sulphuric acid
Extract phosphoric acid by wet process with phosphorus ore, concentration defluorinating, agstone reaction produce MCP, DCP, no DFP product.
（3）Asia：Sulphuric acid extraction phosphorus phosphorus ore produces phosphoric acid by wet process, precipitation defluorination, and the sedimentation method produce DCP；Again with the sedimentation method
DCP and concentration defluorinating phosphoric acid or phosphorous acid production by BEP MCP (MDCP).Only a small amount of technique is pressed North America mode sulphuric acid and is extracted with phosphorus ore
Phosphoric acid by wet process, concentration defluorinating, agstone reaction produce MCP, DCP.DFP product only Japan, Korea S's production, production technology and north
U.S. identical.
Can be seen that the process that traditional feed grade calcium phosphate technology of threonates is exactly remove impurity, purification from technique all over the world,
It is all substantially that the phosphorus in phosphorus ore is converted into that impurity content is few, the high phosphate of effective ingredient.Calcium in phosphorus ore during this
All change into CaCl2Or CaSO4Exclude as impurity, and need to add during subsequent production synthos
Enter substantial amounts of agstone as Ca source, this one-in-and-one-out causes great waste in resource.For this Chinese patent《A kind of
The production method of feed-grade calcium phosphate》（Publication number CN101264873A）In propose and directly react production using phosphoric acid with phosphorus ore
The production method of fodder calcium phosphate salt.Its main technique is that excessive phosphoric acid and ground phosphate rock are added reactor hybrid reaction, system
Obtain the dalcium biphosphate material containing fluorine and phosphoric acid, this material is added in exsiccator and is dried and defluorinate, be obtained and contain free phosphoric acid
Defluorinated calcium phosphate pressed powder, then in this pressed powder add phosphoric acid nertralizer, prepared feed-grade calcium phosphate.
But occur in that some problems in actual moving process.In traditional feed grade calcium phosphate technology of threonates, if
Produced using phosphoric acid by wet process, had a requisite link, that is, the remove impurity of phosphoric acid by wet process, in order to ensure product matter
Amount, the heavy metal ion that the metal cations such as part Fe, Mg in phosphoric acid and As, lead, hydrargyrum etc. are harmful to removes.
In addition, product will be used as feed calcium salt additives, the heavy metal ion that As, Pb, Ge, Hg etc. are harmful to has strict
Require, patent CN101264873A is difficult to accomplish in this, all qualified fodder calcium phosphate salt of its indices to be made
Require that the objectionable impurities in Ore are little, this requirement to phosphorus ore is very high, and only minority disclosure satisfy that through selected phosphorus ore
Require.
Content of the invention
The technical problem to be solved is to provide a kind of phosphoric acid circulation impurity removal method to produce feed-level calcium biphosphate
Technique, this technique is good for the adaptability of ore deposit, product indices particularly sanitary index（Here sanitary index refers to
F and beavy metal impurity）The requirement of feedstuff calcium salt all can be met.
The technical solution adopted for the present invention to solve the technical problems is：Phosphoric acid circulation impurity removal method produces feed grade di(2-ethylhexyl)phosphate
The technique of hydrogen calcium, comprises the steps：
A, sour ore deposit are decomposed：The phosphoric acid processing through remove impurity and raw material ground phosphate rock are mixed into row decomposition reaction；
B, heat preservation settlement：Neutralize slip after the decomposition reaction of step a is carried out heat preservation settlement, from settler bottom separating material
Sedimentation impurity in slurry；
C, decrease temperature crystalline with separate：Slip after step b heat preservation settlement is delivered to crystallization tank, be cooled to 30～60 DEG C laggard
Row solid-liquid separation；
D, filter cake slurrying：Filter cake after step c solid-liquid separation is added water slurrying, controls slip proportion 1.30～1.60；
E, heat preservation settlement：The slip that step d is obtained carries out heat preservation settlement, the sedimentation from settler bottom separation slip
Impurity；
F, prepared product：Slip after step e heat preservation settlement is sent in the exsiccator have high temperature gas flow and is dried,
Feed-level calcium biphosphate semi-finished product are obtained after drying；It is subsequently adding a small amount of free acid in alkaline matter and in semi-finished product, system
Obtain feed-level calcium biphosphate product；
G, the filtrate after step c solid-liquid separation is mixed with phosphoric acid by wet process, then remove impurity；Acid solution after remove impurity is processed is
The phosphoric acid through remove impurity process described in step a simultaneously decomposes for sour ore deposit.
Wherein, in step c, after being cooled to 40～50 DEG C, carry out solid-liquid separation.
Wherein, in step d, control slip proportion 1.45～1.53.
Wherein, alkaline matter described in step f is Calx, Calcium Carbonate, defluorinated tricalcium phosphate, potassium carbonate, sodium carbonate, hydrogen-oxygen
Change at least one in sodium or potassium hydroxide.
Wherein, in above-mentioned processing step a, by the phosphoric acid processing through remove impurity and the mixed slip of raw material ground phosphate rock
H3PO4 concentration >=30%.
Further, by the phosphoric acid processing through remove impurity and raw material ground phosphate rock mixed slip H3PO4Concentration >=50%.
Wherein, in above-mentioned processing step a, the granularity of described ground phosphate rock was that 100 mesh sieves are more than 50%, controlled decomposition reaction
Temperature is 60～120 DEG C, the decomposition reaction time is 2～10 hours.
Further, the granularity of described ground phosphate rock be 100 mesh sieves be more than 70%, control decomposition reaction temperature be 60～
100 DEG C, the decomposition reaction time be 4～8 hours.
Wherein, in above-mentioned processing step b and e, described heat preservation settlement is on the premise of ensureing slip mobility, reduces
Mixing speed, makes under the impurity sedimentation in slip at a temperature of 60～100 DEG C.
Wherein, in above-mentioned processing step f, described exsiccator is spray dryer；Exsiccator hot wind inlet temperature 200～
800 DEG C, offgas outlet temperature control is at 80～250 DEG C.
Further, 250～550 DEG C of above-mentioned technique exsiccator hot wind inlet temperature, 100～180 DEG C of offgas outlet temperature.
Wherein, in above-mentioned processing step g, described remove impurity is to mix the filtrate after step c solid-liquid separation with phosphoric acid by wet process
Afterwards, add the sedimentation impurity that sulfide and step b and step e are separated, be subsequently adding filter aid and filtered, filtration
Filtrate is used for sour ore deposit and decomposes.Wherein, described filter aid is white carbon.
The invention has the beneficial effects as follows：
1st, acid cycle remove impurity, less demanding to phosphorus ore.
Employ phosphorus ore and phosphoric acid direct reaction in the patent technique of publication number CN101264873A, then neutralize unnecessary
Free phosphoric acid, but the impurity in phosphorus ore and harmful substance fully enter product, will can produce qualified fodder calcium phosphate salt
Just phosphorus ore is required higher.
This patent is dissolved by the way of a large amount of phosphoric acid circulations and shifts to an earlier date the objectionable impurities that the mode of remove impurity removes in Ore again,
Greatly promote product quality, the particularly heavy metal ion such as As, Pb can be easily removed.
2nd, remove impurity twice, product quality is lifted.
, in the slip heat preservation settlement in slurry reaction stage and the carrying out in two stages of slurrying, most of acid is insoluble for this patent
Thing, water-insoluble is separated, and greatly improves product water solublity.
3rd, the defluorinate of system multiple spot it is ensured that in product F completely up to standard.
Will be used as feedstuff phosphorus calcium product, product F requires to be less than 0.18%, is much all needed using the technique of Wet-process Phosphoric Acid Production
Phosphoric acid early stage is wanted to do substantial amounts of defluorinate work.This patent is in acid solution remove impurity stage, reaction slurry subsidence stage, slurrying subsidence stage
With slip spraying stage defluorinate, defluorinate efficiency high.
4th, reduce the use of calcium, reduce ardealite discharge capacity.
Traditional feedstuff phosphorus calcium production technology be required for using phosphorus ore produce obtain phosphoric acid again with calcium salt neutralize, production process
In, the Ca in phosphorus ore is changed into ardealite, processes as solid waste, but will add a large amount of calcium salts in follow-up N-process,
Cause very big waste, also increase production cost simultaneously.
The present invention is directly using acid decomposed by phosphoric acid phosphorus ore, and the P2O5 in product about 15～20% arises directly from phosphorus ore,
Compare traditional dalcium biphosphate to produce, this part phosphorus ore requires no Wet-process Phosphoric Acid Production process, that is, without experience sulphuric acid acid
Solution process, accordingly this part phosphorus ore also will not produce solid waste-ardealite, largely decrease ardealite
Yield, reduces environmental protection of enterprise pressure.In addition the Ca in phosphorus ore, completely into product, greatlys save cost.
Brief description
Fig. 1 is schematic flow sheet of the present invention.
Specific embodiment
With reference to specific embodiment, the present invention is further described.
Phosphoric acid circulation impurity removal method of the present invention produces the technique of feed-level calcium biphosphate, comprises the steps：
A, sour ore deposit are decomposed：The phosphoric acid processing through remove impurity and raw material ground phosphate rock are mixed into row decomposition reaction.
The reaction that this process occurs mainly has：
Ca5F(PO4)3+7H3PO4+5H2O=5Ca(H2PO4)2·H2O+HF↑
6HF+SiO2=H2SiF6+2H2O
Following reaction will occur in the case that activated silica is enough：
4HF+SiO2=SiF4↑+2H2O
The heavy metal ion such as arsenic, chromium, lead, hydrargyrum, cadmium mainly exist in nature in the form of the oxide, and this stage occurs
Following reaction：
As2O5+10H+=2As5++5H2O
Cr2O3+6H+=2Cr3++3H2O
PbO+2H+=Pb2++H2O
HgO+2H+=Hg2++2H2O
CdO+4H+=Cd2++2H2O
The oxide such as lead, hydrargyrum is less likely to occur to react under normal circumstances, but H in the system3PO4With a large amount of presence of HF,
Improve acid solution activity so that reaction can smoothly be carried out to the right.
It will be appreciated by persons skilled in the art that this step decomposition reaction is carried out under conditions of stirring, so
Sour ore deposit contact just can be made more preferably, reaction is more fully thorough.Thus, step b and e is also just had preferably " to ensure neutralize slip
On the premise of mobility, reduce mixing speed " description.
Preferably, in order that decomposition reaction is more thorough, this step is by the phosphoric acid processing through remove impurity and raw material ground phosphate rock
Mixed slip H3PO4Concentration >=30%.It is further preferred that mixed slip H3PO4Concentration >=50%.
Preferably, in order that decomposition reaction is more thorough, the granularity of ground phosphate rock described in this step was that 100 mesh sieves are more than
50%, control decomposition reaction temperature to be 60～120 DEG C, the decomposition reaction time is 2～10 hours.It is further preferred that described phosphorus
The granularity of breeze was that 100 mesh sieves are more than 70%, controlled decomposition reaction temperature to be 60～100 DEG C, the decomposition reaction time is 4～8
Hour.
B, heat preservation settlement：Neutralize slip after the decomposition reaction of step a is carried out heat preservation settlement, from settler bottom separating material
Sedimentation impurity in slurry.
Preferably, in order that effect of settling is more preferable, in above-mentioned processing step b, described heat preservation settlement is to ensure slip
On the premise of mobility, reduce mixing speed, make at a temperature of 60～100 DEG C under the impurity sedimentation in slip（Step e is same
Preferably heat preservation settlement at such a temperature）.
C, decrease temperature crystalline with separate：Slip after step b heat preservation settlement is delivered to crystallization tank, is cooled to 30～60 DEG C（Excellent
Select 40～50 DEG C）After carry out solid-liquid separation.Because dalcium biphosphate solubility with temperature changes greatly, in preference temperature（40～
50℃）Under, most of crystallization separates out, and obtains filter acid and cross filtering residue after filter plant separates；And the objectionable impurities such as arsenic, lead
It is dissolved in a large number in acid solution, enter acid solution processing system.
D, filter cake slurrying：Filter cake after step c solid-liquid separation is added water slurrying, controls slip proportion 1.30～1.60（Excellent
Select 1.45～1.53）；
E, heat preservation settlement：Slip after step d is obtained carries out heat preservation settlement, heavy from settler bottom separation slip
Fall impurity.
F, high-temperature spray defluorinate are obtained product：Slip after step e heat preservation settlement is sent into the drying with high temperature gas flow
It is dried in device, after being dried, obtain feed-level calcium biphosphate semi-finished product.This stage, substantial amounts of F was with SiF4Or the form of HF
With high-temperature flue gas effusion.It is subsequently adding a small amount of free acid in alkaline matter and in semi-finished product, prepared feed-level calcium biphosphate
Product.A small amount of free phosphoric acid is also contained, this can not use directly as feed additive in spray product.Add a small amount of
Alkaline matter is neutralized a small amount of free acid in product, and phosphoric acid nertralizer is Calx, Calcium Carbonate, defluorinated tricalcium phosphate, carbonic acid
At least one in potassium, sodium carbonate, sodium hydroxide, potassium hydroxide.
Preferably, in order that defluorination effect is more preferable, described exsiccator is spray dryer；Exsiccator hot wind inlet temperature
200～800 DEG C, offgas outlet temperature control is at 80～250 DEG C.
It is further preferred that 250～550 DEG C of above-mentioned technique exsiccator hot wind inlet temperature, offgas outlet temperature 100～
180℃.
G, the filtrate after step c solid-liquid separation is mixed with phosphoric acid by wet process, then remove impurity；Acid solution after remove impurity is processed is
The phosphoric acid through remove impurity process described in step a simultaneously decomposes for sour ore deposit.
Preferably, described remove impurity be the filtrate after step c solid-liquid separation is mixed with phosphoric acid by wet process after, add sulfide and
The sedimentation impurity that step b and step e are separated, is subsequently adding white carbon and filters, and the filtrate of filtration is used for sour ore deposit and decomposes.This
Skilled person understands, remove impurity of the present invention is not limited to this kind of mode, as long as preferable impurity-eliminating effect can be played.
Acid solution SO after remove impurity process4Content is low, and harmful beavy metal impurity content is low.The reaction occurring mainly has：
2F-+Ca2+=CaF2↓
SO4 2-+Ca2+=CaSO4↓
2As5++5S2-=As2S5↓
2Cr3++3S2-=Cr2S3↓
Pb2++S2-=PbS↓
Hg2++S2-=HgS↓
Cd2++S2-=CdS↓
Described sulfide can be Na2S、P2S5One of or two kinds.Imitated mainly due to its remove impurity using sedimentation impurity
More preferably, good impurity removing effect contains calcium mainly due to it to fruit, can be also relevant with other compositions.The sedimentation impurity that the present invention uses
In do not contain only calcium, and contain phosphorus；Ca is directly entered product entirely from phosphorus ore, phosphorus.Meanwhile, those skilled in the art can
To be understood by, the consumption of sulfide of the present invention and sedimentation impurity is slightly excessive according to theoretical amount under normal circumstances, due to this
Invention phosphoric acid circulation, so the consumption of sulfide and sedimentation impurity can be significantly increased, 2-20 times of such as theoretical amount, so removes
Miscellaneous effect can be more preferably.Under normal circumstances, the sedimentation impurity that step b and step e are separated all returns use.And logical
In the case of often, by the process of this step, mix acid liquor can reach claimed below：As≤5ppm, the heavy metal ion such as lead is equal
≤10ppm.
It will be appreciated by persons skilled in the art that after step f of the present invention is neutralized, product meeting ripening naturally, then
Air-cooled packaging, here is no longer described in detail.
Below by embodiment, the specific embodiment of the present invention is described further, but not therefore by the present invention
Protection domain limit in one embodiment.
Embodiment one
Tested with the phosphorus ore of Kaiyang Region, Guizhou Province for raw material, feedstock specifications are as shown in table 1：
Table 1 raw material Kaiyang Region, Guizhou Province phosphorus ore index
| Index | P2O5 | CaO | F | As | Pb | Cr | Hg | Cd |
| Phosphoric acid | 41.35 | 0.13 | 0.89 | 0.0028 | 0.0012 | 0.0065 | 0.00005 | 0.0001 |
| Phosphorus ore | 35.32 | 48.74 | 2.48 | 0.0044 | 0.0025 | 0.0112 | 0.0001 | 0.0004 |
The temperature of reaction phosphoric acid is increased to 60～80 DEG C in recirculation heater, adds inorganic agent 1（Na2S or P2S5）With
Inorganic agent 2（Prepare in advance, composition is similar to sedimentation impurity of the present invention）, it is simultaneously introduced a small amount of white carbon as helping
Filtering agent.Reaction 30min, filters；Filtering residue uses a small amount of clear water countercurrent washing, P in detection slag2O5Content is 1.1%.Filtrate acid is added
Enter and be warming up to 80～100 DEG C in neutralization reactor, start to throw ore deposit, by detecting H in slip3PO4Concentration controls breeze to add
Amount, when hydrogen ion concentration is reduced to 50%, terminates to throw ore deposit, reacts 5 hours, then stopping stirring, slip heat preservation settlement 0.5 hour,
Deslagging about 5%, slip carries out cooling down, and slurry temperature is down to 40～50 DEG C, starts filter pressing, and filtrate proceeds to intermediate storage tank, filter cake
Add water slurrying, obtains slip 1#, controls slip proportion to be 1.47.Slip heat preservation settlement, releases slag about 5%.Slip adds exsiccator
Atomization is dried, and controls 230～270 DEG C of exsiccator inlet temperature, 110～130 DEG C of outlet temperature, so that the F in slip is escaped.
Calculated according to free acid content in spray product, add a small amount of calcium carbonate powder, mix homogeneously, seal ripening, take after 4 hours
Go out, obtain final products.Product index is shown in Table 4.
Embodiment two
Tested with the raw ore of Yunnan Kunyang phosphorus ore for raw material, indices are as shown in table 2：
Table 2 raw material Yunnan Kunyang phosphorus ore index
| Index | P2O5 | CaO | F | As | Pb | Cr | Hg | Cd |
| Phosphoric acid | 41.35 | 0.13 | 0.89 | 0.0028 | 0.0012 | 0.0065 | 0.00005 | 0.0001 |
| Phosphorus ore | 24.6 | 42.11 | 3.32 | 0.0052 | 0.0020 | 0.0076 | 0.0011 | 0.0003 |
After breeze is levigate, participate in reaction, with embodiment 1, product index is shown in Table 4 to technology controlling and process.
Embodiment three
With certain phosphorus ore of Fuquan, Guizhou area, test after flotation, indices are as shown in table 3：
Table 3 raw material Fuquan, Guizhou phosphorus concentrate index
| Index | P2O5 | CaO | F | As | Pb | Cr | Hg | Cd |
| Phosphoric acid | 41.35 | 0.13 | 0.89 | 0.0028 | 0.0022 | 0.0065 | 0.00005 | 0.0001 |
| Phosphorus ore | 34.12 | 47.26 | 2.48 | 0.0035 | 0.0038 | 0.088 | 0.0012 | 0.0008 |
Every technology controlling and process recycles with embodiment 1, filter pressing acid, carries out continuous operation in 72 hours, final products take comprehensive
Close sample, index is as shown in table 4.
Example IV（Comparative example）
With certain phosphorus ore of Fuquan, Guizhou area, test after flotation（Raw material is with embodiment three）.
According to patent CN101264873A《A kind of production method of feed-grade calcium phosphate》Methods described is tested, gained
Product index is as shown in table 4.
Existing fodder calcium phosphate salt standard mainly has GB GB/T22548-2008, as shown in table 4：
Table 4 feed grade calcium phosphate product quality indicator
From table 4, it can be seen that using the phosphorus ore of different regions, using technique described in this patent, all can get quality more excellent
Feed-level calcium biphosphate product, illustrate that Technological adaptability described in this patent is wide, less demanding to phosphorus ore.Applicant is not using
With raw material simultaneously using contrast patent CN101264873A disclosed in method tested（Presents provides an embodiment
Illustrate as reference）, will there is the product situation not up to standard because of the difference of raw material.As can be seen here, phosphoric acid of the present invention
The technique that circulation impurity removal method produces feed-level calcium biphosphate is applicable not only to various phosphorus ores, and product index is superior, has
Very high using value.
Claims (5)
1. phosphoric acid circulation impurity removal method produces the technique of feed-level calcium biphosphate it is characterised in that comprising the steps：
A, sour ore deposit are decomposed：The phosphoric acid processing through remove impurity and raw material ground phosphate rock are mixed into row decomposition reaction；To live together through removing
The phosphoric acid of reason and raw material ground phosphate rock mixed slip H3PO4Concentration >=30%；
B, heat preservation settlement：Neutralize slip after the decomposition reaction of step a is carried out heat preservation settlement, from settler bottom separation slip
Sedimentation impurity；
C, decrease temperature crystalline with separate：Slip after step b heat preservation settlement is delivered to crystallization tank, carries out solid after being cooled to 30～60 DEG C
Liquid separates；
D, filter cake slurrying：Filter cake after step c solid-liquid separation is added water slurrying, controls slip proportion 1.30～1.60；
E, heat preservation settlement：The slip that step d is obtained carries out heat preservation settlement, and the sedimentation from settler bottom separation slip is miscellaneous
Matter；
F, prepared product：Slip after step e heat preservation settlement is sent in the exsiccator have high temperature gas flow and is dried, be dried
After obtain feed-level calcium biphosphate semi-finished product；It is subsequently adding a small amount of free acid in alkaline matter and in semi-finished product, be obtained and raise
Material level calcium biphosphate product；
G, the filtrate after step c solid-liquid separation is mixed with phosphoric acid by wet process, then remove impurity；Acid solution after remove impurity is processed is step
The phosphoric acid through remove impurity process described in a simultaneously decomposes for sour ore deposit；Described remove impurity be by the filtrate after step c solid-liquid separation with wet
After the mixing of method phosphoric acid, add the sedimentation impurity that sulfide and step b and step e are separated, be subsequently adding filter aid and carry out
Filter, the filtrate of filtration is used for sour ore deposit and decomposes.
2. phosphoric acid circulation impurity removal method according to claim 1 produce feed-level calcium biphosphate technique it is characterised in that：
In step a, the granularity of described ground phosphate rock was that 100 mesh sieves are more than 50%, controlled decomposition reaction temperature to be 60～120 DEG C, decompose
Response time is 2～10 hours.
3. phosphoric acid circulation impurity removal method according to claim 1 produce feed-level calcium biphosphate technique it is characterised in that：
In step b and e, described heat preservation settlement is on the premise of ensureing slip mobility, reduces mixing speed, at 60～100 DEG C
At a temperature of so that the impurity sedimentation in slip is got off.
4. phosphoric acid circulation impurity removal method according to claim 1 produce feed-level calcium biphosphate technique it is characterised in that：
In step f, described exsiccator is spray dryer；200～800 DEG C of exsiccator hot wind inlet temperature, offgas outlet temperature control
At 80～250 DEG C.
5. phosphoric acid circulation impurity removal method according to claim 4 produce feed-level calcium biphosphate technique it is characterised in that：
250～550 DEG C of exsiccator hot wind inlet temperature, 100～180 DEG C of offgas outlet temperature.
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| CN105197905B (en) * | 2015-09-24 | 2018-05-18 | 中化化肥有限公司成都研发中心 | Extract the production method of phosphorus ore coproduction feed-level calcium biphosphate and technical grade phosphorus ammonium |
| CN106829900A (en) * | 2017-01-10 | 2017-06-13 | 四川龙蟒磷化工有限公司 | The method that carbide slag is used for phosphoric acid by wet process desulfurization |
| CN106831002A (en) * | 2017-01-20 | 2017-06-13 | 昆明川金诺化工股份有限公司 | A kind of granular double superhosphate energy-saving production method |
| CN111086977B (en) * | 2019-12-31 | 2021-07-06 | 贵州新东浩化工材料科技有限公司 | Method for preparing MCP and MDCP (Madin-Darby Canine phosphate) by using raffinate acid |
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|---|---|---|---|---|
| CN101264873A (en) * | 2008-04-11 | 2008-09-17 | 李进 | Method for producing feed-grade calcium phosphate |
| CN102815681A (en) * | 2012-06-21 | 2012-12-12 | 中化云龙有限公司 | Method for producing feed-grade calcium dihydrogen phosphate from wet-process phosphoric acid |
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