CN109384208A - A kind of the step application method and system of phosphor ammonium slurry - Google Patents
A kind of the step application method and system of phosphor ammonium slurry Download PDFInfo
- Publication number
- CN109384208A CN109384208A CN201811567073.3A CN201811567073A CN109384208A CN 109384208 A CN109384208 A CN 109384208A CN 201811567073 A CN201811567073 A CN 201811567073A CN 109384208 A CN109384208 A CN 109384208A
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- China
- Prior art keywords
- mother liquor
- tank
- strainer
- drying cylinder
- phosphor ammonium
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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
Abstract
The present invention proposes the step application method and system of a kind of phosphor ammonium slurry, using the full water-soluble of material in mother liquor, carries out atomization drying to mother liquor, produces water-soluble phosphoric acid monoammonium.Now production nutrient control (is mainly influenced by the crystallization yield of industrial grade monoammonium phosphate) in 60%-64%.The program can reduce influence of the mother liquor to system, can adequately utilize products material effectively using the nutrient in mother liquor.
Description
Technical field
The present invention relates to monoammonium phosphate production field more particularly to the step application methods and system of a kind of phosphor ammonium slurry.
Background technique
Since the existing more Wet Processes of Phosphoric Acid in the country does not all carry out phosphoric acid purification, produce in monoammonium phosphate, phosphorus ammonia slurry meeting
With more impurity, and these impurity carried out merely in phosphorus ammonia slurry separation do not meet present environmental requirement and company at
This control.Utilization for phosphorus ammonia slurry, now more production technology are second level utilization, the main knot for producing nutrient and being 73%
The fertilizer grade powdery monoammonium phosphate of brilliant industrial grade monoammonium phosphate and nutrient 55%, as shown in Figure 1.But the Land use systems, not
In continuous crystallisation production, the crystalline mother solution of generation is because of SO4 2-Enrichment can not return to crystallization production system and utilize, but arrive fertilizer grade
The production of chemical fertilizer excessively wastes industrial chemicals again.A kind of improvement project was once used to this, as shown in Fig. 2, returning using mother liquor dilute
Phosphoric acid storage tank returns to production system after diluted acid mixing desulfurization, then with diluted acid together.But in the program, pass through in mother liquor
When desulfurization is mixed in ore pulp, although SO4 2-It is sloughed by Ca, Mg plasma in ore pulp, but ore pulp and NH in mother liquor simultaneously4H2PO4
It reacts, the NH4 in mother liquor+Aluminum phosphate iron complex, and the network formed can be formed with Al, Fe in ore pulp in acid condition
Object is closed after same ore pulp mix common sedimentation, it is hardened to will form subsider bottom, influences the diluted acid desulfurization production cycle.
Summary of the invention
The purpose of the present invention is to propose to the step application method and system of a kind of phosphor ammonium slurry, using in mother liquor material it is complete
Water solubility carries out atomization drying to mother liquor, produces water-soluble phosphoric acid monoammonium.
The present invention is achieved through the following technical solutions:
A kind of step application method of phosphor ammonium slurry, for handling in discontinuous crystallization production, the crystalline mother solution of generation,
The following steps are included:
A, the mother liquor that centrifuge separation generates is delivered to heating tank and is heated to 80 DEG C of concentrations；
B, the mother liquor after being concentrated in step A is delivered to crystallizing tank by pump, passes through the rotary sprayer at the top of crystallizing tank
It is sprayed onto crystallization on fluidized bed and forms monoammonium phosphate crystal；
C, it is packed after the monoammonium phosphate crystal generated in step B being delivered to drying cylinder drying.
Preferably, the monoammonium phosphate crystal formed in the step B is entered back into after filter screen selects in step C.
A kind of step application system of phosphor ammonium slurry, including mother liquor hold tank, mother liquor hold tank pass through the first conveyance conduit
It is connected to heating tank top, exhaust pipe is provided at the top of heating tank, heating pot bottom is arranged the second conveyance conduit and is connected to knot
The rotary sprayer of brilliant tank, rotary sprayer are arranged in the top of crystallizing tank, fluidized bed, crystallizing tank are arranged below rotary sprayer
Discharge gate is arranged in bottom, and discharge gate, which goes out, is provided with conveyer belt, and the conveyer belt other end connects drying cylinder, and the drying cylinder other end is provided
Material mouth.
Preferably, the drying cylinder uses steam heat-exchanging seasoning.
Preferably, described conveyer belt one end connects discharge gate, the other end is connected to elevator, lift outlet connection filter
Net, strainer, which is divided under strainer upper outlet and strainer, to be exported, and strainer upper outlet is connected to crusher, and crusher outlet is connected to promotion
Machine, outlet is connected to drying cylinder under strainer.
This method to mother liquor carry out using only, using the full water-soluble of material in mother liquor, atomization drying is carried out to mother liquor,
Water-soluble phosphoric acid monoammonium is produced, now produces nutrient control in 60%-64% (mainly by the crystallization yield shadow of industrial grade monoammonium phosphate
It rings).The program can reduce influence of the mother liquor to system effectively using the nutrient in mother liquor, can adequately utilize production
Product raw material.
Detailed description of the invention
Fig. 1 is to produce the process flow chart that phosphorus ammonia slurry second level utilizes in monoammonium phosphate in the prior art in the present invention.
Fig. 2 is the technique for producing the improvement project that phosphorus ammonia slurry second level utilizes in monoammonium phosphate in the present invention in the prior art
Flow chart.
Fig. 3 is a kind of process flow chart of the step application method of phosphor ammonium slurry in the present invention.
Fig. 4 is a kind of production line schematic diagram of the step application system of phosphor ammonium slurry in the present invention.
Appended drawing reference is as follows:
1, mother liquor hold tank, the 2, first conveyance conduit, 3, heating tank, 4, exhaust pipe, the 5, second conveyance conduit, 6, crystallization
Tank, 7, conveyer belt, 8, drying cylinder, 9, elevator, 10, strainer, 11, crusher, 12, fluidized bed, 13, rotary sprayer, 14, change
Hot cylinder.
Specific embodiment
In order to make the objectives, technical solutions, and advantages of the present invention clearer, with reference to the accompanying drawings and embodiments, right
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.
As shown in figure 3, a kind of step application method of phosphor ammonium slurry is generated for handling in discontinuous crystallization production
Crystalline mother solution, comprising the following steps:
A, the mother liquor that centrifuge separation generates is delivered to heating tank 3 and is heated to 80 DEG C of concentrations；
B, the mother liquor after being concentrated in step A is delivered to crystallizing tank 6 by pump, passes through the rotating spraying at 6 top of crystallizing tank
Device 13 is sprayed onto crystallization on fluidized bed 12 and forms monoammonium phosphate crystal；
C, it is packed after the monoammonium phosphate crystal generated in step B being delivered to the drying of drying cylinder 8.
Preferably, the monoammonium phosphate crystal formed in the step B is entered back into after filter screen selects in step C.
As shown in figure 4, a kind of step application system of phosphor ammonium slurry, including mother liquor hold tank 1, mother liquor hold tank 1 pass through
First conveyance conduit 2 is connected to 3 top of heating tank, and exhaust pipe 4,3 bottom of heating tank setting second are provided at the top of heating tank 3
Conveyance conduit 5 is connected to the rotary sprayer 13 of crystallizing tank 6, and the top of crystallizing tank 6, rotating spraying is arranged in rotary sprayer 13
Fluidized bed 12 is set below device 13, and discharge gate is arranged in 6 bottom of crystallizing tank, and discharge gate goes out to be provided with conveyer belt 7, and conveyer belt 7 is another
Discharge port is arranged in end connection drying cylinder 8,8 other end of drying cylinder.
Preferably, the drying cylinder 8 uses steam heat-exchanging seasoning, the outside of drying cylinder 8 is provided with heat exchanger tube 14,
Steam is passed through inside heat exchanger tube 14 for exchanging heat, steam is passed through from bottom, is discharged from top, and arrow indicates airflow direction in Fig. 4.
Preferably, described 7 one end of conveyer belt connects discharge gate, the other end is connected to elevator 9, and the outlet of elevator 9 connects
Strainer 10 is connect, strainer, which is divided under strainer upper outlet and strainer, to be exported, and strainer upper outlet is connected to crusher 11, and crusher outlet connects
It is connected to elevator 9, outlet is connected to drying cylinder 8 under strainer.
When specifically used, the principle of crystallizing tank 6 be concentration after mother liquor flow into be located at make in the rotary sprayer 13 of tower top
Spraying at drop again, drop decline process at the top of high tower is contacted with cold fluidized bed 12, keen draft self-fluidized type bed 12 it is more
Orifice plate is passed through, and making returning charge and granule materials in fluidized bed 12 as crystal seed is in fluidization.At the same time, it would be desirable to which granulation is melted
Material or slurry, solution are coated on seed surface after being atomized into particle with compressed air, form thin film.Because of fluidised object
Material continuous tumbling motion in fluidized bed 12 is conducive to the progress of heat and mass transport so gas, affixed touching are well.Such as charging
For melt, then the melt film that seed surface is applied will solidify quickly.If charging is slurry or solution, then crystal seed table is coated on
Layered material slurry or solution on face will be dried because moisture evaporates rapidly.So constantly it is repeated, crystal seed is gradually grown up, to
Self-fluidized type bed 12 flows out after particle reaches requirement.Its subsequent process is identical as other prillings.The bulky grain screened out
It is recycled after rejoining heater together as returning charge with fine powder after crusher 11 is broken.Fluidized bed 12 and rotating spraying
The specific structure of device 13 is referred to the prior art.
From economic benefit, existing workshop mother liquor is averaged 5m3/ h, density 1.3.The control of mother liquor amount, the phosphorus ammonia slurry step
By in the way of, using mother liquor produce water-soluble phosphoric acid monoammonium 2.4t/h.Existing market water-soluble phosphoric acid monoammonium (60-64) price
Between 2850-2950.
Save mother liquor gross profit are as follows: 2.4 × 2850=6840 member/h.
Its drying cost are as follows:
Combustion gas cost: 2.78 × 200=556 member/h (the step charging standard for not considering natural gas)
Power consumption: 0.55 × 360=198 member/h
Because mother liquor has been calculated using its cost into industrial grade monoammonium phosphate finished product, therefore put aside its cost of material.The phosphorus
The cascade utilization of ammonia slurry can produce economic benefit: (6840-556-198) × 7000=4260.2w member.
Described is only presently preferred embodiments of the present invention, is not intended to limit the invention, it is all in spirit of the invention and
Made any modifications, equivalent replacements, and improvements etc., should all be included in the protection scope of the present invention within principle.
Claims (5)
1. a kind of step application method of phosphor ammonium slurry, for handling in discontinuous crystallization production, the crystalline mother solution of generation,
It is characterized in that, comprising the following steps:
A, the mother liquor that centrifuge separation generates is delivered to heating tank and is heated to 80 DEG C of concentrations；
B, the mother liquor after being concentrated in step A is delivered to crystallizing tank by pump, is sprayed by the rotary sprayer at the top of crystallizing tank
Crystallization forms monoammonium phosphate crystal on to fluidized bed；
C, it is packed after the monoammonium phosphate crystal generated in step B being delivered to drying cylinder drying.
2. a kind of step application method of phosphor ammonium slurry as described in claim 1, which is characterized in that formed in the step B
Monoammonium phosphate crystal entered back into after filter screen selects in step C.
3. a kind of step application system of phosphor ammonium slurry, which is characterized in that including mother liquor hold tank, mother liquor hold tank passes through first
Conveyance conduit is connected to heating tank top, and exhaust pipe is provided at the top of heating tank, and the second conveyance conduit is arranged in heating pot bottom
It is connected to the rotary sprayer of crystallizing tank, the top of crystallizing tank is arranged in rotary sprayer, setting fluidisation below rotary sprayer
Discharge gate is arranged in bed, crystallization pot bottom, and discharge gate, which goes out, is provided with conveyer belt, and the conveyer belt other end connects drying cylinder, and drying cylinder is another
Discharge port is arranged in one end.
4. a kind of step application system of phosphor ammonium slurry as claimed in claim 3, which is characterized in that the drying cylinder is using steaming
Vapour heat exchange seasoning.
5. a kind of step application system of phosphor ammonium slurry as claimed in claim 3, which is characterized in that described conveyer belt one end connects
Run in material mouth, the other end is connected to elevator, and lift outlet connects strainer, and strainer is divided under strainer upper outlet and strainer
Mouthful, strainer upper outlet is connected to crusher, and crusher outlet is connected to elevator, and outlet is connected to drying cylinder under strainer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811567073.3A CN109384208A (en) | 2018-12-20 | 2018-12-20 | A kind of the step application method and system of phosphor ammonium slurry |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811567073.3A CN109384208A (en) | 2018-12-20 | 2018-12-20 | A kind of the step application method and system of phosphor ammonium slurry |
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| CN109384208A true CN109384208A (en) | 2019-02-26 |
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| CN201811567073.3A Pending CN109384208A (en) | 2018-12-20 | 2018-12-20 | A kind of the step application method and system of phosphor ammonium slurry |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1063311A (en) * | 1990-12-17 | 1992-08-05 | 阿切尔丹尼尔斯密德兰公司 | The method for preparing granular L-lysine |
| RU2368567C1 (en) * | 2008-05-29 | 2009-09-27 | Закрытое акционерное общество "Научно-производственная компания "Интерфос" | Method of obtaining edible ammonium phosphates |
| CN102674282A (en) * | 2012-05-16 | 2012-09-19 | 瓮福（集团）有限责任公司 | Method for producing granular monoammonium phosphate |
| CN202808364U (en) * | 2012-05-16 | 2013-03-20 | 瓮福（集团）有限责任公司 | Equipment for producing granular monoammonium phosphate from crystal ammonium phosphate filter residue and mother liquid |
| CN103130205A (en) * | 2013-03-11 | 2013-06-05 | 马光明 | Method for producing industrial monoammonium phosphate and coproducing water-soluble ammonium sulfate phosphate |
| CN103303887A (en) * | 2013-05-28 | 2013-09-18 | 瓮福（集团）有限责任公司 | Method for producing high-nutrient monoammonium phosphate by dual-tube reverse process |
| CN104058378A (en) * | 2014-07-09 | 2014-09-24 | 昆明隆祥化工有限公司 | Method for producing monoammonium phosphate and magnesium ammonium phosphate by using wet concentrated phosphoric acid residues |
| CN105036852A (en) * | 2015-07-14 | 2015-11-11 | 湖北三宁化工股份有限公司 | Method for producing macroelement water-soluble fertilizer by using industrial grade monoammonium phosphate mother liquor |
-
2018
- 2018-12-20 CN CN201811567073.3A patent/CN109384208A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1063311A (en) * | 1990-12-17 | 1992-08-05 | 阿切尔丹尼尔斯密德兰公司 | The method for preparing granular L-lysine |
| RU2368567C1 (en) * | 2008-05-29 | 2009-09-27 | Закрытое акционерное общество "Научно-производственная компания "Интерфос" | Method of obtaining edible ammonium phosphates |
| CN102674282A (en) * | 2012-05-16 | 2012-09-19 | 瓮福（集团）有限责任公司 | Method for producing granular monoammonium phosphate |
| CN202808364U (en) * | 2012-05-16 | 2013-03-20 | 瓮福（集团）有限责任公司 | Equipment for producing granular monoammonium phosphate from crystal ammonium phosphate filter residue and mother liquid |
| CN103130205A (en) * | 2013-03-11 | 2013-06-05 | 马光明 | Method for producing industrial monoammonium phosphate and coproducing water-soluble ammonium sulfate phosphate |
| CN103303887A (en) * | 2013-05-28 | 2013-09-18 | 瓮福（集团）有限责任公司 | Method for producing high-nutrient monoammonium phosphate by dual-tube reverse process |
| CN104058378A (en) * | 2014-07-09 | 2014-09-24 | 昆明隆祥化工有限公司 | Method for producing monoammonium phosphate and magnesium ammonium phosphate by using wet concentrated phosphoric acid residues |
| CN105036852A (en) * | 2015-07-14 | 2015-11-11 | 湖北三宁化工股份有限公司 | Method for producing macroelement water-soluble fertilizer by using industrial grade monoammonium phosphate mother liquor |
Non-Patent Citations (3)
| Title |
|---|
| 姚礼炳: "流化床喷雾造粒装置", 医药工程设计, no. 6, pages 6 - 10 * |
| 庄艳萍: "湿法磷酸制备工业级磷酸一铵试验研究", 磷肥与复肥, vol. 24, no. 5, pages 14 - 16 * |
| 王毕德等: "工业磷铵母液制备工业磷酸一铵的工艺研究", 无机盐工业, vol. 49, no. 10, pages 46 - 48 * |
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