CN218188871U - Material circulating system for iron phosphate synthesis - Google Patents
Material circulating system for iron phosphate synthesis Download PDFInfo
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- CN218188871U CN218188871U CN202123304402.5U CN202123304402U CN218188871U CN 218188871 U CN218188871 U CN 218188871U CN 202123304402 U CN202123304402 U CN 202123304402U CN 218188871 U CN218188871 U CN 218188871U
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Abstract
The utility model relates to a material circulation system for ferric phosphate is synthetic relates to the synthetic technical field of ferric phosphate, spray absorption tower and ammonia jar including ferrous sulfate edulcoration reactor, ferric phosphate synthesis reactor, filter equipment, ammonia, ferric phosphate synthesis reactor is connected with filter equipment, filter equipment keeps away from the one end and the ammonia of ferric phosphate synthesis reactor and sprays the absorption tower and be connected, ferrous sulfate edulcoration reactor one end sprays the absorption tower with the ammonia and is connected, the ferrous sulfate edulcoration reactor other end is connected with the ferric phosphate synthesis reactor, the ammonia jar is used for providing the aqueous ammonia to ferrous sulfate edulcoration reactor. This application can unify the processing to ammonia, solid waste and acid waste liquid, saves the treatment cost, and convenient operation improves the treatment effeciency.
Description
Technical Field
The application relates to the technical field of iron phosphate synthesis, in particular to a material circulation system for iron phosphate synthesis.
Background
At present, the main synthesis method of iron phosphate is a controlled precipitation method, which uses ferrous sulfate as a by-product of titanium dioxide as a raw material, dissolves the ferrous sulfate, adds ammonia water to remove impurities and filters to obtain a base solution, then adds phosphate or phosphoric acid at a certain temperature to obtain ferric phosphate dihydrate, and the ferric phosphate dihydrate is calcined at a certain temperature to obtain an iron phosphate product. By controlling parameters such as pH value, reaction temperature, stirring speed, phosphorus source types, phosphorus source adding speed, calcining temperature, time and the like, iron phosphate products with different iron-phosphorus ratios, morphologies and particle size distributions can be obtained.
In the iron phosphate synthesis process, ammonia gas, solid waste after impurity removal, acidic waste liquid and other various wastes can be generated, and the currently mainstream method is to add an ammonia recovery device in the impurity removal stage and separately treat the solid waste and the acidic waste liquid.
However, in the actual operation process, the inventor finds that the ammonia recovery device can only recover ammonia alone, is difficult to recover ammonia, solid waste and acidic waste liquid in a unified way, is easy to cost a large amount of production cost, and causes huge economic burden to enterprises.
SUMMERY OF THE UTILITY MODEL
In order to improve the problem that ammonia, solid waste and acid waste liquid are handled respectively and are leaded to the treatment cost to increase, this application provides a material circulation system for ferric phosphate is synthetic.
The application provides a material circulation system for ferric phosphate is synthetic adopts following technical scheme:
the utility model provides a material circulation system for ferric phosphate is synthetic, includes ferrous sulfate edulcoration reactor, ferric phosphate synthesis reactor, filter equipment, ammonia and sprays the absorption tower and the aqua ammonia jar, the ferric phosphate synthesis reactor is connected with filter equipment, filter equipment keeps away from the one end of ferric phosphate synthesis reactor and sprays the absorption tower with the ammonia and be connected, ferrous sulfate edulcoration reactor one end sprays the absorption tower with the ammonia and is connected, the ferrous sulfate edulcoration reactor other end is connected with the ferric phosphate synthesis reactor, the aqua ammonia jar is used for providing the aqueous ammonia to ferrous sulfate edulcoration reactor.
Through adopting above-mentioned technical scheme, the aqueous ammonia jar carries the aqueous ammonia in to ferrous sulfate edulcoration reactor, the aqueous ammonia takes place chemical reaction with ferrous sulfate and produces ammonia and base liquor, the ammonia gets into ammonia spray absorption tower, the base liquor gets into in the iron phosphate synthesis reactor and takes place chemical reaction with phosphate or phosphoric acid and generates the iron phosphate, solid waste and acid waste liquid, filter equipment filters the sifting out to fixed discarded object, acid waste liquid gets into ammonia spray absorption tower and ammonia and takes place neutralization chemical reaction, acid waste liquid absorbs the ammonia, and then the completion is to the ammonia, solid waste and acid waste liquid carry out unified processing, save the treatment cost, and convenient for operation, and the treatment effeciency is improved.
Preferably, the ammonia spraying absorption tower comprises an air inlet end, an liquid outlet end, a plurality of packing layers and a plurality of spraying pieces arranged corresponding to the packing layers, the packing layers and the spraying pieces are located between the air inlet end and the liquid outlet end, and the spraying pieces are connected with one end, far away from the iron phosphate synthesis reactor, of the filtering device.
Through adopting above-mentioned technical scheme, the inlet end is used for supplying the ammonia to get into, sprays the piece and sprays the acid waste liquid to the packing layer on, the ammonia carries out chemical reaction with the acid waste liquid on the packing layer, generates the aqueous ammonia, goes out the liquid end and is used for discharging the aqueous ammonia, convenient operation saves the resource, effectively improves the reuse ability of resource.
Preferably, the spraying pieces and the filler layers are arranged alternately.
By adopting the technical scheme, the spraying pieces and the filler layers are alternately arranged, so that on one hand, the contact area of ammonia and acidic waste liquid is conveniently increased, and the chemical reaction rate is increased; on the other hand, the arrangement of the spraying pieces can be optimized, and the attractiveness of the ammonia gas spraying absorption tower is improved.
Preferably, a gas outlet and a liquid outlet are arranged on the ferrous sulfate impurity removal reactor, the gas outlet is connected with the ammonia gas spraying absorption tower through a conversion assembly, and a ferrous sulfate liquid storage tank is connected between the liquid outlet and the iron phosphate synthesis reactor.
By adopting the technical scheme, ammonia gas generated by the ferrous sulfate impurity removal reactor is discharged through the gas outlet, and enters the ammonia gas spray absorption tower through the conversion assembly after being discharged from the gas outlet; the base solution generated by the ferrous sulfate impurity removal reactor enters the ferrous sulfate liquid storage tank through the liquid outlet for storage, so that the possibility of leakage of the ferrous sulfate solution is reduced.
Preferably, the conversion assembly comprises a tee joint and a first air pump, one way of the tee joint, which is far away from the air outlet pipe, is connected with the ammonia gas spraying absorption tower, the other way of the tee joint, which is far away from the air outlet pipe, is connected with the first air pump, and one end of the first air pump, which is far away from the tee joint, is connected with the air inlet end.
Through adopting above-mentioned technical scheme, the ammonia directly gets into ammonia and sprays the absorption tower, is absorbed by the acid waste liquid, and the remaining ammonia that does not absorb loops through tee bend and first air pump and gets into again and spray the absorption tower, realizes that the acid waste liquid absorbs the circulation of ammonia.
Preferably, the ferrous sulfate impurity removal reactor is connected with an ammonia liquid recovery tank, and one end of the ammonia liquid recovery tank, which is far away from the ferrous sulfate impurity removal reactor, is connected with the liquid outlet end.
Through adopting above-mentioned technical scheme, ammonia and acid waste liquid take place chemical reaction and produce the aqueous ammonia in the ammonia sprays the absorption tower, and the aqueous ammonia sprays the absorption tower through going out liquid end exhaust ammonia, gets into the ammonia liquor recovery jar from going out liquid end exhaust aqueous ammonia, accomplishes the recovery to the ammonia liquor, is convenient for reuse environmental protection and energy saving to the ammonia liquor.
Preferably, an acidic waste liquid storage tank is connected between the filtering device and the ammonia gas spraying absorption tower, the acidic waste liquid storage tank is used for storing acidic waste liquid filtered by the filtering device, and the acidic waste liquid storage tank is connected with the spraying piece through a first liquid pump.
By adopting the technical scheme, the acidic waste liquid storage tank stores the acidic waste liquid, so that the possibility of leakage of the waste liquid is reduced, and further the pollution to the environment is reduced; the first liquid pump is used for sucking the acidic waste liquid in the acidic waste liquid storage tank into the spraying piece, and then the spraying water pressure of the spraying piece is improved.
Preferably, an ammonia gas outlet is formed in the iron phosphate synthesis reactor, and the ammonia gas outlet is connected with the spraying piece through a second air pump.
Through adopting above-mentioned technical scheme, the ammonia that produces among the iron phosphate synthesis reactor wears out the ammonia export and gets into under the suction effect of second air pump and spray in the piece, further strengthens the water pressure that sprays of spraying on the one hand, and on the other hand can also reduce leaking of ammonia, resources are saved.
In summary, the present application includes at least one of the following beneficial technical effects:
the ammonia water tank conveys ammonia water into the ferrous sulfate impurity removal reactor, the ammonia water and ferrous sulfate undergo a chemical reaction to generate ammonia gas and base liquid, the ammonia gas enters an ammonia gas spraying absorption tower, the base liquid enters an iron phosphate synthesis reactor and undergoes a chemical reaction with phosphate or phosphoric acid to generate iron phosphate, solid waste and acidic waste liquid, a filtering device filters and screens out fixed waste, the acidic waste liquid enters the ammonia gas spraying absorption tower and undergoes a neutralization chemical reaction with the ammonia gas, the acidic waste liquid absorbs the ammonia gas, and then the ammonia gas, the solid waste and the acidic waste liquid are treated in a unified way, so that the treatment cost is saved, the operation is convenient, and the treatment efficiency is improved;
the ammonia gas directly enters the ammonia gas spray absorption tower and is absorbed by the acidic waste liquid, and the unabsorbed residual ammonia gas sequentially passes through the tee joint and the first air pump and reenters the spray absorption tower, so that the cyclic absorption of the acidic waste liquid on the ammonia gas is realized;
the ammonia gas that produces among the iron phosphate synthesis reactor wears out the ammonia export and gets into under the suction effect of second air pump and spray in the piece, further strengthens the spraying water pressure that sprays the piece on the one hand, and on the other hand can also reduce leaking of ammonia, resources are saved.
Drawings
Fig. 1 is a schematic structural diagram for embodying the whole circulation system in the embodiment of the present application.
Description of reference numerals: 1. a ferrous sulfate impurity removal reactor; 11. an air outlet; 12. a liquid outlet; 13. a conversion component; 131. a tee joint; 132. a first air pump; 133. a third air pump; 14. a third liquid pump; 2. an iron phosphate synthesis reactor; 21. an ammonia gas outlet; 22. a second air pump; 23. a fifth liquid pump; 3. a filtration device; 4. ammonia gas sprays the absorber; 41. an air inlet end; 42. a liquid outlet end; 43. a first filler layer; 44. a second packing layer; 45. spraying parts; 451. a first sprayer; 452. a second sprayer; 46. a sixth liquid pump; 5. an ammonia tank; 51. a second liquid pump; 6. a ferrous sulfate liquid storage tank; 61. a fourth liquid pump; 7. an ammonia liquor recovery tank; 71. a seventh liquid pump; 8. storing the acidic waste liquid; 81. a first liquid pump.
Detailed Description
The present application is described in further detail below with reference to fig. 1.
The embodiment of the application discloses a material circulation system for iron phosphate synthesis. Referring to fig. 1, a material circulation system for iron phosphate synthesis comprises a ferrous sulfate impurity removal reactor 1, an iron phosphate synthesis reactor 2, a filtering device 3, an ammonia gas spray absorption tower 4, an ammonia water tank 5, the ammonia water tank 5 and matched gas path and liquid path equipment. The output end of the ammonia water tank 5 is connected with the ferrous sulfate impurity removal reactor 1 and is used for injecting ammonia water into the ferrous sulfate impurity removal reactor 1. One end of the output end of the ferrous sulfate impurity removal reactor 1 is connected with the iron phosphate synthesis reactor 2, and the other end is connected with the ammonia gas spray absorption tower 4. The output end of the iron phosphate synthesis reactor 2 is connected with an ammonia gas spraying absorption tower 4 through a filtering device 3, and the filtering device 3 is used for filtering solid waste generated in the iron phosphate synthesis reactor 2. An ammonia water tank 5, a ferrous sulfate impurity removal reactor 1, an iron phosphate synthesis reactor 2, a filtering device 3 and a nitrogen spray absorption tower are connected to form a closed loop.
When the device works, ammonia water in the ammonia water tank 5 is injected into the ferrous sulfate impurity removal reactor 1, the ammonia water and the ferrous sulfate undergo a chemical reaction to generate ammonia gas and a base solution containing the ferrous sulfate, the base solution containing the ferrous sulfate is injected into the iron phosphate synthesis reactor 2, and the base solution containing the ferrous sulfate undergoes a chemical reaction with phosphate to generate iron phosphate, solid waste, acidic waste liquid and a small amount of ammonia gas. Filter equipment 3 filters solid waste and separates out, and acid waste liquid continues to pour into ammonia and sprays the absorption tower 4, and the ammonia that ferrous sulfate edulcoration reactor 1 generated lets in ammonia and sprays the absorption tower 4, and acid waste liquid absorbs the ammonia, finally accomplishes the unified processing to ammonia, solid waste and acid waste liquid, saves the treatment cost, and convenient operation improves the treatment effeciency.
Referring to fig. 1, install second liquid pump 51 between aqueous ammonia jar 5 and the ferrous sulfate edulcoration reactor 1, second liquid pump 51 is arranged in pouring into ferrous sulfate edulcoration reactor 1 with the aqueous ammonia in aqueous ammonia jar 5, the aqueous ammonia carries out the edulcoration to the ferrous sulfate solution after taking place chemical reaction with ferrous sulfate, generate ammonia and the base solution that contains ferrous sulfate after the edulcoration, liquid outlet 12 has been seted up to the bottom of ferrous sulfate edulcoration reactor 1, liquid outlet 12 department is connected with third liquid pump 14, the output of third liquid pump 14 is connected with ferrous sulfate liquid storage pot 6, third liquid pump 14 is used for pouring into the ferrous sulfate liquid storage pot 6 with the base solution that contains ferrous sulfate after the edulcoration and stores and stews, reduce the possibility that the ferrous sulfate solution leaked, resources are saved. A fourth liquid pump 61 is connected between the ferrous sulfate liquid storage tank 6 and the iron phosphate synthesis reactor 2, the fourth liquid pump 61 is used for injecting the supernatant in the ferrous sulfate liquid storage tank 6 into the iron phosphate synthesis reactor 2, and the base solution containing ferrous sulfate and phosphate undergo a chemical reaction to generate iron phosphate, solid waste, acidic waste liquid and a small amount of ammonia gas.
Referring to fig. 1, an ammonia gas outlet 21 is formed in the iron phosphate synthesis reactor 2, the ammonia gas outlet 21 is located at the upper end of the iron phosphate synthesis reactor 2, the ammonia gas outlet 21 is connected to a second air pump 22, and the bottom of the iron phosphate synthesis reactor 2 is connected to a fifth liquid pump 23. The output end of the fifth liquid pump 23 is connected with the filtering device 3, in the embodiment of the present application, the filtering device 3 adopts a plate-and-frame filter, and the filtering device 3 is used for filtering the solid waste in the iron phosphate synthesis reactor 2. The end of the filter device 3 remote from the fifth liquid pump 23 is connected to an acidic waste liquid storage tank 8, and the acidic waste liquid storage tank 8 is used for storing acidic waste liquid. The output end of the acidic waste liquid storage tank 8 is connected with a first liquid pump 81, the output end of the first liquid pump 81 and the output end of the second air pump 22 are connected with a spraying piece 45, and the spraying piece 45 is used for spraying the acidic waste liquid into the ammonia spraying absorption tower 4. The spraying part 45 sequentially comprises a first sprayer 451 and a second sprayer 452 from top to bottom, a first filler layer 43 and a second filler layer 44 are arranged in the ammonia gas spraying absorption tower 4, the first filler layer 43 is positioned above the second filler layer 44, the first filler layer 43 is positioned between the first sprayer 451 and the second sprayer 452, and the second filler layer 44 is positioned below the second sprayer 452. The first packing layer 43 and the second packing layer 44 may be made of ceramic, metal, or plastic, and in the embodiment of the present invention, a corrosion-resistant polypropylene material is used. First sprayer 451 sprays the acidic waste liquid onto first packing layer 43, and second sprayer 452 sprays the acidic waste liquid onto second packing layer 44 for the acidic waste liquid evenly distributed is on first packing layer 43 and second packing layer 44, increases the area of contact of acidic waste liquid and air, makes the gas-liquid mixture even.
Referring to fig. 1, in order to improve the absorption efficiency of ammonia, a conversion assembly 13 is connected between the ferrous sulfate impurity removal reactor 1 and the ammonia spray absorption tower 4, the conversion assembly 13 includes a third air pump 133 and a tee joint 131, an air outlet 11 is arranged at the upper end of the ferrous sulfate impurity removal reactor 1, an input end of the third air pump 133 is communicated with the air outlet 11, the tee joint 131 is connected with an output end of the third air pump 133, one end of the tee joint 131 far away from the third air pump 133 is connected with the bottom of the ammonia spray absorption tower 4, an air inlet 41 is arranged at the upper part of the ammonia spray absorption tower 4, the other end of the tee joint 131 far away from the third air pump 133 is connected with the air inlet 41 through a first air pump 132, so that ammonia enters from the upper part and the bottom of the ammonia spray absorption tower 4 respectively, so that ammonia is in full contact with a first filler layer 43 and a second filler layer 44, the contact area of ammonia and acidic waste liquid is increased, so that the absorption rate of the acidic waste liquid on ammonia is accelerated, and the treatment efficiency is improved.
Referring to fig. 1, a liquid outlet end 42 is arranged at the bottom of the ammonia gas spraying absorption tower 4, a sixth liquid pump 46 is connected to the liquid outlet end 42, an output end of the sixth liquid pump 46 is connected to the ammonia liquid recovery tank 7, the sixth liquid pump 46 is used for extracting ammonia liquid which is subjected to chemical reaction in the ammonia gas spraying absorption tower 4 and injecting the ammonia liquid into the ammonia liquid recovery tank 7, and the ammonia liquid recovery tank 7 is used for recovering and storing the ammonia liquid. In order to improve the secondary utilization rate of resources, a seventh liquid pump 71 is connected between the ammonia liquid recovery tank 7 and the ferrous sulfate impurity removal reactor 1, and the seventh liquid pump 71 is used for extracting the ammonia liquid in the ammonia liquid recovery tank 7 and injecting the ammonia liquid into the ferrous sulfate impurity removal reactor 1 to participate in impurity removal reaction, so that the ammonia liquid is recycled, and the energy-saving and environment-friendly effects are realized.
The implementation principle of the material circulation system for iron phosphate synthesis in the embodiment of the application is as follows: during operation, firstly, the second liquid pump 51 pumps the ammonia water in the ammonia water tank 5, and injects the ammonia water into the ferrous sulfate impurity removal reactor 1 for impurity removal, so as to generate ammonia gas and a base solution containing ferrous sulfate after impurity removal. The third liquid pump 14 extracts the base solution containing ferrous sulfate and injects the base solution into the ferrous sulfate storage tank 6 for standing. The fourth liquid pump 61 extracts the supernatant in the ferrous sulfate liquid storage tank 6 and injects the supernatant into the iron phosphate synthesis reactor 2, and the ferrous sulfate and the phosphate in the iron phosphate synthesis reactor 2 undergo a chemical reaction to generate iron phosphate, solid waste, acidic waste liquid and a small amount of ammonia gas. The fifth liquid pump 23 pumps the acidic waste liquid and the solid waste in the iron phosphate synthesis reactor 2 and injects the pumped acidic waste liquid and the solid waste into the filter device 3, the filter device 3 filters the solid waste, and the filtered acidic waste liquid flows into the acidic waste liquid storage tank 8. The first liquid pump 81 pumps the acidic waste liquid in the acidic waste liquid storage tank 8 and transfers the acidic waste liquid to the first sprayer 451 and the second sprayer 452, and at the same time, the second air pump 22 pumps a small amount of ammonia gas generated in the iron phosphate synthesis reactor 2 and injects the ammonia gas into the first sprayer 451 and the second sprayer 452.
Secondly, the ammonia gas that produces in the ferrous sulfate edulcoration reactor 1 is extracted and is carried towards ammonia spraying absorption tower 4 to third air pump 133, a part of ammonia gas directly injects the ammonia gas through tee 131 and sprays the recovery tower into ammonia gas, first air pump 132 extracts the ammonia gas through another part of another route of tee 131 and injects into ammonia gas spraying reactor, first spray thrower 451 sprays the acid waste liquid to first packing layer 43, second spray thrower 452 sprays the acid waste liquid to second packing layer 44, the ammonia gas contacts with first packing layer 43 and second packing layer 44 respectively, make the acid waste liquid absorb the ammonia gas, reduce the possibility that the ammonia gas leaked. The ammonia gas and the acidic waste liquid are subjected to chemical reaction to generate ammonia liquid which falls into the bottom of the ammonia gas spraying and recovering tower.
And finally, the sixth liquid pump 46 extracts the ammonia liquid in the ammonia spraying absorption tower 4 and injects the ammonia liquid into the ammonia liquid recovery tank 7, and the seventh liquid pump 71 extracts the ammonia liquid in the ammonia liquid recovery tank 7 and injects the ammonia liquid into the ferrous sulfate impurity removal reactor 1, so that a circulation loop is formed finally, the reuse of the ammonia liquid is improved, and resources are saved.
The above are preferred embodiments of the present application, and the scope of protection of the present application is not limited thereto, so: equivalent changes in structure, shape and principle of the present application shall be covered by the protection scope of the present application.
Claims (8)
1. A material circulation system for iron phosphate synthesis is characterized in that: including ferrous sulfate edulcoration reactor (1), iron phosphate synthesis reactor (2), filter equipment (3), ammonia spray absorption tower (4) and aqua ammonia jar (5), iron phosphate synthesis reactor (2) are connected with filter equipment (3), the one end that iron phosphate synthesis reactor (2) were kept away from in filter equipment (3) sprays absorption tower (4) with the ammonia and is connected, ferrous sulfate edulcoration reactor (1) one end is connected with ammonia spray absorption tower (4), ferrous sulfate edulcoration reactor (1) other end is connected with iron phosphate synthesis reactor (2), aqua ammonia jar (5) are used for providing the aqueous ammonia to ferrous sulfate edulcoration reactor (1).
2. The material circulation system for iron phosphate synthesis according to claim 1, characterized in that: the ammonia spraying absorption tower (4) comprises an air inlet end (41), a liquid outlet end (42), a plurality of packing layers and a plurality of spraying pieces (45) which are arranged corresponding to the packing layers, wherein the packing layers and the spraying pieces (45) are located between the air inlet end (41) and the liquid outlet end (42), and the spraying pieces (45) are connected with one end, far away from the iron phosphate synthesis reactor (2), of the filtering device (3).
3. The material circulation system for iron phosphate synthesis according to claim 2, characterized in that: the spraying pieces (45) and the packing layers are alternately arranged.
4. The material circulation system for iron phosphate synthesis according to claim 2, characterized in that: be equipped with gas outlet (11) and liquid outlet (12) on ferrous sulfate edulcoration reactor (1), gas outlet (11) are connected with ammonia spray absorption tower (4) through conversion subassembly (13), be connected with ferrous sulfate liquid storage pot (6) between liquid outlet (12) and ferric phosphate synthesis reactor (2).
5. The material circulation system for iron phosphate synthesis according to claim 4, characterized in that: conversion subassembly (13) are including tee bend (131) and first air pump (132), one logical and ammonia gas spraying absorption tower (4) of keeping away from the outlet duct of tee bend (131) are connected, another logical and first air pump (132) of keeping away from the outlet duct of tee bend (131) are connected, the one end that tee bend (131) were kept away from in first air pump (132) is connected with inlet end (41).
6. The material circulation system for iron phosphate synthesis according to claim 2, characterized in that: the device is characterized in that the ferrous sulfate impurity removal reactor (1) is connected with an ammonia liquid recovery tank (7), and one end, far away from the ferrous sulfate impurity removal reactor (1), of the ammonia liquid recovery tank (7) is connected with a liquid outlet end (42).
7. The material circulation system for iron phosphate synthesis according to claim 2, characterized in that: be connected with acid waste liquid storage tank (8) between filter equipment (3) and ammonia spray absorption tower (4), acid waste liquid storage tank (8) are used for storing the acid waste liquid after filter equipment (3) filters, acid waste liquid storage tank (8) are connected through first liquid pump (81) with spraying piece (45).
8. The material circulation system for iron phosphate synthesis according to claim 2, characterized in that: be equipped with ammonia gas outlet (21) on iron phosphate synthesis reactor (2), ammonia gas outlet (21) are connected through second air pump (22) with spraying (45).
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| CN202123304402.5U CN218188871U (en) | 2021-12-25 | 2021-12-25 | Material circulating system for iron phosphate synthesis |
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| CN202123304402.5U CN218188871U (en) | 2021-12-25 | 2021-12-25 | Material circulating system for iron phosphate synthesis |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116531924A (en) * | 2023-05-19 | 2023-08-04 | 湖北朗润环保科技有限公司 | Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater |
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2021
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116531924A (en) * | 2023-05-19 | 2023-08-04 | 湖北朗润环保科技有限公司 | Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater |
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