CN114956120A - Granular ammonium sulfate production device and production method thereof - Google Patents
Granular ammonium sulfate production device and production method thereof Download PDFInfo
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- CN114956120A CN114956120A CN202210509451.2A CN202210509451A CN114956120A CN 114956120 A CN114956120 A CN 114956120A CN 202210509451 A CN202210509451 A CN 202210509451A CN 114956120 A CN114956120 A CN 114956120A
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- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
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- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
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Abstract
The invention relates to the technical field of chemical equipment, in particular to a granular ammonium sulfate production device and a production method thereof, wherein the granular ammonium sulfate production device comprises a solid-phase material circulating system, a liquid-phase material system and a gas-phase material system; the solid-phase material circulating system realizes solid-phase material granulation; the liquid-phase material system realizes guniting granulation; the gas-phase material system realizes the treatment of granulation tail gas. The device realizes the batch production of the granular ammonium sulfate, and has the characteristics of short flow, simple operation and strong applicability compared with the traditional granular ammonium sulfate production process; the production efficiency is high, the product quality is stable, and the produced product not only keeps the original characteristic of good water solubility, but also has the advantages of uniform granularity, high strength, difficult caking, convenient spreading and application, and sustained fertilizer effect. In addition, the method has the characteristics of high recovery rate of tail gas dust and avoiding equipment corrosion; the granulator gas phase channel is provided with an air quantity regulating flashboard, and the air quantity in the granulator can be adjusted according to the production load.
Description
Technical Field
The invention relates to the technical field of chemical equipment and granular ammonium sulfate production, in particular to a granular ammonium sulfate production device and a production method thereof.
Background
At present, the domestic method for producing ammonium sulfate mainly comprises a synthesis method, a recovery method, a gypsum method and a secondary recovery method, but the product is mainly amorphous or powdery; the production method of the granular ammonium sulfate mainly uses powdery materials as master batches to be extruded into granules or crystallized into granules, and finished product granules are irregular or too small; few enterprises depend on the phosphogypsum to prepare granular ammonium sulfate, the grain diameter of the product is 1-2mm, and the color difference of the product is large. The granular ammonium sulfate produced by extrusion granulation or crystallization granulation has irregular and non-round granules; the particles produced by crystallization are generally smaller; the control in the production processes of the two is more complicated.
Disclosure of Invention
Based on the technical problems, the invention provides a production device and a production method of granular ammonium sulfate.
In order to achieve the purpose, the invention provides the following technical scheme:
the invention protects a granular ammonium sulfate production device, which comprises a solid-phase material circulating system, a liquid-phase material system and a gas-phase material system; the solid-phase material circulating system realizes solid-phase material granulation; the liquid-phase material system realizes guniting granulation; the gas-phase material system realizes the treatment of granulation tail gas;
the solid phase material circulating system comprises: the device comprises a granulator 1, a dryer 2, a natural gas combustion furnace 3, an air blower 4, a belt conveyor A5, a lifting machine A6, a vibrating mesh screen A7, a vibrating mesh screen B8, a crusher A9, a crusher B10, a belt conveyor B11, a belt conveyor C12, a lifting machine B13, a belt conveyor D14, a fluidized bed cooler 15, a fluidized bed air blower A16, a fluidized bed air blower B17, a fluidized bed induced draft fan A18, a fluidized bed induced draft fan B19, a lifting machine C20, a plane rotary screen 21, a lifting machine D22, a belt conveyor E23, a wrapping cylinder 24 and a belt conveyor F25;
the outlet end of the granulator 1 is connected with the inlet end of a dryer 2, and the lower end of the dryer 2 is provided with a natural gas combustion furnace 3 and a blower 4; the outlet end of the dryer 2 is connected with a belt conveyor A5; the output end of the belt conveyor A5 is connected with the inlet end of a hoisting machine A6; the outlet end of the hoister A6 is respectively connected with a vibrating mesh screen A7 and a vibrating mesh screen B8 in parallel; the rear ends of the vibrating mesh screen A7 and the vibrating mesh screen B8 are respectively connected with a crusher A9 and a crusher B10; qualified material outlets of the vibrating mesh screen A7 and the vibrating mesh screen B8 are connected with an input end of a belt conveyor B11, and an output end of the belt conveyor B11 is connected with an input end of a belt conveyor D14; the output end of the belt conveyor D14 is connected with the fluidized bed cooler 15; a fluidized bed induced draft fan A18 and a fluidized bed induced draft fan B19 are arranged at the upper end of the fluidized bed cooler 15 in parallel; the lower end of the fluidized bed cooler 15 is provided with a fluidized bed blower A16 and a fluidized bed blower B17 in parallel; the outlet end of the fluidized bed cooler 15 is connected with the inlet end of an elevator C20; the outlet end of the hoister C20 is aligned with the plane rotary screen 21; the discharge end of the plane rotary screen 21 is connected with the inlet end of a lifter D22, and the outlet end of the lifter D22 is connected with the input end of a belt conveyor E23; the output end of the belt conveyor E23 is connected with the wrapping drum 24; the output end of the wrapping drum 24 is connected with a belt conveyor F25 and enters a bulk finished product area; the belt conveyor C12 is arranged below the components and used for collecting unqualified materials, the output end of the belt conveyor C12 is connected with the inlet end of a hoisting machine B13, and the inlet end of the hoisting machine B13 is aligned with the inlet end of the granulator 1 to complete circulation;
the liquid phase material system comprises: a tubular reactor 26, an ammonia spray shaft 27, a branch sulfuric acid spray pipe 28, a liquid ammonia pump 29, a tubular reactor feed pump 30, a tubular reactor feed tank 31, a sulfuric acid diluter 32, a cooling tower 33, a circulating water pump 34, a dilute sulfuric acid delivery pump 35, a concentrated sulfuric acid delivery pump 36, a dilute sulfuric acid storage tank 37, a concentrated sulfuric acid storage tank 38, an MAP dissolution tank 39, an MAP metering belt 40, a primary scrubber 41, a primary scrubber circulating pump 42, a pipeline scrubber circulating pump 43, a secondary scrubber 44, a secondary scrubber circulating pump A45, a secondary scrubber circulating pump B46, a scrubber 47, a scrubber circulating pump A48 and a scrubber circulating pump B49;
the washing tower 47 is sequentially connected with the secondary washer 44 and the primary washer 41 in a circulating manner, and the lower end of the washing tower 47 is connected with a washing tower circulating pump A48 and a washing tower circulating pump B49 in parallel; the lower end of the secondary scrubber 44 is connected with a secondary scrubber circulating pump A45 and a secondary scrubber circulating pump B46 in parallel; the lower end of the first-stage washer 41 is connected with a first-stage washer circulating pump 42 and a pipeline washer circulating pump 43 in parallel; the pipelines in front of the first-stage scrubber 41 and the first-stage scrubber circulating pump 42 are respectively connected with an MAP dissolving tank 39 and a tubular reactor feeding tank 31; a MAP measuring belt 40 is arranged above the MAP dissolving tank 39; the output port of the MAP dissolution tank 39 is connected with the sulfuric acid diluter 32; the output end of the tubular reactor feeding trough 31 is sequentially connected with a tubular reactor feeding pump 30 and a tubular reactor 26; the outlet end of the concentrated sulfuric acid storage tank 38 is sequentially connected with a concentrated sulfuric acid delivery pump 36 and a sulfuric acid diluter 32; the outlet of the sulfuric acid diluter 32 is sequentially connected with a water cooling tower 33 and a circulating water pump 34, and the outlet of the circulating water pump 34 is connected with the sulfuric acid diluter 32; the output port of the sulfuric acid diluter 32 is sequentially connected with a dilute sulfuric acid storage tank 37, a dilute sulfuric acid delivery pump 35 and the tubular reactor 26; the liquid ammonia pump 29 is connected with the tubular reactor 26; an ammonia spraying shaft 27 is arranged above the tubular reactor 26; a branch sulfuric acid spray pipe 28 is arranged below the tubular reactor 26, and the other end of the branch sulfuric acid spray pipe 28 is connected with a concentrated sulfuric acid delivery pump 36; a granulator material bed 56 is arranged below the ammonia spray shaft 27, the branch pipe sulfuric acid spray pipes 28 and the tubular reactor 26;
the gas phase feed system comprises: a granulation tail gas induced draft fan 50, a drying tail gas induced draft fan 51, a centrifugal dust collector A52, a centrifugal dust collector B53, a bag-type dust collector 54 and a gas-phase ash conveying system 55; the inlet of the granulation tail gas induced draft fan 50 is connected with the first-stage scrubber 41 and the second-stage scrubber 44 in series, and the outlet is connected with the washing tower 47; the output end of the dry tail gas induced draft fan 51 is connected with the washing tower 47, the input end of the dry tail gas induced draft fan is sequentially connected with the bag-type dust collector 54 and the centrifugal dust collector A52, and the input end of the centrifugal dust collector A52 is connected with the tail gas end of the dryer 2; the output end of the centrifugal dust collector B53 is connected with the secondary scrubber 44, and the input end is connected with the tail gas end of the dryer 2; the washing tower 47 is connected with the tail gas end of the fluidized bed cooler 15; the gas-solid separation end of the tail gas end of the dryer 2 is connected with a gas-phase ash conveying system 55, and the gas-phase ash conveying system 55 is connected with the input end of a belt conveyor C12 of the solid-phase circulating system;
further, the washing tower 47 is also provided with a tail gas outlet, and the tail gas from the fluidized bed cooler 15, the tail gas from the granulation tail gas induced draft fan 50 and the tail gas from the drying tail gas induced draft fan 51 are jointly treated and then evacuated.
Further, the tubular reactor 26 is divided into a mixing section, an adjusting section and a nozzle section, wherein the mixing section and the adjusting section use a polytetrafluoroethylene lining steel pipe, the thickness of the polytetrafluoroethylene lining is more than or equal to 10mm, the length of a pipe fitting is less than or equal to 700mm, and the nozzle section uses a 904L stainless steel pipe; the tubular reactor 26 is a double nozzle with a spraying angle of 25-45 deg.
Furthermore, the branch pipe sulfuric acid spraying pipes 28 are distributed in a cross mode with the ammonia spraying shaft 27, the ammonia spraying shaft 27 is provided with a 1# ammonia branch pipe, a 2# ammonia branch pipe, a 3# ammonia branch pipe and a 4# ammonia branch pipe, and the branch pipe sulfuric acid spraying pipes 28 are arranged in the middle of the 1# ammonia branch pipe and the 2# ammonia branch pipe and used for adjusting the heat of the system in production.
Furthermore, the gas phase channel of the granulator 1 is provided with an air volume adjusting flashboard, and the air volume in the granulator can be adjusted according to the production load.
The invention also protects the production method of the granular ammonium sulfate production device; the method specifically comprises the following steps:
Further, the MAP solution obtained in step 1 is prepared into a MAP solution having a concentration of 5% without phosphoric acid, and P is supplied into the tubular reactor 26 2 O 5 And respectively adding a certain amount of concentrated sulfuric acid into the first-stage scrubber 41, the second-stage scrubber 44 and the washing tower 47, treating the tail gas in stages to meet the tail gas emission index, controlling the pH value of washing water to be less than or equal to 5 in the process, improving the recovery rate of tail gas ammonia, and avoiding equipment corrosion.
Compared with the prior art, the invention has the following beneficial effects:
the device realizes the batch production of the granular ammonium sulfate, and has the characteristics of short flow, simple operation and strong applicability compared with the traditional granular ammonium sulfate production process; the production efficiency is high, the product quality is stable, and the produced product not only keeps the original characteristic of good water solubility, but also has the advantages of uniform granularity, high strength, difficult caking, convenient spreading and application, and sustained fertilizer effect. In addition, the method has the characteristics of high recovery rate of tail gas dust and avoiding equipment corrosion; the granulator gas phase channel is provided with an air quantity regulating flashboard, and the air quantity in the granulator can be regulated according to the production load.
Drawings
FIG. 1 is a schematic diagram of the overall structure of a solid phase material circulation system of the device of the present invention;
FIG. 2 is a schematic structural diagram of a liquid-phase material system and a gas-phase material system according to the present invention.
In the figure: 1. a granulator; 2. a dryer; 3. a natural gas combustion furnace; 4. a blower; 5. A belt conveyor A; 6. a hoist A; 7. vibrating the mesh screen A; 8. vibrating the mesh screen B; 9. a crusher A; 10. a crusher B; 11. a belt conveyor B; 12. a belt conveyor C; 13. A hoist B; 14. a belt conveyor D; 15. a fluidized bed cooler; 16. a fluidized bed blower A; 17. a fluidized bed blower B; 18. a fluidized bed induced draft fan A; 19. a fluidized bed induced draft fan B; 20. a hoist C; 21. a plane rotary screen; 22. a hoist D; 23. a belt conveyor E; 24. a wrapping drum; 25. a belt conveyor F; 26. a tubular reactor; 27. an ammonia spray shaft; 28. branch sulfuric acid spray pipes; 29. a liquid ammonia pump; 30. a tubular reactor feed pump; 31. A tubular reactor feed trough; 32. a sulfuric acid diluter; 33. a water cooling tower; 34. a water circulating pump; 35. a dilute sulfuric acid delivery pump; 36. a concentrated sulfuric acid delivery pump; 37. a dilute sulfuric acid storage tank; 38. a concentrated sulfuric acid storage tank; 39. an MAP dissolution tank; 40. a MAP metering belt; 41. a first-stage scrubber; 42. a first-stage scrubber circulating pump; 43. a pipeline scrubber circulation pump; 44. a secondary scrubber; 45. a secondary scrubber circulating pump A; 46. a second scrubber circulating pump B; 47. a washing tower; 48. a washing tower circulating pump A; 49. a washing tower circulating pump B; 50. a granulation tail gas draught fan; 51. a dry tail gas draught fan; 52. a centrifugal dust remover A; 53. a centrifugal dust collector B; 54. A bag-type dust collector; 55. a gas-phase ash conveying system; 56. a granulator material bed.
Detailed Description
The technical solutions of the present invention will be described below clearly and completely in conjunction with the embodiments, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Referring to the attached drawings 1-2, the granular ammonium sulfate production device comprises a solid phase material circulating system, a liquid phase material system and a gas phase material system; the solid-phase material circulating system realizes granulation of the solid-phase material; the liquid-phase material system realizes guniting granulation; the gas-phase material system realizes the treatment of granulation tail gas;
the solid phase material circulation system includes: the device comprises a granulator 1, a dryer 2, a natural gas combustion furnace 3, an air blower 4, a belt conveyor A5, a lifting machine A6, a vibrating mesh screen A7, a vibrating mesh screen B8, a crusher A9, a crusher B10, a belt conveyor B11, a belt conveyor C12, a lifting machine B13, a belt conveyor D14, a fluidized bed cooler 15, a fluidized bed air blower A16, a fluidized bed air blower B17, a fluidized bed induced draft fan A18, a fluidized bed induced draft fan B19, a lifting machine C20, a plane rotary screen 21, a lifting machine D22, a belt conveyor E23, a wrapping cylinder 24 and a belt conveyor F25; the outlet end of the granulator 1 is connected with the inlet end of a dryer 2, and the lower end of the dryer 2 is provided with a natural gas combustion furnace 3 and a blower 4; the outlet end of the dryer 2 is connected with a belt conveyor A5; the output end of the belt conveyor A5 is connected with the inlet end of a hoist A6; the outlet end of the hoister A6 is respectively connected with a vibrating mesh screen A7 and a vibrating mesh screen B8 in parallel; the rear ends of the vibrating mesh screen A7 and the vibrating mesh screen B8 are respectively connected with a crusher A9 and a crusher B10; qualified material outlets of the vibrating mesh screen A7 and the vibrating mesh screen B8 are connected with an input end of a belt conveyor B11, and an output end of the belt conveyor B11 is connected with an input end of a belt conveyor D14; the output end of the belt conveyor D14 is connected with the fluidized bed cooler 15; a fluidized bed induced draft fan A18 and a fluidized bed induced draft fan B19 are arranged at the upper end of the fluidized bed cooler 15 in parallel; the lower end of the fluidized bed cooler 15 is provided with a fluidized bed blower A16 and a fluidized bed blower B17 in parallel; the outlet end of the fluidized bed cooler 15 is connected with the inlet end of the lifter C20; the outlet end of the hoister C20 is aligned with the plane rotary screen 21; the discharge end of the plane rotary screen 21 is connected with the inlet end of a lifter D22, and the outlet end of the lifter D22 is connected with the input end of a belt conveyor E23; the output end of the belt conveyor E23 is connected with the wrapping drum 24; the output end of the wrapping drum 24 is connected with a belt conveyor F25 and enters a bulk finished product area; the belt conveyor C12 is arranged below the components and used for collecting unqualified materials, the output end of the belt conveyor C12 is connected with the inlet end of a hoisting machine B13, and the inlet end of the hoisting machine B13 is aligned with the inlet end of the granulator 1 to complete circulation;
the liquid phase material system comprises: a tubular reactor 26, an ammonia spray shaft 27, a branch sulfuric acid spray pipe 28, a liquid ammonia pump 29, a tubular reactor feed pump 30, a tubular reactor feed tank 31, a sulfuric acid diluter 32, a cooling tower 33, a circulating water pump 34, a dilute sulfuric acid delivery pump 35, a concentrated sulfuric acid delivery pump 36, a dilute sulfuric acid storage tank 37, a concentrated sulfuric acid storage tank 38, an MAP dissolution tank 39, an MAP metering belt 40, a primary scrubber 41, a primary scrubber circulating pump 42, a pipeline scrubber circulating pump 43, a secondary scrubber 44, a secondary scrubber circulating pump A45, a secondary scrubber circulating pump B46, a scrubber 47, a scrubber circulating pump A48 and a scrubber circulating pump B49; the washing tower 47 is sequentially connected with the second-stage washer 44 and the first-stage washer 41 in a circulating manner, and the lower end of the washing tower 47 is connected with a washing tower circulating pump A48 and a washing tower circulating pump B49 in parallel; the lower end of the secondary scrubber 44 is connected with a secondary scrubber circulating pump A45 and a secondary scrubber circulating pump B46 in parallel; the lower end of the first-stage washer 41 is connected with a first-stage washer circulating pump 42 and a pipeline washer circulating pump 43 in parallel; the pipelines in front of the first-stage scrubber 41 and the first-stage scrubber circulating pump 42 are respectively connected with an MAP dissolution tank 39 and a tubular reactor feeding tank 31; an MAP measuring belt 40 is arranged above the MAP dissolving tank 39; the output port of the MAP dissolution tank 39 is connected with the sulfuric acid diluter 32; the output end of the tubular reactor feeding trough 31 is sequentially connected with a tubular reactor feeding pump 30 and a tubular reactor 26; the outlet end of the concentrated sulfuric acid storage tank 38 is sequentially connected with a concentrated sulfuric acid delivery pump 36 and a sulfuric acid diluter 32; the output port of the sulfuric acid diluter 32 is sequentially connected with a water cooling tower 33 and a circulating water pump 34, and the outlet of the circulating water pump 34 is connected with the sulfuric acid diluter 32; the output port of the sulfuric acid diluter 32 is sequentially connected with a dilute sulfuric acid storage tank 37, a dilute sulfuric acid delivery pump 35 and the tubular reactor 26; a liquid ammonia pump 29 is connected with the tubular reactor 26; an ammonia spraying shaft 27 is arranged above the tubular reactor 26; a branch sulfuric acid spray pipe 28 is arranged below the tubular reactor 26, and the other end of the branch sulfuric acid spray pipe 28 is connected with a concentrated sulfuric acid delivery pump 36; a granulator material bed 56 is arranged below the ammonia spray shaft 27, the branch pipe sulfuric acid spray pipes 28 and the tubular reactor 26;
the gas phase material system comprises: a granulation tail gas induced draft fan 50, a drying tail gas induced draft fan 51, a centrifugal dust collector A52, a centrifugal dust collector B53, a bag-type dust collector 54 and a gas-phase ash conveying system 55; the inlet of a granulation tail gas draught fan 50 is connected with the first-stage scrubber 41 and the second-stage scrubber 44 in series, and the outlet is connected with the washing tower 47; the output end of the dry tail gas induced draft fan 51 is connected with the washing tower 47, the input end of the dry tail gas induced draft fan is sequentially connected with the bag-type dust collector 54 and the centrifugal dust collector A52, and the input end of the centrifugal dust collector A52 is connected with the tail gas end of the dryer 2; the output end of the centrifugal dust collector B53 is connected with the secondary scrubber 44, and the input end is connected with the tail gas end of the dryer 2; the washing tower 47 is connected with the tail gas end of the fluidized bed cooler 15; the gas-solid separation end of the tail gas end of the dryer 2 is connected with the gas-phase ash conveying system 55, and the gas-phase ash conveying system 55 is connected with the input end of a belt conveyor C12 of the solid-phase circulating system.
Preferably, the washing tower 47 is further provided with a tail gas outlet for discharging the tail gas from the fluidized bed cooler 15, the tail gas from the granulation tail gas induced draft fan 50 and the tail gas from the drying tail gas induced draft fan 51 after being jointly treated.
Optimally, the tubular reactor 26 is divided into a mixing section, an adjusting section and a nozzle section, the mixing section and the adjusting section use polytetrafluoroethylene lining steel pipes, the thickness of the polytetrafluoroethylene lining is more than or equal to 10mm, the length of a pipe fitting is less than or equal to 700mm, and the nozzle section uses 904L stainless steel pipes; the tubular reactor 26 is a double nozzle with a spraying angle of 25-45 deg.
Optimally, the branch sulfuric acid spray pipes 28 and the ammonia spray shaft 27 are distributed in a crossed mode, the ammonia spray shaft 27 is provided with a 1# ammonia branch pipe, a 2# ammonia branch pipe, a 3# ammonia branch pipe and a 4# ammonia branch pipe, and the branch sulfuric acid spray pipes 28 are arranged in the middle of the 1# ammonia branch pipe and the 2# ammonia branch pipe and used for adjusting the heat of the system in production.
Optimally, the gas phase channel of the granulator 1 is provided with an air volume adjusting flashboard, and the air volume in the granulator can be adjusted according to the production load.
Example 2
A production method of a granular ammonium sulfate production device; the method specifically comprises the following steps:
Optimally, the MAP solution in step 1 is prepared into a MAP solution with the concentration of 5 percent in the case of no phosphoric acid, and then the MAP solution is fed into the tubular reactor 26Supplement P 2 O 5 And respectively adding a certain amount of concentrated sulfuric acid into the first-stage scrubber 41, the second-stage scrubber 44 and the washing tower 47, treating the tail gas in stages to meet the tail gas emission index, controlling the pH value of washing water to be less than or equal to 5 in the process, improving the recovery rate of tail gas ammonia, and avoiding equipment corrosion.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The utility model provides a granule thiamine apparatus for producing which characterized in that: comprises a solid phase material circulating system, a liquid phase material system and a gas phase material system; the solid-phase material circulating system realizes solid-phase material granulation; the liquid-phase material system realizes guniting granulation; the gas-phase material system realizes the treatment of granulation tail gas;
the solid phase material circulating system comprises: the device comprises a granulator (1), a dryer (2), a natural gas combustion furnace (3), an air blower (4), a belt conveyor A (5), a lifter A (6), a vibrating mesh screen A (7), a vibrating mesh screen B (8), a crusher A (9), a crusher B (10), a belt conveyor B (11), a belt conveyor C (12), a lifter B (13), a belt conveyor D (14), a fluidized bed cooler (15), a fluidized bed air blower A (16), a fluidized bed air blower B (17), a fluidized bed induced draft fan A (18), a fluidized bed induced draft fan B (19), a lifter C (20), a plane rotary screen (21), a lifter D (22), a belt conveyor E (23), a wrapping cylinder (24) and a belt conveyor F (25);
the outlet end of the granulator (1) is connected with the inlet end of the dryer (2), and the lower end of the dryer (2) is provided with a natural gas combustion furnace (3) and a blower (4); the outlet end of the dryer (2) is connected with a belt conveyor A (5); the output end of the belt conveyor A (5) is connected with the inlet end of a lifter A (6); the outlet end of the hoister A (6) is respectively connected with a vibrating mesh screen A (7) and a vibrating mesh screen B (8) in parallel; the rear ends of the vibrating mesh screen A (7) and the vibrating mesh screen B (8) are respectively connected with a crusher A (9) and a crusher B (10); qualified material outlets of the vibrating mesh screen A (7) and the vibrating mesh screen B (8) are connected with an input end of a belt conveyor B (11), and an output end of the belt conveyor B (11) is connected with an input end of a belt conveyor D (14); the output end of the belt conveyor D (14) is connected with a fluidized bed cooler (15); a fluidized bed induced draft fan A (18) and a fluidized bed induced draft fan B (19) are arranged at the upper end of the fluidized bed cooler (15) in parallel; the lower end of the fluidized bed cooler (15) is provided with a fluidized bed blower A (16) and a fluidized bed blower B (17) in parallel; the outlet end of the fluidized bed cooler (15) is connected with the inlet end of a lifter C (20); the outlet end of the hoister C (20) is aligned with the plane rotary screen (21); the discharge end of the plane rotary screen (21) is connected with the inlet end of a lifter D (22), and the outlet end of the lifter D (22) is connected with the input end of a belt conveyor E (23); the output end of the belt conveyor E (23) is connected with a wrapping drum (24); the output end of the wrapping cylinder (24) is connected with a belt conveyor F (25) and enters a bulk finished product area; the belt conveyor C (12) is arranged below the components and used for collecting unqualified materials, the output end of the belt conveyor C (12) is connected with the inlet end of a hoister B (13), and the inlet end of the hoister B (13) is aligned with the inlet end of the granulator (1) to complete circulation;
the liquid phase material system comprises: the device comprises a tubular reactor (26), an ammonia spray shaft (27), a branch sulfuric acid spray pipe (28), a liquid ammonia pump (29), a tubular reactor feed pump (30), a tubular reactor feed tank (31), a sulfuric acid diluter (32), a water cooling tower (33), a circulating water pump (34), a dilute sulfuric acid delivery pump (35), a concentrated sulfuric acid delivery pump (36), a dilute sulfuric acid storage tank (37), a concentrated sulfuric acid storage tank (38), an MAP dissolving tank (39), an MAP metering belt (40), a primary scrubber (41), a primary scrubber circulating pump (42), a pipeline scrubber circulating pump (43), a secondary scrubber (44), a secondary scrubber circulating pump A (45), a secondary scrubber circulating pump B (46), a scrubber (47), a scrubber circulating pump A (48) and a scrubber circulating pump B (49);
the washing tower (47) is sequentially connected with a secondary washer (44) and a primary washer (41) in a circulating manner, and the lower end of the washing tower (47) is connected with a washing tower circulating pump A (48) and a washing tower circulating pump B (49) in parallel; the lower end of the secondary scrubber (44) is connected with a secondary scrubber circulating pump A (45) and a secondary scrubber circulating pump B (46) in parallel; the lower end of the first-stage washer (41) is connected with a first-stage washer circulating pump (42) and a pipeline washer circulating pump (43) in parallel; a MAP dissolving tank (39) and a tubular reactor feeding tank (31) are respectively connected to pipelines in front of the primary scrubber (41) and the primary scrubber circulating pump (42); a MAP measuring belt (40) is arranged above the MAP dissolving tank (39); the output port of the MAP dissolution tank (39) is connected with a sulfuric acid diluter (32); the output end of the tubular reactor feeding groove (31) is sequentially connected with a tubular reactor feeding pump (30) and a tubular reactor (26); the outlet end of the concentrated sulfuric acid storage tank (38) is sequentially connected with a concentrated sulfuric acid delivery pump (36) and a sulfuric acid diluter (32); the output port of the sulfuric acid diluter (32) is sequentially connected with a water cooling tower (33) and a circulating water pump (34), and the outlet of the circulating water pump (34) is connected with the sulfuric acid diluter (32); the output port of the sulfuric acid diluter (32) is sequentially connected with a dilute sulfuric acid storage tank (37), a dilute sulfuric acid delivery pump (35) and a tubular reactor (26); the liquid ammonia pump (29) is connected with the tubular reactor (26); an ammonia spraying shaft (27) is arranged above the tubular reactor (26); a branch sulfuric acid spray pipe (28) is arranged below the tubular reactor (26), and the other end of the branch sulfuric acid spray pipe (28) is connected with a concentrated sulfuric acid delivery pump (36); a granulator material bed (56) is arranged below the ammonia spray shaft (27), the branch pipe sulfuric acid spray pipe (28) and the tubular reactor (26);
the gas phase feed system comprises: a granulation tail gas induced draft fan (50), a drying tail gas induced draft fan (51), a centrifugal dust collector A (52), a centrifugal dust collector B (53), a bag-type dust collector (54) and a gas-phase ash conveying system (55); the inlet of the granulation tail gas induced draft fan (50) is connected with the first-stage scrubber (41) and the second-stage scrubber (44) in series, and the outlet is connected with the washing tower (47); the output end of the dry tail gas induced draft fan (51) is connected with the washing tower (47), the input end of the dry tail gas induced draft fan is sequentially connected with the bag-type dust collector (54) and the centrifugal dust collector A (52), and the input end of the centrifugal dust collector A (52) is connected with the tail gas end of the dryer (2); the output end of the centrifugal dust collector B (53) is connected with the secondary scrubber (44), and the input end of the centrifugal dust collector B is connected with the tail gas end of the dryer (2); the washing tower (47) is connected with the tail gas end of the fluidized bed cooler (15); the gas-solid separation end of the tail gas end of the dryer (2) is connected with a gas-phase ash conveying system (55), and the gas-phase ash conveying system (55) is connected with the input end of a belt conveyor C (12) of the solid-phase circulating system.
2. The apparatus for producing granular ammonium sulfate according to claim 1, wherein: and a tail gas outlet is also formed in the washing tower (47).
3. The apparatus for producing granular ammonium sulfate according to claim 1, wherein: the tubular reactor (26) is divided into a mixing section, an adjusting section and a nozzle section, the mixing section and the adjusting section use a polytetrafluoroethylene lining steel pipe, the thickness of the polytetrafluoroethylene lining is more than or equal to 10mm, the length of a pipe fitting is less than or equal to 700mm, and the nozzle section uses a 904L stainless steel pipe; the tubular reactor (26) is provided with double nozzles, and the spraying angle is 25-45 degrees.
4. The apparatus for producing granular ammonium sulfate according to claim 1, wherein: the branch pipe sulfuric acid spray pipes (28) and the ammonia spray shafts (27) are distributed in a crossed mode, the ammonia spray shafts (27) are provided with a 1# ammonia branch pipe, a 2# ammonia branch pipe, a 3# ammonia branch pipe and a 4# ammonia branch pipe, and the branch pipe sulfuric acid spray pipes (28) are arranged in the middle of the 1# ammonia branch pipe and the 2# ammonia branch pipe.
5. The apparatus for producing granular ammonium sulfate according to claim 1, wherein: and a gas phase channel of the granulator (1) is provided with an air quantity adjusting flashboard.
6. The production method of a granular ammonium sulfate production apparatus according to any one of claims 1 to 5, characterized in that: the method specifically comprises the following steps:
step 1, dilute sulfuric acid preparation process: sending concentrated sulfuric acid into a concentrated sulfuric acid storage tank (38), sending a part of concentrated sulfuric acid into a sulfuric acid diluter (32) through a concentrated sulfuric acid pump (36), mixing and diluting with a solution from a MAP dissolution tank (39), and preparing the concentrated sulfuric acid with the concentration of 55-75% and the density of 1.50-1.70g/cm 3 The temperature of the dilute sulfuric acid is controlled to be lower than 65 ℃ in the preparation process, and phosphoric acid or MAP solution is added to ensure that P in the dilute sulfuric acid is 2 O 5 The concentration is controlled within 1.5 percent, the granulation effect is ensured, and the product economy is improved;
step 2, the process of amino acid neutralization reaction: the prepared dilute sulfuric acid is sent into a tubular reactor (26) through a dilute sulfuric acid delivery pump (35) and is subjected to neutralization reaction with ammonia from a liquid ammonia pump (29), and the mass ratio of the dilute acid to the ammonia is controlled to be 2.88:1 so as to meet the condition that the pH value of a material at a granulation outlet is less than or equal to 6;
step 3, a spraying granulation process: in the slurry spraying process, the pressure of the tubular reactor (26) is controlled to be 0.25-0.55MPa, the temperature is 100-; the tubular reactor (26) is provided with double nozzles, the spraying angle is 25-45 degrees, in order to meet the granulation mechanism, the temperature is controlled at 70-80 ℃, the condition of low-temperature granulation is prevented, the particle strength is reduced, the operation requirement of a dust removal system is met, partial concentrated sulfuric acid is sprayed on the surface of a granulator material bed (56), the temperature of the granulator material bed (56) is improved, the total amount of branch sulfuric acid spray pipes (28) is controlled to be less than or equal to 2.0m 3 /h；
Step 4, the operation process of the natural gas combustion furnace is as follows: the load of the natural gas combustion furnace (3) meets the system operation requirement, and the consumption of single ton of product natural gas is controlled to be 10-20Nm 3 Controlling the temperature of the drying tail gas at 70-75 ℃; meanwhile, the operation requirement of a bag-type dust collector (54) is met, and the temperature of purified gas is ensured to be 60-65 ℃.
7. The production method of the granular ammonium sulfate production device according to claim 6, characterized in that: preparing MAP solution with concentration of 5% from the MAP solution in the step 1 under the condition of no phosphoric acid, and supplementing P into the tubular reactor 26 2 O 5 A certain amount of concentrated sulfuric acid is respectively added into the first-stage scrubber (41), the second-stage scrubber (44) and the scrubbing tower (47), the tail gas is treated in stages, the tail gas emission index is met, the pH value of scrubbing water is controlled to be less than or equal to 5 in the process, the recovery rate of tail gas ammonia is improved, and equipment corrosion is avoided.
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| CN101648713A (en) * | 2009-07-23 | 2010-02-17 | 瓮福（集团）有限责任公司 | Method for producing granular ammonium sulfate |
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| CN103664300A (en) * | 2013-12-20 | 2014-03-26 | 青海云天化国际化肥有限公司 | Method for producing granules and synthesizing ammonium sulfate through drum spray granulation by ammonia acid process |
| US8974763B1 (en) * | 2013-12-18 | 2015-03-10 | Rentech, Inc. | System and method for production of granular ammonium sulfate |
| CN206529300U (en) * | 2017-02-06 | 2017-09-29 | 青海云天化国际化肥有限公司 | Particle ammonium sulfate production apparatus and system |
| CN217126936U (en) * | 2022-05-10 | 2022-08-05 | 青海云天化国际化肥有限公司 | Granular ammonium sulfate production device |
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| CN101850989A (en) * | 2009-04-02 | 2010-10-06 | 河北天人化工股份有限公司 | Preparation method of large-particle ammonium sulfate |
| CN101648713A (en) * | 2009-07-23 | 2010-02-17 | 瓮福（集团）有限责任公司 | Method for producing granular ammonium sulfate |
| US8974763B1 (en) * | 2013-12-18 | 2015-03-10 | Rentech, Inc. | System and method for production of granular ammonium sulfate |
| CN103664300A (en) * | 2013-12-20 | 2014-03-26 | 青海云天化国际化肥有限公司 | Method for producing granules and synthesizing ammonium sulfate through drum spray granulation by ammonia acid process |
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