CN110562944B - High-ammonia-utilization-rate low-ammonia-emission-amount diammonium production system and production method - Google Patents
High-ammonia-utilization-rate low-ammonia-emission-amount diammonium production system and production method Download PDFInfo
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Abstract
The invention discloses a diammonium production system with high ammonia utilization rate and low ammonia emission and a production method thereof, belonging to the technical field of ammonium phosphate. Comprises a slurry tank, a tubular reactor, a granulating device, a drying device and a tail gas treatment device; the tail gas treatment device comprises a Venturi scrubber, a granulation washing tower, a first drying circulation tank, a second drying washing tower, a dust collection washing circulation tank, a fluorine washing tower, a fluorine washing circulation tank and an ammonia absorption circulation tank; the ammonia absorption circulating tank, the venturi scrubber, the granulating and washing tower and the second drying tower form a circulating spray structure, and the circulating spray structure is connected with the slurry tank through a pipeline; one spray head of the pipeline spray structure, which is close to the tail gas outlet of the granulating device, is connected with the first drying circulation tank, the concentrated phosphoric acid supply device and the ammonia absorption circulation tank through pipelines, and the other spray heads are connected with the ammonia absorption circulation tank through pipelines. The driving time can be increased to improve the product yield, meanwhile, the production cost can be reduced, and the environmental protection requirement can be met.
Description
Technical Field
The invention belongs to the technical field of ammonium phosphate, and particularly relates to a diammonium production system with high ammonia utilization rate and low ammonia emission and a production method thereof.
Background
Diammonium phosphate, also known as diammonium phosphate, ammonium hydrogen phosphate, is a white crystal of formula (NH) 4 ) 2 HPO 4 Dissolving in water and heating to 155 ℃ to decompose, but at room temperature there is also a possibility that ammonia gas is gradually released to form monoammonium phosphate. The product specification is as follows: 64% (N18: P) 2 O 5 46）、61%（N17：P 2 O 5 45）、57% （N15：P 2 O 5 42). To increase the storage endurance, some products are added with a coating agent during the production process, so that the appearance of the product is brown or yellow.
General preparation of diammonium phosphateThe preparation method comprises the following steps: the concentrated phosphoric acid and the washing liquid from the tail gas treatment device are mixed in a slurry tank, and then are sent to a tubular reactor to carry out neutralization reaction with ammonia gas, and then are sent to a granulating device to carry out granulation with the ammonia gas after the neutralization reaction. Referring to fig. 1, the tail gas treatment apparatus includes a venturi scrubber, a pre-wash circulation tank, a granulation washing tower, a granulation circulation tank, a first drying washing tower, a first drying circulation tank, a second drying washing tower, a second drying circulation tank, a dust collection washing tower, a dust collection circulation tank, a fluorine washing tower, and a fluorine washing circulation tank; the tail gas outlet of the granulating device, the Venturi scrubber, the granulating and washing tower and the fluorine washing tower are sequentially connected through pipelines to form a granulating tail gas treatment channel, a pipeline spraying structure is arranged on a pipeline between the tail gas outlet of the granulating device and the air inlet of the Venturi scrubber, and the pipeline spraying structure comprises a plurality of spray heads arranged in the pipeline; the tail gas outlet of the drying device, the first drying washing tower, the second drying washing tower (for improving the washing effect) and the fluorine washing tower are sequentially connected through pipelines to form a drying tail gas treatment channel; the dust collection washing tower is used for collecting other tail gases (such as cooling tail gases, dust collection of a conveyor belt, water vapor of a slurry tank and the like) except the granulating tail gases and the drying tail gases, and a tail gas outlet of the dust collection washing tower is connected with the fluorine washing tower through a pipeline to form other tail gas treatment channels. The fluorine washing circulation tank and the fluorine washing tower form a circulation spray structure, the circulation spray structure is connected with the dust collection washing circulation tank through a pipeline to send washing liquid with a certain concentration to the dust collection washing circulation tank, process water is supplemented at the position of the fluorine washing circulation tank, the dust collection washing circulation tank and the dust collection washing tower form a circulation spray structure, the circulation spray structure is connected with the first drying circulation tank through a pipeline to send the washing liquid to the first drying circulation tank, and the density of the first drying circulation tank is 1.12-1.18g/cm 3 The neutralization degree is less than 0.15) and the first drying and washing tower form a circulating spray structure, and the circulating spray structure is connected with the second drying and circulating tank through a pipeline to send washing liquid with a certain concentration to the second drying and circulating tank; a second drying circulation tank (density of 1.15-1.20g/cm 3 The neutralization degree is less than 0.15) and the second drying washing tower form a circulating spray structure, and the circulating spray structure is connected with the pre-washing circulating tank through a pipeline to send washing liquid with a certain concentration to the pre-washing circulating tank. Pre-wash circulation tank (density 1.51-1.52 g/cm) 3 Neutralization degree 0.50-0.55) and the Chinese text through a pipelineThe hill scrubber forms a circulating spray structure, which is connected with a spray liquid inlet of the pipeline spray structure (the washing liquid flows to the venturi scrubber) through a pipeline, and is connected with the granulation circulation tank through a pipeline to send the washing liquid with a certain concentration to the granulation circulation tank. The granulation circulation tank and the granulation washing tower form a circulation spray structure, and the circulation spray structure is connected with the slurry tank through a pipeline to send washing liquid with a certain concentration to the slurry tank.
The Chinese patent with application number 201510589060.6 discloses a preparation method of granular diammonium phosphate, which comprises the following steps:
(1) Carrying out heat exchange on water with the temperature of more than or equal to 55 ℃ and liquid ammonia with the concentration of more than 99.6% from an ammonia storage tank in a heat exchanger to obtain gas ammonia with the temperature of more than or equal to 45 ℃;
(2) Granulating
Feeding gas ammonia into a tubular reactor, carrying out mixed reaction with mixed phosphoric acid for 2-5s to obtain ammonium phosphate slurry, conveying the ammonium phosphate slurry to a slurry distributor, spraying the ammonium phosphate slurry onto a material layer of a granulator through a slurry spraying nozzle for rotary drum granulation, and supplementing the gas ammonia into the material layer of the granulator at the same time, so that the neutralization degree of an outlet material is 1.75-1.88, and the temperature is 90-98 ℃, thereby obtaining an intermediate product and granulation tail gas;
(3) Cooling, crushing and sieving
Cooling the intermediate product to a temperature of less than or equal to 75 ℃ through a cooling facility, crushing and screening to obtain granular diammonium phosphate and tail gas of each process, cooling the granular diammonium phosphate to a packaging temperature through a cooling fluidized bed, and then packaging the finished product;
(4) Tail gas treatment
(1) And (3) granulating tail gas treatment: NH-containing scrubbing of granulation gas to gas with fresh concentrated phosphoric acid cycle 3 The concentration is less than 20mg/m 3 Obtaining a washing acid;
(2) and (3) cooling tail gas treatment: dedusting the cooled tail gas by a cyclone dust collector and circularly washing the cooled tail gas by water until the dust concentration of the gas is less than 30mg/m 3 Obtaining fine powder and water washing liquid;
(3) crushing and screening tail gas treatment: dedusting the crushed and screened tail gas by a dry cloth bag deduster until the dust concentration of the gas is less than 30mg/m 3 Obtaining fine powder.
The applicant has found the following problems when using the prior art for the production of diammonium:
1. the ammonia content in the tail gas discharged by the granulating device is large, the washing liquid sprayed by the spray head close to the tail gas outlet reacts with ammonia gas, the spray liquid is quickly solidified to form crystals under the condition of high neutralization degree (more than 0.7), pipelines between the spray head and the granulating device and the venturi scrubber are easy to be blocked, and the pipelines are required to be cleaned for at least 4 times in one quarter.
2. The final tail gas treated by the fluorine washing tower has lighter ammonia smell (even if the spraying amount of each spraying tower is increased or the spraying amount of each spraying tower has lighter ammonia smell and cannot be improved), so that the diammonium production plant area has more obvious ammonia smell, is frequently complained by other plant areas and does not meet the tail gas emission standard.
Disclosure of Invention
The embodiment of the invention provides a diammonium production system with high ammonia utilization rate and low ammonia emission and a production method thereof, wherein after the process is improved, ammonia smell is avoided in tail gas, the tail gas emission standard is met, the ammonia utilization rate is improved by about 1%, and a pipeline and a spray nozzle are not blocked. The technical scheme is as follows:
in one aspect, embodiments of the present invention provide a high ammonia utilization and low ammonia emission diammonium production system, the system comprising a slurry tank 1, a tubular reactor, a granulation device 2, a drying device, and a tail gas treatment device; the tail gas treatment device comprises a cyclone separator, a Venturi scrubber 4, a granulation washing tower 5, a first drying washing tower 6, a first drying circulation tank 11, a second drying washing tower 7, a dust collection washing tower 9, a dust collection washing circulation tank 15, a fluorine washing tower 8, a fluorine washing circulation tank 13 and an ammonia absorption circulation tank 10; the tail gas outlet of the granulating device 2, the Venturi scrubber 4, the granulating and washing tower 5 and the fluorine washing tower 8 are sequentially connected through pipelines to form a granulating tail gas treatment channel, a pipeline spray structure 3 is arranged on a pipeline between the tail gas outlet of the granulating device 2 and the air inlet of the Venturi scrubber 4, and the pipeline spray structure 3 comprises a plurality of spray heads 24 arranged in the pipeline; the tail gas outlet of the drying device, the cyclone separator, the first drying washing tower 6, the second drying washing tower 7 and the fluorine washing tower 8 are sequentially connected through pipelines to form a drying tail gas treatment channel; the dust collection washing tower 9 is used for collecting other tail gases except granulation tail gases and drying tail gases, and a tail gas outlet of the dust collection washing tower is connected with the fluorine washing tower 8 through a pipeline; the fluorine washing circulation tank 13 and the fluorine washing tower 8 form a circulating spray structure and are connected with the dust collection washing circulation tank 15 through a pipeline, process water is supplemented at the position of the fluorine washing circulation tank 13, the dust collection washing circulation tank 15 and the dust collection washing tower 9 form a circulating spray structure and are connected with the first drying circulation tank 11 through a pipeline; the ammonia absorption circulation tank 10 forms a circulation spray structure with the Venturi scrubber 4, the granulation washing tower 5 and the second drying washing tower 7 respectively, and is connected with the slurry tank 1 through a pipeline; one spray head 24 of the pipeline spraying structure 3, which is close to the tail gas outlet of the granulating device 2, is connected with the first drying circulation tank 11, the concentrated phosphoric acid supply device and the ammonia absorption circulation tank 10 through pipelines, other spray heads 24 are connected with the ammonia absorption circulation tank 10 through pipelines, and the spraying amount of one spray head 24, which is close to the tail gas outlet of the granulating device 2, is 1.8-2.2 times that of the other spray heads 24.
Specifically, in the embodiment of the present invention, the diameter of the pipeline between the tail gas outlet of the granulating device 2 and the air inlet of the venturi scrubber 4 is 0.8-1.3m, the included angle between the pipeline and the horizontal plane is 10-35 degrees, the pipeline is inclined downwards from the tail gas outlet of the granulating device 2 to the air inlet at the top of the venturi scrubber 4, and a spray nozzle 24 is arranged on the axis of the pipeline at intervals of 1.2-1.8 m.
Wherein, the spray head 24 in the embodiment of the invention is arranged towards the air inlet direction of the Venturi scrubber 4, and uniformly sprays the spray liquid to the periphery to spray the spray liquid in a conical surface; the spraying amount of one spray nozzle 24 near the tail gas outlet of the granulating device 2 is 65-70m 3 And/h, the spraying amount of other spray heads 24 is 30-35m 3 /h。
Wherein, the first drying circulation tank 11, the dust collection washing circulation tank 15, the fluorine washing circulation tank 13 and the ammonia absorption circulation tank 10 in the embodiment of the invention are provided with stirrers.
Specifically, the ammonia absorption circulation tank 10 in the embodiment of the invention is lower than the venturi scrubber 4, the granulation washing tower 5 and the second drying washing tower 7, is connected with a spray liquid inlet of the granulation washing tower 5 through a pipeline with a granulation washing pump 20, is connected with a spray liquid inlet of the second drying washing tower 7 through a pipeline with a second drying washing pump 19, and is connected with a spray liquid inlet of the venturi scrubber 4 and a spray liquid inlet of the pipeline spray structure 3 through a pipeline with an ammonia absorption pump 22; the fluorine washing circulation tank 13 is respectively connected with a spray liquid inlet of the fluorine washing tower 8 and the dust collection washing circulation tank 15 through a pipeline with a fluorine washing pump 14; the dust collection washing circulation tank 15 is respectively connected with a spray liquid inlet of the dust collection washing tower 9 and the first drying circulation tank 11 through a pipeline with a dust collection washing pump 16; the first drying circulation tank 11 is connected with a spray liquid inlet of the first drying and washing tower 6 through a pipeline with a first drying and washing pump 12; the ammonia absorption circulation tank 10 is connected with the slurry tank 1 through a pipeline with a second dry washing pump 19, a granulation washing pump 20 or an ammonia absorption pump 22; a multi-way pipe is arranged on the spray liquid inlet of one spray head 24 close to the tail gas outlet of the granulating device 2; the multi-way pipe is connected with the first drying circulation tank 11 through a pipeline with a first drying washing pump 12 and a regulating valve, is connected with the ammonia absorption circulation tank 10 through a pipeline with an ammonia absorption pump 22 and a regulating valve, and is connected with a concentrated phosphoric acid supply device through a pipeline with a phosphoric acid pump 18 and a regulating valve.
In another aspect, embodiments of the present invention also provide a method of producing diammonium using the aforementioned Gao An utilization and low ammonia emission diammonium production system, the method comprising: mixing concentrated phosphoric acid with washing liquid from a tail gas treatment device in a slurry tank 1, feeding the mixed mixture into a tubular reactor to perform neutralization reaction with ammonia gas, and feeding the neutralized reaction into a granulating device 2 to perform granulation with the ammonia gas; the ammonia absorption circulating tank 10 is respectively combined with a Venturi scrubber 4, a granulating and washing tower 5 and a second drying and washing tower 7 to form circulating spraying, and washing liquid is sent to the slurry tank 1; the spray liquid of one spray head 24 near the tail gas outlet of the granulating device 2 is formed by compounding concentrated phosphoric acid, washing liquid from the first drying circulation tank 11 and washing liquid from the ammonia absorption circulation tank 10, and the density of the spray liquid is 1.48-1.49g/cm 3 The neutralization degree is 0.1-0.2; the spray liquid of the other spray heads 24 is the washing liquid from the ammonia absorption circulation tank 10, and the density is 1.51-1.53g/cm 3 The neutralization degree is 0.5-0.6.
Further, the ratio of ammonia gas to slurry from the slurry tank 1 in the tubular reactor is 0.238-0.242t/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The density of the washing liquid from the first drying circulation tank 11 is 1.12-1.18g/cm 3 The neutralization degree is less than 0.15; the mass percentage concentration of the concentrated phosphoric acid is 45-50%.
Wherein, the spray liquid of a spray head 24 near the tail gas outlet of the granulating device 2 in the embodiment of the invention is formed by compounding concentrated phosphoric acid, washing liquid from the first drying circulation tank 11 and washing liquid from the ammonia absorption circulation tank 10 according to the volume ratio of 20-30:5-9:16-24.
Specifically, in the embodiment of the present invention, the spraying amount of one nozzle 24 near the tail gas outlet of the granulating apparatus 2 is 65-70m 3 And/h, the spraying amount of other spray heads 24 is 30-35m 3 /h。
The tail gas from the drying device in the embodiment of the invention is sequentially sent to a first drying and washing tower 6, a second drying and washing tower 7 and a fluorine washing tower 8 after dust removal by a cyclone dust remover, the tail gas from the granulating device 2 is sequentially sent to a pipeline spray structure 3, a venturi scrubber 4, a granulating and washing tower 5 and a fluorine washing tower 8, and other tail gas is sequentially sent to a dust collection and washing tower 9 and a fluorine washing tower 8; the process water is supplemented at the position of the fluorine washing circulation tank 13, the fluorine washing circulation tank 13 and the fluorine washing tower 8 form circulation spraying, and the washing liquid is sent to the dust collection washing circulation tank 15, the dust collection washing circulation tank 15 and the dust collection washing tower 9 form circulation spraying, and the washing liquid is sent to the first drying circulation tank 11, and the first drying circulation tank 11 and the first drying washing tower 6 form circulation spraying, and the washing liquid is sent to a spray head 24 close to the tail gas outlet of the granulating device 2.
The technical scheme provided by the embodiment of the invention has the beneficial effects that: the embodiment of the invention provides a diammonium production system with high ammonia utilization rate and low ammonia emission and a production method thereof, wherein slurry with a certain concentration and neutralization degree is adopted to absorb ammonia dust overflowed from a granulating device, so that the tail gas absorption effect is good, no ammonia smell exists in the tail gas, the tail gas meets the tail gas emission standard, and the ammonia utilization rate is improved by about 1%; the spray density of a spray head close to the tail gas outlet of the granulating device is reduced, the spray effect is improved, the low-neutralization-degree and low-density operation is realized, the ammonia absorption capacity is improved, and the spray head and the pipeline are prevented from being blocked. The whole system has simpler structure and easy maintenance, and can reduce the use of at least two stirrers. In conclusion, the invention can increase the driving time to improve the product yield, reduce the production cost and meet the environmental protection requirement.
Drawings
FIG. 1 is a schematic block diagram of a prior art diammonium production system;
FIG. 2 is a schematic block diagram of a high ammonia utilization and low ammonia emission diammonium production system provided by this example;
FIG. 3 is a schematic diagram of a high ammonia utilization and low ammonia emission diammonium production system provided by an embodiment of the present invention;
fig. 4 is a schematic structural diagram of a pipe spray structure according to an embodiment of the present invention.
In the figure: 1 slurry tank, 2 granulation device, 3 pipeline spray structure, 4 venturi scrubber, 5 granulation washing tower, 6 first drying washing tower, 7 second drying washing tower, 8 fluorine washing tower, 9 dust collecting washing tower, 10 ammonia absorption circulation tank, 11 first drying circulation pump, 12 first drying washing pump, 13 fluorine washing circulation tank, 14 fluorine washing pump, 15 dust collecting washing circulation tank, 16 dust collecting washing pump, 17 concentrated phosphoric acid storage tank, 18 phosphoric acid pump, 19 second drying washing pump, 20 granulation washing pump, 21 slurry pump, 22 ammonia absorption pump, 23 air outlet pipe, 24 shower nozzle.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings, for the purpose of making the objects, technical solutions and advantages of the present invention more apparent.
Example 1
Referring to fig. 2-4, an embodiment of the present invention provides a high ammonia utilization and low ammonia emission diammonium production system comprising a slurry tank 1, a tubular reactor, a granulating device 2, a drying device, a tail gas treatment device, and the like. The tail gas treatment device comprises a cyclone dust collector (mainly used for dust removal), a venturi scrubber 4, a granulation washing tower 5, a first drying washing tower 6 (mainly used for dust removal), a first drying circulation tank 11, a second drying washing tower 7 (mainly used for ammonia removal), a dust collection washing tower 9, a dust collection washing circulation tank 15, a fluorine washing tower 8, a fluorine washing circulation tank 13, an ammonia absorption circulation tank 10 and the like; the tail gas outlet of the granulating device 2, the Venturi scrubber 4, the granulating and washing tower 5 and the fluorine washing tower 8 are sequentially connected through pipelines to form a granulating tail gas treatment channel for treating granulating tail gas, a pipeline spray structure 3 is arranged on a pipeline (an air outlet pipe 23) between the tail gas outlet of the granulating device 2 and an air inlet of the Venturi scrubber 4, and the pipeline spray structure 3 comprises a plurality of spray heads 24 (vortex nozzles) arranged in the pipeline (the air outlet pipe 23). The tail gas outlet of the drying device, the cyclone dust collector, the first drying washing tower 6, the second drying washing tower 7 and the fluorine washing tower 8 are sequentially connected through pipelines to form a drying tail gas treatment channel for treating the drying tail gas. The dust collection washing tower 9 is used for collecting other tail gases (cooling tail gases, reaction tank tail gases, screening tail gases, conveyor belt dust collection and the like) except the granulation tail gases and the drying tail gases, and a tail gas outlet of the dust collection washing tower is connected with the fluorine washing tower 8 through a pipeline for treating the other tail gases. The fluorine washing circulation tank 13 and the fluorine washing tower 8 form a circulating spray structure and are connected with the dust collection washing circulation tank 15 through a pipeline, process water (tap water or recycled wastewater and the like) is supplemented at the position of the fluorine washing circulation tank 13, and the dust collection washing circulation tank 15 and the dust collection washing tower 9 form a circulating spray structure and are connected with the first drying circulation tank 11 through a pipeline. The ammonia absorption circulation tank 10 (which is large in volume and requires three spray circulation towers to be supplied simultaneously) forms a circulation spray structure with the venturi scrubber 4, the granulation scrubber 5 and the second drying tower 7, respectively, and is connected with the slurry tank 1 (output to the tubular reactor through the slurry pump 21) through a pipeline for delivering the washing liquid with a certain concentration to the slurry tank for utilizing the washing liquid. The pipe spray structure 3 is connected with the first drying circulation tank 11, the concentrated phosphoric acid supply device (concentrated phosphoric acid storage tank 17) and the ammonia absorption circulation tank 10 through pipes to compound three liquids to obtain a spray liquid meeting requirements, and the other spray heads 24 (except for the spray head 24 near the tail gas outlet of the granulating device 2) are connected with the ammonia absorption circulation tank 10 through pipes, wherein the spray amount of the spray head 24 near the tail gas outlet of the granulating device 2 is 1.8-2.2 times that of the spray amount of the other spray heads 24 (single).
Specifically, referring to fig. 3 and 4, in the embodiment of the present invention, the diameter of the pipe (circular straight hanging) between the tail gas outlet of the granulating device 2 and the air inlet of the venturi scrubber 4 is 0.8-1.3m, and the included angle between the pipe and the horizontal plane is 10-35 °, and a nozzle 24 is arranged on the axis of the pipe at intervals of 1.2-1.8m from the tail gas outlet of the granulating device 2 obliquely downward to the air inlet at the top of the venturi scrubber 4.
Referring to fig. 3 and 4, the spray head 24 in the embodiment of the present invention is disposed towards the air inlet of the venturi scrubber 4, and sprays the spray liquid uniformly to the periphery to spray the spray liquid in a conical surface (specifically, a vortex nozzle, the angle of the cone is not required, and the cone angle is preferably 90-150 °); the spraying amount of one spray nozzle 24 near the tail gas outlet of the granulating device 2 is 65-70m 3 And/h, the spraying amount of other spray heads 24 is 30-35m 3 /h。
Wherein, the first drying circulation tank 11, the dust collection washing circulation tank 15, the fluorine washing circulation tank 13 and the ammonia absorption circulation tank 10 in the embodiment of the invention are provided with stirrers.
Specifically, the ammonia absorption circulation tank 10 in the embodiment of the present invention is lower than the venturi scrubber 4, the prilling scrubber 5, and the second drying scrubber 7, and is located directly below the venturi scrubber 4, the prilling scrubber 5, and the second drying scrubber 7 (specifically, a ground tank), and is connected to the spray liquid inlet of the prilling scrubber 5 through a pipeline with a prilling scrubber pump 20, and is connected to the spray liquid inlet of the second drying scrubber 7 through a pipeline with a second drying scrubber pump 19, and is connected to the spray liquid inlet of the venturi scrubber 4 and the spray liquid inlet of the pipe spray structure 3 through a pipeline with an ammonia absorption pump 22. The fluorine washing circulation tank 13 (specifically, a geosyncline, which is arranged right below the fluorine washing tower 8 and is connected with the washing liquid treatment at the bottom of the washing tower through a pipeline) is respectively connected with a spray liquid inlet of the fluorine washing tower 8 and the dust collection washing circulation tank 15 through a pipeline with a fluorine washing pump 14. The dust collection washing circulation tank 15 (specifically, a ground tank, which is arranged right below the dust collection washing tower 9) is respectively connected with a spray liquid inlet of the dust collection washing tower 9 and the first drying circulation tank 11 through a pipeline with a dust collection washing pump 16. The first drying circulation tank 11 (specifically, a ground tank, provided immediately below the first drying and washing tower 6) is connected to the spray liquid inlet of the first drying and washing tower 6 through a pipe line with a first drying and washing pump 12. The ammonia absorption circulation tank 10 is connected to the slurry tank 1 through a pipe line with a second dry washing pump 19, a granulation washing pump 20 or an ammonia absorption pump 22. A multi-way pipe is arranged on the spray liquid inlet of one spray head 24 close to the tail gas outlet of the granulating device 2; the multi-way pipe is connected to the first drying circulation tank 11 via a line with the first drying and washing pump 12 and the regulating valve, it is connected to the ammonia absorption circulation tank 10 via a line with the second drying and washing pump 19, the granulation and washing pump 20 or the ammonia absorption pump 22 (preferably the ammonia absorption pump 22) and the regulating valve, and it is connected to the concentrated phosphoric acid supply via a line with the phosphoric acid pump 18 and the regulating valve.
The piping between the foregoing structures is provided with pumps, fans, valves and/or flow meters, etc. as needed, as is well known to those skilled in the art.
Example 2
Referring to fig. 2-4, example 2 provides a process for producing diammonium using the high ammonia utilization and low ammonia emission diammonium production system of example 1, the process comprising:
the concentrated phosphoric acid and the washing liquid from the tail gas treatment device are mixed in a slurry tank 1 (ammonia is or is not fed), the mixed washing liquid and ammonia are subjected to neutralization reaction (phosphoric acid is or is not fed) in a tubular reactor, the reaction mixture is fed into a granulating device 2 to react with the ammonia for granulation after the neutralization reaction, the tail gas treatment device is used for absorbing tail gas of the granulating device, tail gas of a drying device and other tail gases, and the washing liquid is fed into the slurry tank 1. The ammonia absorption circulation tank 10 forms circulation spraying with the Venturi scrubber 4, the granulation washing tower 5 and the second drying washing tower 7 respectively, and the washing liquid is sent to the slurry tank 1. The spray liquid of one spray head 24 near the exhaust outlet of the granulating apparatus 2 is composed of concentrated phosphoric acid (concentration 45-50%), the washing liquid from the first drying circulation tank 11 (density 1.12-1.18 g/cm) 3 Neutralization < 0.15) and a washing liquid (density of 1.51-1.53 g/cm) from the ammonia absorption circulation tank 10 3 Neutralization degree of 0.5-0.6), the density of the spray liquid is 1.48-1.49g/cm 3 The neutralization degree is 0.1-0.2, and the tail gas treatment effect is best and the equipment cannot be blocked through experiments;the spray liquid of the other spray heads 24 is the washing liquid from the ammonia absorption circulation tank 10, and the density is 1.51-1.53g/cm 3 The neutralization degree is 0.5-0.6.
Further, the ratio of ammonia gas to slurry from the slurry tank 1 in the tubular reactor is 0.238-0.242t/m 3 (0.245 t/m before improvement) 3 Left and right); the density of the washing liquid from the first drying circulation tank 11 is 1.12-1.18g/cm 3 The neutralization degree is less than 0.15; the mass percentage concentration of the concentrated phosphoric acid is 45-50% (46% or 48% in general).
Wherein, the spray liquid of a spray head 24 near the tail gas outlet of the granulating device 2 in the embodiment of the invention is formed by compounding concentrated phosphoric acid, washing liquid from the first drying circulation tank 11 and washing liquid from the ammonia absorption circulation tank 10 according to the volume ratio of 20-30:5-9:16-24.
Specifically, in the embodiment of the present invention, the spraying amount of one nozzle 24 near the tail gas outlet of the granulating apparatus 2 is 65-70m 3 And/h, the spraying amount of other spray heads 24 is 30-35m 3 /h。
The tail gas from the drying device in the embodiment of the invention is dedusted by a cyclone, and then sequentially sent to a first drying and washing tower 6, a second drying and washing tower 7 and a fluorine washing tower 8 (dry tail gas treatment process), the tail gas from the granulating device 2 is sequentially sent to a pipeline spray structure 3, a venturi scrubber 4, a granulating and washing tower 5 and a fluorine washing tower 8 (granulation tail gas treatment process), and other tail gas is sequentially sent to a dust collecting and washing tower 9 and a fluorine washing tower 8 (other tail gas treatment process). The process water is supplemented at the position of the fluorine washing circulation tank 13, the fluorine washing circulation tank 13 and the fluorine washing tower 8 form circulation spraying, the washing liquid is sent to the dust collection washing circulation tank 15, the dust collection washing circulation tank 15 and the dust collection washing tower 9 form circulation spraying, the washing liquid is sent to the first drying circulation tank 11, the first drying circulation tank 11 and the first drying washing tower 6 form circulation spraying, and the washing liquid is sent to a spray head 24 close to the tail gas outlet of the granulating device 2.
The "first" and "second" in this embodiment are only used for distinguishing, and have no other special meaning.
The following is a simple accounting (model is simpler) of the improved system:
1. the power of the two stirring paddles is 15KW, the annual period is 15KW, 2=30 KW, 24H, 330 days is approximately equal to 230000 degrees, 0.6 yuan=14.3 ten thousand yuan.
2. Annual yield 24 ten thousand tons of diammonium to calculate ammonia yield: 240000 x 0.18 x 17/14 x 0.01= 524.57 tons of ammonia, for a total of 157.37 ten thousand tons of liquid ammonia per 3000 tons of liquid ammonia.
3. An ammonia recovery circulating tank is newly built to invest 30 ten thousand yuan (three sets of tank equipment can be used in other workshops and can resist part of cost).
The profit of the current year after transformation is more obtained by 157.37+14.3-30= 141.67 ten thousand yuan (no maintenance and parking cost is counted).
4. The pipeline and the spray head can not be blocked after transformation, only 1 routine maintenance in a quarter is needed, the driving time can be prolonged, at least 2 hours are overhauled each time in the prior art, at least 2 people can extend the driving time for at least 24 hours in the whole year (the yield can be improved by 240000/330=727 tons).
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (9)
1. A diammonium production system with high ammonia utilization rate and low ammonia emission comprises a slurry tank (1), a tubular reactor, a granulating device (2), a drying device and a tail gas treatment device;
the tail gas treatment device comprises a cyclone separator, a Venturi scrubber (4), a granulation washing tower (5), a first drying washing tower (6), a first drying circulation tank (11), a second drying washing tower (7), a dust collection washing tower (9), a dust collection washing circulation tank (15), a fluorine washing tower (8) and a fluorine washing circulation tank (13);
the tail gas outlet of the granulating device (2), the Venturi scrubber (4), the granulating and scrubbing tower (5) and the fluorine scrubbing tower (8) are sequentially connected through pipelines to form a granulating tail gas treatment channel, a pipeline spray structure (3) is arranged on a pipeline between the tail gas outlet of the granulating device (2) and the air inlet of the Venturi scrubber (4), and the pipeline spray structure (4) comprises a plurality of spray heads (24) arranged in the pipeline;
the tail gas outlet of the drying device, the cyclone separator, the first drying washing tower (6), the second drying washing tower (7) and the fluorine washing tower (8) are sequentially connected through pipelines to form a drying tail gas treatment channel;
the dust collection washing tower (9) is used for collecting other tail gases except granulation tail gases and drying tail gases, and a tail gas outlet of the dust collection washing tower is connected with the fluorine washing tower (8) through a pipeline;
the fluorine washing circulation tank (13) and the fluorine washing tower (8) form a circulating spray structure and are connected with the dust collection washing circulation tank (15) through a pipeline, process water is supplemented at the position of the fluorine washing circulation tank (13), the dust collection washing circulation tank (15) and the dust collection washing tower (9) form a circulating spray structure and are connected with the first drying circulation tank (11) through a pipeline; it is characterized in that the method comprises the steps of,
the tail gas treatment device also comprises an ammonia absorption circulating groove (10); the ammonia absorption circulation tank (10) is respectively connected with the venturi scrubber (4), the granulation washing tower (5) and the second drying washing tower (7) to form a circulation spraying structure, and the circulation spraying structure is connected with the slurry tank (1) through a pipeline; one spray head (24) of the pipeline spray structure (3) close to the tail gas outlet of the granulating device (2) is connected with the first drying circulation tank (11), the concentrated phosphoric acid supply device and the ammonia absorption circulation tank (10) through pipelines, other spray heads (24) are connected with the ammonia absorption circulation tank (10) through pipelines, and the spraying amount of one spray head (24) close to the tail gas outlet of the granulating device (2) is 1.8-2.2 times of the spraying amount of the other spray heads (24);
the spray head (24) is arranged towards the air inlet direction of the Venturi scrubber (4) and uniformly sprays the spray liquid to the periphery to spray the spray liquid in a conical surface; the spraying amount of a spray nozzle (24) close to the tail gas outlet of the granulating device (2) is 65-70m 3 And/h, the spraying amount of other spray heads (24) is 30-35m 3 /h；
The spray liquid of a spray head (24) close to the tail gas outlet of the granulating device (2) is formed by compounding concentrated phosphoric acid, washing liquid from a first drying circulation tank (11) and washing liquid from an ammonia absorption circulation tank (10), and the density of the spray liquid is 1.48-1.49g/cm 3 The neutralization degree is 0.1-0.2; the spray liquid of other spray heads (24) is the wash liquid from the ammonia absorption circulation tank (10) with the density of 1.51-1.53g/cm 3 Middle (a)The sum is 0.5-0.6.
2. The high ammonia utilization and low ammonia emission diammonium production system according to claim 1, characterized in that the diameter of the pipe between the tail gas outlet of the prilling device (2) and the air inlet of the venturi scrubber (4) is 0.8-1.3m and its angle with the horizontal is 10-35 °, and that a spray head (24) is arranged at intervals of 1.2-1.8m on the axis from the tail gas outlet of the prilling device (2) obliquely downwards to the air inlet at the top of the venturi scrubber (4).
3. The high ammonia utilization and low ammonia emission diammonium production system according to claim 1, wherein agitators are arranged in the first drying circulation tank (11), the dust collection washing circulation tank (15), the fluorine washing circulation tank (13) and the ammonia absorption circulation tank (10).
4. The high ammonia utilization and low ammonia emission diammonium production system according to claim 1, characterized in that the ammonia absorption circulation tank (10) is lower than the venturi scrubber (4), the prilling scrubber (5) and the second drying scrubber (7), which is connected to the spray liquid inlet of the prilling scrubber (5) by a pipe with a prilling scrubber pump (20), which is connected to the spray liquid inlet of the second drying scrubber (7) by a pipe with a second drying scrubber pump (19), which is connected to the spray liquid inlet of the venturi scrubber (4) and to the spray liquid inlet of the pipe spray structure (3) by a pipe with an ammonia absorption pump (22); the fluorine washing circulation tank (13) is respectively connected with a spray liquid inlet of the fluorine washing tower (8) and the dust collection washing circulation tank (15) through a pipeline with a fluorine washing pump (14); the dust collection washing circulation tank (15) is respectively connected with a spray liquid inlet of the dust collection washing tower (9) and the first drying circulation tank (11) through a pipeline with a dust collection washing pump (16); the first drying circulation tank (11) is connected with a spray liquid inlet of the first drying washing tower (6) through a pipeline with a first drying washing pump (12); the ammonia absorption circulation tank (10) is connected with the slurry tank (1) through a pipeline with a second drying and washing pump (19), a granulating and washing pump (20) or an ammonia absorption pump (22); a multi-way pipe is arranged on a spray liquid inlet of a spray head (24) close to a tail gas outlet of the granulating device (2); the multi-way pipe is connected with the first drying circulation tank (11) through a pipeline with a first drying washing pump (12) and a regulating valve, is connected with the ammonia absorption circulation tank (10) through a pipeline with an ammonia absorption pump (22) and a regulating valve, and is connected with the concentrated phosphoric acid supply device through a pipeline with a phosphoric acid pump (18) and a regulating valve.
5. A process for producing diammonium using the high ammonia utilization and low ammonia emission diammonium production system of any one of claims 1-4, the process comprising: mixing concentrated phosphoric acid with washing liquid from a tail gas treatment device in a slurry tank (1), feeding the mixed mixture into a tubular reactor to perform neutralization reaction with ammonia gas, and feeding the neutralized reaction into a granulating device (2) to perform granulation with the ammonia gas; it is characterized in that the method comprises the steps of,
the ammonia absorption circulation tank (10) respectively forms circulation spraying with the Venturi scrubber (4), the granulation washing tower (5) and the second drying washing tower (7), and the washing liquid is sent to the slurry tank (1); the spray liquid of a spray head (24) close to the tail gas outlet of the granulating device (2) is formed by compounding concentrated phosphoric acid, washing liquid from a first drying circulation tank (11) and washing liquid from an ammonia absorption circulation tank (10), and the density of the spray liquid is 1.48-1.49g/cm 3 The neutralization degree is 0.1-0.2; the spray liquid of other spray heads (24) is the wash liquid from the ammonia absorption circulation tank (10) with the density of 1.51-1.53g/cm 3 The neutralization degree is 0.5-0.6.
6. The production method according to claim 5, characterized in that the ratio of ammonia gas to slurry from the slurry tank (1) in the tubular reactor is 0.238-0.242t/m 3 The method comprises the steps of carrying out a first treatment on the surface of the The density of the washing liquid from the first drying circulation tank (11) is 1.12-1.18g/cm 3 The neutralization degree is less than 0.15; the mass percentage concentration of the concentrated phosphoric acid is 45-50%.
7. The production method according to claim 5, characterized in that the spray liquid of one spray head (24) near the tail gas outlet of the granulating device (2) is composed of concentrated phosphoric acid, the washing liquid from the first drying circulation tank (11) and the washing liquid from the ammonia absorption circulation tank (10) in a volume ratio of 20-30:5-9:16-24.
8. The production method according to claim 5, characterized in that the spraying amount of one spray head (24) near the tail gas outlet of the granulating device (2) is 65-70m 3 And/h, the spraying amount of other spray heads (24) is 30-35m 3 /h。
9. The production method according to claim 5, wherein the tail gas from the drying device is sequentially sent to a first drying washing tower (6), a second drying washing tower (7) and a fluorine washing tower (8) after dust removal by a cyclone dust remover, the tail gas from the granulating device (2) is sequentially sent to a pipeline spray structure (3), a venturi scrubber (4), a granulating washing tower (5) and a fluorine washing tower (8), and the other tail gas is sequentially sent to a dust collection washing tower (9) and a fluorine washing tower (8); the method comprises the steps that process water is supplemented at a fluorine washing circulation tank (13), the fluorine washing circulation tank (13) and a fluorine washing tower (8) form circulation spraying, washing liquid is sent to a dust collection washing circulation tank (15), the dust collection washing circulation tank (15) and a dust collection washing tower (9) form circulation spraying, washing liquid is sent to a first drying circulation tank (11), the first drying circulation tank (11) and a first drying washing tower (6) form circulation spraying, and washing liquid is sent to a spray head (24) close to a tail gas outlet of a granulating device (2).
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101549861A (en) * | 2009-04-24 | 2009-10-07 | 瓮福（集团）有限责任公司 | A diammonium phosphate exhaust washing method |
| CN204093287U (en) * | 2014-08-29 | 2015-01-14 | 甘肃瓮福化工有限责任公司 | The recycling system of ammonia in tail gas |
| CN104511239A (en) * | 2013-12-18 | 2015-04-15 | 广西鹿寨化肥有限责任公司 | Method for improving washing effect of ammonium phosphate granulation tail gas |
| CN105013310A (en) * | 2015-07-08 | 2015-11-04 | 瓮福（集团）有限责任公司 | Ammonium phosphate granulating tail gas washing device and method |
| CN106348267A (en) * | 2016-08-29 | 2017-01-25 | 宜都兴发化工有限公司 | Method for producing diammonium phosphate with nitrogen and phosphorus containing wastewater |
| RU2016120297A (en) * | 2016-05-25 | 2017-11-28 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Московский технологический университет" | METHOD FOR GRANULATING MINERAL FERTILIZERS |
| CN207856566U (en) * | 2018-01-03 | 2018-09-14 | 湖北祥云(集团)化工股份有限公司 | A kind of exhaust gas processing device being used for composite fertilizer and non-wastewater discharge |
-
2019
- 2019-09-10 CN CN201910851384.0A patent/CN110562944B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101549861A (en) * | 2009-04-24 | 2009-10-07 | 瓮福（集团）有限责任公司 | A diammonium phosphate exhaust washing method |
| CN104511239A (en) * | 2013-12-18 | 2015-04-15 | 广西鹿寨化肥有限责任公司 | Method for improving washing effect of ammonium phosphate granulation tail gas |
| CN204093287U (en) * | 2014-08-29 | 2015-01-14 | 甘肃瓮福化工有限责任公司 | The recycling system of ammonia in tail gas |
| CN105013310A (en) * | 2015-07-08 | 2015-11-04 | 瓮福（集团）有限责任公司 | Ammonium phosphate granulating tail gas washing device and method |
| RU2016120297A (en) * | 2016-05-25 | 2017-11-28 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Московский технологический университет" | METHOD FOR GRANULATING MINERAL FERTILIZERS |
| CN106348267A (en) * | 2016-08-29 | 2017-01-25 | 宜都兴发化工有限公司 | Method for producing diammonium phosphate with nitrogen and phosphorus containing wastewater |
| CN207856566U (en) * | 2018-01-03 | 2018-09-14 | 湖北祥云(集团)化工股份有限公司 | A kind of exhaust gas processing device being used for composite fertilizer and non-wastewater discharge |
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Denomination of invention: A high ammonia utilization rate and low ammonia emission diammonium production system and production method Effective date of registration: 20230731 Granted publication date: 20230512 Pledgee: Bank of China Limited Huanggang branch Pledgor: HUBEI XIANGYUN (Group) CHEMICAL Co.,Ltd. Registration number: Y2023420000318 |