CN220034363U - Liquid ammonium polyphosphate fertilizer apparatus for producing - Google Patents
Liquid ammonium polyphosphate fertilizer apparatus for producing Download PDFInfo
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- CN220034363U CN220034363U CN202321500468.8U CN202321500468U CN220034363U CN 220034363 U CN220034363 U CN 220034363U CN 202321500468 U CN202321500468 U CN 202321500468U CN 220034363 U CN220034363 U CN 220034363U
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- storage tank
- liquid
- heat exchanger
- washing
- ammonium polyphosphate
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- 239000007788 liquid Substances 0.000 title claims abstract description 86
- 239000004114 Ammonium polyphosphate Substances 0.000 title claims abstract description 60
- 235000019826 ammonium polyphosphate Nutrition 0.000 title claims abstract description 60
- 229920001276 ammonium polyphosphate Polymers 0.000 title claims abstract description 60
- 239000003337 fertilizer Substances 0.000 title claims abstract description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 87
- 238000005406 washing Methods 0.000 claims abstract description 77
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000003860 storage Methods 0.000 claims abstract description 70
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 40
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 35
- 238000004519 manufacturing process Methods 0.000 claims abstract description 29
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000004202 carbamide Substances 0.000 claims abstract description 8
- 229910021529 ammonia Inorganic materials 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000004090 dissolution Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 229920006395 saturated elastomer Polymers 0.000 claims description 7
- 239000013505 freshwater Substances 0.000 claims description 5
- 238000005201 scrubbing Methods 0.000 claims description 4
- 239000012141 concentrate Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 16
- 238000006386 neutralization reaction Methods 0.000 abstract description 11
- 238000001816 cooling Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 150000001413 amino acids Chemical class 0.000 abstract description 5
- 238000001704 evaporation Methods 0.000 abstract description 4
- 230000008020 evaporation Effects 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 20
- 239000007789 gas Substances 0.000 description 19
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000002994 raw material Substances 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000006261 foam material Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000012768 molten material Substances 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 229920000137 polyphosphoric acid Polymers 0.000 description 3
- 239000012047 saturated solution Substances 0.000 description 3
- 239000002689 soil Substances 0.000 description 3
- 239000011573 trace mineral Substances 0.000 description 3
- 235000013619 trace mineral Nutrition 0.000 description 3
- WTHDKMILWLGDKL-UHFFFAOYSA-N urea;hydrate Chemical compound O.NC(N)=O WTHDKMILWLGDKL-UHFFFAOYSA-N 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- DLYUQMMRRRQYAE-UHFFFAOYSA-N tetraphosphorus decaoxide Chemical compound O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 description 2
- 239000004254 Ammonium phosphate Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- DZHMRSPXDUUJER-UHFFFAOYSA-N [amino(hydroxy)methylidene]azanium;dihydrogen phosphate Chemical compound NC(N)=O.OP(O)(O)=O DZHMRSPXDUUJER-UHFFFAOYSA-N 0.000 description 1
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 description 1
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 description 1
- 229910000148 ammonium phosphate Inorganic materials 0.000 description 1
- 235000019289 ammonium phosphates Nutrition 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000013522 chelant Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 235000019837 monoammonium phosphate Nutrition 0.000 description 1
- 239000006012 monoammonium phosphate Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000000379 polymerizing effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
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- Fertilizers (AREA)
Abstract
The utility model relates to the technical field of production of liquid ammonium polyphosphate fertilizer products, in particular to a liquid ammonium polyphosphate fertilizer production device, wherein a tail gas washing system comprises a first-stage washing tower, a washing liquid storage tank and a washing pump which are sequentially connected, one side of the washing liquid storage tank is provided with a phosphoric acid inlet, and a liquid outlet of the washing pump is respectively connected with the first-stage washing tower and a second-stage heat exchanger; the concentration system comprises a concentration pump, a heater, a concentration tower and a concentrated solution storage tank which are connected in sequence, and a urea feed inlet is arranged on the concentrated solution storage tank; the feed inlet of the polymerization reaction system is connected with a concentrated solution storage tank through a tubular reactor, the polymerization reaction system is connected with a primary heat exchanger and a temporary storage tank in sequence, and the temporary storage tank is connected with a secondary heat exchanger and a product storage tank. The method adopts the mode of separating and recycling the heat of the neutralization reaction of the amino acid in a sectional way, reduces the energy consumption of phosphoric acid concentration, liquid ammonia evaporation and product cooling, and reduces the energy consumption cost of product cooling while fully utilizing the heat of the neutralization reaction of the amino acid.
Description
Technical Field
The utility model relates to the technical field of liquid ammonium polyphosphate fertilizer production, in particular to a liquid ammonium polyphosphate fertilizer production device.
Background
Ammonium polyphosphate fertilizer is a product obtained by polymerizing phosphorus sources such as polyphosphoric acid, hot phosphoric acid, refined phosphoric acid, industrial monoammonium phosphate and urea phosphate, and nitrogen sources such as ammonia and urea under certain process conditions, and the polymerization degree is generally 2-10, and can be classified into solid ammonium polyphosphate and liquid ammonium polyphosphate according to the form of the product. The ammonium polyphosphate fertilizer has a certain chelating function, can chelate calcium, magnesium, zinc, iron and other ions contained in the soil, is not easy to fix when being applied to the soil, and can improve the migration distance of phosphorus in the soil, thereby improving the utilization rate of phosphorus elements.
For a long time, domestic studies have made a lot of literature on the production of ammonium polyphosphate from wet phosphoric acid, wherein CN104528682a discloses a method for preparing an aqueous solution of fully water-soluble ammonium polyphosphate from wet phosphoric acid, which mainly comprises: the wet-process phosphoric acid with concentration of 30-80% and ammonia gas are heated to 150-300 deg.C, and the condensation reaction is continuously carried out in the liquid environment formed by mixing wet-process phosphoric acid, ammonia gas, ammonium phosphate, ammonium polyphosphate and water, so as to initially prepare ammonium polyphosphate water solution. However, the polymerization process of ammonium polyphosphate is a dehydration process, and the polymerization in a water-soluble environment of the method inevitably requires high polymerization temperature conditions and high energy consumption. CN107892278A discloses a method for producing water-soluble ammonium polyphosphate liquid, which mainly comprises: industrial wet phosphoric acid, liquid ammonia and gas ammonia are used as raw materials, high-temperature molten materials are prepared through tubular neutralization polycondensation reaction and further neutralization polycondensation reaction in a polymerization kettle, and then the molten materials are cooled in a water-soluble ammonium polyphosphate water agent preparation tank with a cooling jacket to prepare ammonium polyphosphate liquid; the method has high requirement on the concentration of phosphoric acid, the mass fraction of phosphoric acid is 72-76% based on phosphorus pentoxide, and the method is a batch reaction, so that the production scale is difficult to expand.
At present, the main liquid ammonium polyphosphate in the market mainly takes TVA in the United states as a process developed in the sixty of the last century, takes polyphosphoric acid, hot phosphoric acid, industrial wet phosphoric acid and the like as main raw materials, and partially passes through ammonia to neutralize in a tubular reactor to generate a molten material, the molten material is further ammoniated after being added into a mixing tank, and meanwhile, the liquid material in the mixing tank removes excessive reaction heat through an external circulation cooling system, so that the temperature of the material in the mixing tank is kept below 80 ℃. The process has high requirements on the quality of raw material phosphoric acid, and the production of polyphosphoric acid and hot phosphoric acid belongs to high energy consumption production; when industrial wet phosphoric acid is used as raw material, the phosphoric acid needs to be concentrated to 75% or 85% of phosphoric acid content. However, in the production process of liquid ammonium polyphosphate, in order to avoid hydrolysis of ammonium polyphosphate, a large amount of reaction heat needs to be removed by an external circulation cooling device, resulting in waste of reaction heat. In addition, in the industrial wet-process phosphoric acid production process, the cost is high, and the agricultural beneficial elements such as calcium, magnesium, sulfur, iron and the like contained in the wet-process phosphoric acid are removed.
In summary, the problems of high requirements on the quality of raw material phosphoric acid, waste of reaction heat, high production cost, insufficient full quantitative utilization of medium trace element resources contained in wet-process phosphoric acid and the like exist in the traditional liquid ammonium polyphosphate production process and device. Therefore, there is an urgent need for a device for continuously and stably producing liquid ammonium polyphosphate fertilizer by using wet phosphoric acid as a raw material on the basis of fully utilizing the neutralization reaction heat of medium trace elements and amino acids in phosphoric acid.
Disclosure of Invention
The utility model aims to provide a liquid ammonium polyphosphate fertilizer production device, which solves the problems of high requirements on the quality of raw material phosphoric acid, waste of reaction heat, high production cost, insufficient full utilization of medium trace element resources contained in wet phosphoric acid and the like in the traditional liquid ammonium polyphosphate production process and device provided in the background art.
In order to achieve the above object, the present utility model provides a liquid ammonium polyphosphate fertilizer production apparatus, which is characterized in that: the device comprises a concentration system, a polymerization reaction system and a tail gas washing system, wherein the tail gas washing system comprises a first-stage washing tower, a washing liquid storage tank and a washing pump which are sequentially connected, one side of the washing liquid storage tank is provided with a phosphoric acid inlet, and a liquid outlet of the washing pump is respectively connected with the first-stage washing tower and a second-stage heat exchanger; the concentration system comprises a concentration pump, a heater, a concentration tower and a concentrated solution storage tank which are sequentially connected, wherein a urea feed inlet is formed in the concentrated solution storage tank, the concentrated solution storage tank is connected with the feed inlet of the concentration pump, and the feed inlet of the concentration pump is also connected with the secondary heat exchanger; the feed inlet of the polymerization reaction system is connected with the concentrated solution storage tank through the tubular reactor, the discharge outlet of the polymerization reaction system is sequentially connected with the primary heat exchanger and the temporary storage tank, the temporary storage tank is connected with the product feed inlet of the secondary heat exchanger, the product discharge outlet on the secondary heat exchanger is connected with the product storage tank, the liquid inlet of the primary heat exchanger is connected with the liquid ammonia providing device, the outlet of the primary heat exchanger is connected with the ammonia inlet of the tubular reactor, and the air inlet of the primary washing tower is connected with the air outlet of the polymerization reaction system.
Preferably, a liquid ammonia feeding port is arranged on one side of the temporary storage tank, and the liquid ammonia feeding port is connected with the liquid ammonia providing device.
Preferably, an ammonia storage tank is arranged between the outlet of the primary heat exchanger and the ammonia inlet of the tubular reactor, a tertiary heat exchanger is arranged between the secondary heat exchanger and the product storage tank, a liquid inlet of the tertiary heat exchanger is connected with the liquid ammonia providing device, and an exhaust port of the tertiary heat exchanger is connected with the ammonia storage tank.
Preferably, the polymerization reaction system comprises a flash chamber and a polymerization tank which are sequentially connected, wherein an overflow port of the polymerization tank is connected with a dissolution tank, an outlet of the dissolution tank is connected with a collecting tank, and a discharge port of the collecting tank is connected with a primary heat exchanger; the heat source of the polymerization tank is provided by a heating system.
Preferably, one side of the upper part of the heater is provided with a saturated steam inlet, and the other side of the lower part of the heater is provided with a condensate outlet.
Preferably, a venturi scrubber is arranged at the air inlet of the primary scrubbing tower, and the liquid outlet of the scrubbing pump is connected with the inlet of the venturi scrubber.
Preferably, the air outlet of the first-stage washing tower is connected with the air inlet of the second-stage washing tower, a water inlet is arranged at the air inlet of the second-stage washing tower, and a washing liquid outlet at the bottom of the second-stage washing tower is connected with the washing liquid storage tank.
Preferably, the product discharge port of the three-stage heat exchanger is also connected with the dissolution tank through a circulating pipeline, and the circulating pipeline is provided with a fresh water feed port.
Compared with the prior art, the utility model has the beneficial effects that:
1. in the liquid ammonium polyphosphate fertilizer production device, the mode of separating points and recycling the heat of the neutralization reaction of the amino acid in a sectional way is adopted, so that the energy consumption of phosphoric acid concentration, liquid ammonia evaporation and product cooling is reduced, the contradiction problem that the quality control of the product needs external circulation cooling when the raw materials are heated at high temperature in pretreatment of the traditional liquid ammonium polyphosphate device is effectively solved, and the energy consumption cost of product cooling is reduced while the heat of the neutralization reaction of the amino acid is fully utilized.
2. In the liquid ammonium polyphosphate fertilizer production device, the processes of continuous neutralization reaction, gas-liquid separation, polymerization reaction and dissolution absorption are carried out by adopting step-by-step separation equipment, so that the independent and unified organic combination of the neutralization reaction, the gas-liquid separation, the polymerization reaction and the dissolution absorption is realized, the problems of low polymerization efficiency and high energy consumption in water environment at high temperature in the traditional liquid ammonium polyphosphate production are effectively solved, the polymerization efficiency is improved, and the polymerization energy consumption cost is reduced.
3. In the liquid ammonium polyphosphate fertilizer production device, the mode of tail gas washing and polymerization reaction separation is adopted, so that the problem of low ammonia gas efficiency in washing and absorbing polymerization tail gas under the high-temperature condition in the traditional liquid ammonium polyphosphate device is effectively solved, and the environmental protection input cost is saved.
Drawings
FIG. 1 is a schematic diagram of the structure of the present utility model;
FIG. 2 is a schematic diagram of a concentrating system according to the present disclosure;
FIG. 3 is a schematic structural diagram of a polymerization system of the present utility model;
FIG. 4 is a schematic diagram of an exhaust gas scrubbing system according to the present disclosure;
the meaning of each reference sign in the figure is:
1. a water inlet; 2. a second-stage scrubber; 3. a washing liquid storage tank; 4. a phosphoric acid inlet; 5. a washing pump; 6. a venturi scrubber; 7. a first-stage washing tower; 8. a tail gas fan; 9. a concentrating branch; 10. a secondary heat exchanger; 11. a concentrate pump inlet manifold; 12. a concentration pump; 13. a heater; 14. a saturated steam inlet; 15. a condensate outlet; 16. a concentration tower; 17. a concentrate storage tank; 18. urea feed inlet; 19. a feed pump; 20. a tubular reactor; 21. a flash chamber; 22. a polymerization tank; 23. a heating system; 24. a dissolution tank; 25. a collection tank; 26. a material liquid pump; 27. a primary heat exchanger; 28. a temporary storage tank; 29. a liquid ammonia feed inlet; 30. a circulation pump; 31. a three-stage heat exchanger; 32. a circulation line; 33. fresh water feed inlet; 34. a first liquid ammonia inlet; 35. a second liquid ammonia inlet; 36. an ammonia storage tank; 37. an ammonia supply line; 38. a product take-out port; 39. product storage tank.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The utility model provides a liquid ammonium polyphosphate fertilizer production device, which is shown in fig. 1-4, and comprises an exhaust gas washing system, a concentration system and a polymerization reaction system, wherein the exhaust gas washing and absorbing system comprises a secondary washing tower 2, a washing liquid storage tank 3 and a primary washing tower 7, the concentration system comprises a secondary heat exchanger 10, a heater 13, a concentration tower 16 and a concentrated liquid storage tank 17, the polymerization reaction system comprises a tubular reactor 20, a flash chamber 21, a polymerization tank 22, a dissolving tank 24, a collecting tank 25, a primary heat exchanger 27, a temporary storage tank 28, and further comprises an ammonia storage tank 36, a tertiary heat exchanger 31, a circulating pipeline 32 and a product storage tank 39.
In this embodiment, water is sent into the secondary washing tower 2 through the water inlet 1 and then enters the washing liquid storage tank 3, the washing liquid storage tank 3 is communicated with the primary washing tower 7 through the venturi scrubber 6 by the washing pump 5, one side of the primary washing tower 7 is connected with the flash chamber 21 through a pipeline, the other side of the primary washing tower 7 is communicated with the secondary washing tower 2 through the tail gas fan 8, a phosphoric acid inlet 4 is arranged on one side of the washing liquid storage tank 3, after the water is mixed with phosphoric acid which is added into the washing liquid storage tank 3 through the phosphoric acid inlet 4, the mixture is sent to the venturi scrubber 6 through the washing pump 5, ammonia in reaction tail gas pumped from the flash chamber 21 and the polymerization tank 22 by the tail gas fan 8 is washed and absorbed, and after gas-liquid separation of the primary washing tower 7, the washing liquid which absorbs the ammonia is refluxed to the washing liquid storage tank 3. The ammonia gas contained in the tail gas after the two countercurrent washing is absorbed and then is emptied, and the washing liquid is recovered into the washing liquid storage tank 3.
Specifically, the washing liquid is communicated with the secondary heat exchanger 10 through the concentrating branch 9, enters a concentrating system through the concentrating pump inlet branch 11, and is communicated with the heater 13, the concentrating tower 16 and the concentrated liquid storage tank 17 through the concentrating pump 12; urea is added into a concentrated solution storage tank 17 through a urea water inlet 18, the concentrated solution storage tank 17 is communicated with a tubular reactor 20 through a feed pump 19, one side of the upper part of a heater 13 is provided with a saturated steam inlet 14, the other side of the lower part of the heater 13 is provided with a condensate outlet 15, washing liquid is conveyed through a washing pump 5, and is sent to a secondary heat exchanger 10 through a concentration branch 9 to exchange heat with ammonium polyphosphate circulating liquid for heating; enters a concentration pump 12 through a concentration pump inlet branch pipe 11, is sent into a heater 13 together with concentrated circulating liquid through the concentration pump 12, enters a concentration tower 16 for concentration after being preheated by saturated steam, enters the heater 13 from a steam inlet 14 after saturated steam is saturated, and is discharged from a condensate outlet 15; the concentrated solution is refluxed to the concentrated solution storage tank 17, urea is added into the concentrated solution storage tank 17 through the urea water inlet 18, and is uniformly mixed with the concentrated solution, and then is sent to the tubular reactor 20 through the reaction feed pump 19.
Further, the feed liquid from the reaction feed pump 19 and the gas ammonia supplied through the ammonia supply line 37 undergo neutralization reaction in the tubular reactor 20, the foam material after the reaction is sprayed into the flash chamber 21 under the self-prepared pressure, and the foam material is further polymerized under the condition of heat preservation and heating after evaporating moisture and exhausting gases such as carbon dioxide, ammonia gas and the like, and then enters the polymerization tank 22, and the heat source is supplied by the heating system 23; the polymerized foam material overflows to a dissolving tank 24, is dissolved and absorbed by the ammonium polyphosphate solution from an absorption circulating pipeline 32, flows into a collecting tank 25, is sent to a primary heat exchanger 27 through a feed liquid pump 26, exchanges heat with liquid ammonia added through a first liquid ammonia inlet 34, is cooled, is discharged into a temporary storage tank 28, and part of liquid ammonia is added into the temporary storage tank 28 through a liquid ammonia feed port 29 to further neutralize free acid in the ammonium polyphosphate feed liquid, so that the ammonium polyphosphate saturated solution is prepared.
Further, part of the liquid ammonia enters the primary heat exchanger 27 through the first liquid ammonia inlet 34 to exchange heat with the ammonium polyphosphate absorption liquid and then enters the ammonia storage tank 36; the saturated ammonium polyphosphate solution is sent to a secondary heat exchanger 10 through a circulating pump 30, subjected to heat exchange and temperature reduction with the washing liquid from a washing liquid storage tank 3, enters a tertiary heat exchanger 31, and part of liquid ammonia enters the tertiary heat exchanger 31 through a second liquid ammonia inlet 35, is fully subjected to heat exchange with the circulating ammonium polyphosphate solution, and is converted into gas ammonia to enter an ammonia storage tank 36; the ammonium polyphosphate solution subjected to heat exchange and temperature reduction with the liquid ammonia is conveyed to the dissolving tank 24 through the circulating pipeline 32, fresh water is added into the circulating pipeline 32 through the fresh water feed port 33, and foamed ammonium polyphosphate overflowed from the polymerization tank 22 is dissolved and absorbed; the liquid ammonium polyphosphate fertilizer product is withdrawn from the product take-off 38 and sent to a product storage tank 39.
When the liquid ammonium polyphosphate fertilizer production device is used, firstly, water is continuously added into the secondary washing tower 2 through the water inlet 1, a small amount of ammonia in the tail gas is washed, then the ammonia is refluxed to the washing liquid storage tank 3, and is mixed with phosphoric acid which is continuously added into the washing liquid storage tank 3 through the phosphoric acid inlet 4, and then the mixture is sent into the Venturi scrubber 6 through the washing pump 5, so that ammonia in the polymerized tail gas is washed and absorbed;
then, the washing liquid is sent to a secondary heat exchanger 10 through a washing pump 5 and a concentration branch 9, and exchanges heat with the ammonium polyphosphate circulating liquid to raise the temperature; enters a concentration pump 12 through a concentration pump inlet branch pipe 11, is sent to a heater 13 for heating, enters a concentration tower 16 for concentration, flows into a concentrated solution storage tank 17, and is circularly concentrated or cascade concentrated to the required concentration;
urea is added into a concentrated solution storage tank 17 through a urea water inlet 18, is uniformly mixed with concentrated solution, is sent to a tubular reactor 20 through a reaction feed pump 19, is subjected to neutralization reaction with gas ammonia provided by an ammonia supply pipeline 37 in the tubular reactor 20, and after the reacted foam material enters a flash evaporation chamber 21 to evaporate moisture, enters a polymerization tank 22 to be subjected to polymerization reaction under the condition of heat preservation and heating, overflows into a dissolving tank 24, is dissolved and absorbed by ammonium polyphosphate circulating solution, flows into a collecting tank 25, is sent to a primary heat exchanger 27 through a feed liquid pump 26, is subjected to heat exchange with liquid ammonia added through a first liquid ammonia inlet 34, and flows into a temporary storage tank 28 after being cooled;
adding part of liquid ammonia into a temporary storage tank 28 through a liquid ammonia feed port 29, further neutralizing free acid in the ammonium polyphosphate feed liquid to prepare an ammonium polyphosphate saturated solution, and conveying the ammonium polyphosphate saturated solution to a secondary heat exchanger 10 and a tertiary heat exchanger 31 through a circulating pump 30, and respectively exchanging heat with washing liquid and liquid ammonia to cool;
the cooled ammonium polyphosphate solution is partially returned to the dissolution tank 24 via the absorption circulation line 32 to dissolve the absorbed ammonium polyphosphate, and partially taken out as a liquid ammonium polyphosphate fertilizer product from the product take-out port 38 to the product storage tank 39.
Finally, it should be noted that, in the embodiment, the primary heat exchanger 27, the secondary heat exchanger 10, the tertiary heat exchanger 31, and the like, the electronic components in the above components are all universal standard components or components known to those skilled in the art, the structure and principle thereof are all known by those skilled in the art through technical manuals or known through routine experiment methods, all the electrical components in the device are connected by wires at the idle position, and the specific connection means should refer to the sequential working order among the electrical components in the working principle to complete the electrical connection, which is known in the art.
The foregoing has shown and described the basic principles, principal features and advantages of the utility model. It will be understood by those skilled in the art that the present utility model is not limited to the above-described embodiments, and that the above-described embodiments and descriptions are only preferred embodiments of the present utility model, and are not intended to limit the utility model, and that various changes and modifications may be made therein without departing from the spirit and scope of the utility model as claimed. The scope of the utility model is defined by the appended claims and equivalents thereof.
Claims (8)
1. A liquid ammonium polyphosphate fertilizer apparatus for producing, its characterized in that: the device comprises a concentration system, a polymerization reaction system and a tail gas washing system, wherein the tail gas washing system comprises a primary washing tower (7), a washing liquid storage tank (3) and a washing pump (5) which are sequentially connected, a phosphoric acid inlet (4) is formed in one side of the washing liquid storage tank (3), and a liquid outlet of the washing pump (5) is respectively connected with the primary washing tower (7) and a secondary heat exchanger (10); the concentration system comprises a concentration pump (12), a heater (13), a concentration tower (16) and a concentrated solution storage tank (17) which are sequentially connected, wherein a urea feed inlet (18) is arranged on the concentrated solution storage tank (17), the concentrated solution storage tank (17) is connected with the feed inlet of the concentration pump (12), and the feed inlet of the concentration pump (12) is also connected with the secondary heat exchanger (10); the utility model provides a polymerization reaction system feed inlet is connected with concentrate storage tank (17) through tubular reactor (20), polymerization reaction system discharge gate is connected with one-level heat exchanger (27), interim storage tank (28) in proper order, interim storage tank (28) are connected with second grade heat exchanger (10) product feed inlet, the product discharge gate on second grade heat exchanger (10) is connected with product storage tank (39), one-level heat exchanger (27) feed inlet is connected with liquid ammonia providing device, one-level heat exchanger (27) export is connected with the ammonia import of tubular reactor (20), one-level scrubbing tower (7) air inlet is connected with polymerization reaction system gas vent.
2. The liquid ammonium polyphosphate fertilizer production apparatus of claim 1, wherein: and a liquid ammonia feeding port (29) is arranged on one side of the temporary storage tank (28), and the liquid ammonia feeding port (29) is connected with a liquid ammonia providing device.
3. The liquid ammonium polyphosphate fertilizer production apparatus of claim 1, wherein: an ammonia storage tank (36) is arranged between the outlet of the primary heat exchanger (27) and the ammonia inlet of the tubular reactor (20), a tertiary heat exchanger (31) is arranged between the secondary heat exchanger (10) and the product storage tank (39), the liquid inlet of the tertiary heat exchanger (31) is connected with a liquid ammonia supply device, and the air outlet of the tertiary heat exchanger (31) is connected with the ammonia storage tank (36).
4. The liquid ammonium polyphosphate fertilizer production apparatus of claim 1, wherein: the polymerization reaction system comprises a flash chamber (21) and a polymerization tank (22) which are sequentially connected, wherein an overflow port of the polymerization tank (22) is connected with a dissolving tank (24), an outlet of the dissolving tank (24) is connected with a collecting tank (25), and a discharge port of the collecting tank (25) is connected with a primary heat exchanger (27); the heat source of the polymerization tank (22) is provided by a heating system (23).
5. The liquid ammonium polyphosphate fertilizer production apparatus of claim 1, wherein: a saturated steam inlet (14) is formed in one side of the upper portion of the heater (13), and a condensate outlet (15) is formed in the other side of the lower portion of the heater (13).
6. The liquid ammonium polyphosphate fertilizer production apparatus of claim 1, wherein: the air inlet of the primary washing tower (7) is provided with a Venturi scrubber (6), and the liquid outlet of the washing pump (5) is connected with the inlet of the Venturi scrubber (6).
7. The liquid ammonium polyphosphate fertilizer production apparatus of claim 1, wherein: the air outlet of the first-stage washing tower (7) is connected with the air inlet of the second-stage washing tower (2), the air inlet of the second-stage washing tower (2) is provided with a water inlet (1), and the washing liquid outlet at the bottom of the second-stage washing tower (2) is connected with a washing liquid storage tank (3).
8. A liquid ammonium polyphosphate fertilizer apparatus for producing according to claim 3, wherein: the product discharge port of the three-stage heat exchanger (31) is also connected with the dissolution tank (24) through a circulating pipeline (32), and the circulating pipeline (32) is provided with a fresh water feed port (33).
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| CN202321500468.8U CN220034363U (en) | 2023-06-13 | 2023-06-13 | Liquid ammonium polyphosphate fertilizer apparatus for producing |
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