Production method and co-production method of monoammonium phosphate production device

Abstract

The invention discloses a production method and a co-production method of a monoammonium phosphate production device, the production device comprises a first device and a second device, and the co-production method is characterized in that the first device and the second device are partially connected, so that the effect that the two devices are simultaneously matched for production is achieved. The method provided by the invention can break through the limitation of the processing capacity of the existing production equipment. The first device and the second device can separately produce monoammonium phosphate, after the first device and the second device are linked for production, part of slurry can be introduced into the second device for drying and other links, and the pressure of the first device is relieved, so that the production load is increased, and the yield is increased. Meanwhile, indexes such as the moisture content of the monoammonium phosphate can be optimized, the moisture of the monoammonium phosphate product is further reduced and is more stable through reasonable treatment of a drying link of the second device, and the stability and consistency of the quality of the monoammonium phosphate are improved.

Description

Technical Field

[0001] This invention belongs to the field of chemical production technology, and particularly relates to the production method and co-production method of monoammonium phosphate production equipment. Background Technology

[0002] In the production of monoammonium phosphate (MAP), the production load and methods are relatively limited due to constraints imposed by the processing capacity of equipment such as heaters, three-cylinder pumps, hot blast furnaces, and dust collectors. Furthermore, the production process also suffers from problems such as high exhaust gas temperatures leading to significant energy losses, excessive steam consumption, and low thermal energy utilization. Therefore, a MAP production unit capable of being adjusted according to product requirements is needed.

[0003] Patent application CN103613083A discloses a method for producing industrial-grade monoammonium phosphate by combining wet-process phosphoric acid and high-purity phosphoric acid. The method involves neutralizing the filtrate obtained after desulfurization of phosphate rock powder and wet-process phosphoric acid with ammonia or ammonia water twice to obtain a phosphate slurry. The filtrate obtained after adjusting the pH value with high-purity phosphoric acid is then concentrated, crystallized, and dried to obtain industrial-grade monoammonium phosphate product.

[0004] Patent application CN118221083A discloses a slurry-based method for producing powdered ammonia (MAP), which effectively solves the problems of frequent blockages in the production pipes, high energy consumption, and high consumption of primary steam. By introducing the secondary steam generated during neutralization into a cooling tower for liquid ammonia evaporation, steam consumption is reduced.

[0005] However, the aforementioned patent applications all pertain to the production of monoammonium phosphate using a single device, and do not address the technical challenge of producing monoammonium phosphate through a combination of multiple devices. Summary of the Invention

[0006] To solve the above-mentioned technical problems, the present invention provides a production method and co-production method for a monoammonium phosphate production apparatus.

[0007] The present invention is achieved through the following technical solutions.

[0008] The production method of the monoammonium phosphate production apparatus provided by the present invention includes the process of producing monoammonium phosphate by using a first apparatus and a second apparatus respectively.

[0009] Preferably, the method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: Phosphoric acid is fed into the acid mixing tank and then into the neutralization tank via a transfer pump; A2: After being vaporized in the first ammonia evaporator, the liquid ammonia is fed into the neutralization tank at 0.60 MPa via the first buffer tank; A3: Phosphoric acid and ammonia gas react in a neutralization tank to produce slurry A, which is then sent to a gas-liquid separator for separation. A4: After slurry A is fed into the first heater, the second heater and the third heater in sequence through the feed pipe, slurry A is heated, evaporated and concentrated to obtain slurry B; A5. After being pressurized by the first and third cylinder pumps and the second and third cylinder pumps, the slurry B is sprayed into the first drying tower and the second drying tower respectively, and dried to obtain powdered monoammonium phosphate.

[0010] Preferably, the method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: Phosphoric acid with a concentration of 20-30% is fed into the acid mixing tank and then into the neutralization tank by a transfer pump at a rate of 5-9 m³ / h. A2: Liquid ammonia with a concentration of 70-90% is sent to the ammonia evaporator for vaporization, and then fed into the neutralization tank at 0.1-0.9 MPa via a buffer tank; A3: Phosphoric acid and gaseous ammonia react in a neutralization tank, with the degree of neutralization controlled at 0.98-1.03 and the pH value controlled at 4-4.6, to generate slurry A, which is then sent to a gas-liquid separator for separation. A4: After slurry A is fed into the first heater, the second heater and the third heater in sequence through the feed pipe, slurry A is heated, evaporated and concentrated to obtain slurry B; A5. After being pressurized by the first three-cylinder pump and the second three-cylinder pump, the slurry B is sprayed into the first drying tower at a temperature of 120-130℃ and the second drying tower at a temperature of 120-130℃ respectively, and dried for 5-10 minutes to obtain powdered monoammonium phosphate.

[0011] Preferably, in step A4, slurry A is heated, evaporated, and concentrated to obtain slurry B with a specific gravity of 1-2 g / cm³ and a pH value of 4-4.6.

[0012] Preferably, the method for producing monoammonium phosphate using the second apparatus includes the following steps: B1. Transfer the phosphoric acid from the storage tank into the tubular reactor; B2. Liquid ammonia with a concentration of 70-90% is sent to the second ammonia evaporator for vaporization, and then sent to the S1 tubular reactor via the second buffer tank; B3. Liquid ammonia and phosphoric acid undergo a neutralization reaction in a tubular reactor to obtain slurry C; B4. The slurry C in the tubular reactor is sprayed into the drying tower and flash-dried in a countercurrent manner with the cold air from the bottom of the drying tower. Powder A is obtained at the bottom of the drying tower, and after screening and crushing, powdered monoammonium phosphate is obtained.

[0013] Preferably, the method for producing monoammonium phosphate using the second apparatus includes the following steps: B1. Phosphoric acid with a P2O5 concentration of 44.5-47% in the storage tank is fed into the tubular reactor; B2. Liquid ammonia with a concentration of 70-90% is sent to the second ammonia evaporator for vaporization, and then sent to the S1 tubular reactor at 0.96MPa via the second buffer tank. B3. Liquid ammonia and phosphoric acid are neutralized in a tubular reactor at a temperature of 120-140℃ for 1-4 seconds, with the degree of neutralization controlled between 1 and 1.1 and the pH controlled between 4.5 and 5, to obtain slurry C with a water content of 20-30%. B4. The slurry C in the tubular reactor is sprayed into the drying tower and flash-dried in a countercurrent manner with the cold air from the bottom of the drying tower. It is dried at 50-70℃ for 5-10 minutes, and powder A is obtained at the bottom of the drying tower. After screening and crushing, powdered monoammonium phosphate is obtained.

[0014] Preferably, in step B4, the specific gravity of the sprayed slurry is controlled to be 1.3-1.8 g / mL.

[0015] A co-production method for a monoammonium phosphate (MAP) production unit includes a first co-production method and a second co-production method. The first co-production method includes connecting a first heater of the first unit to a drying tower of the second unit for MAP production. The second co-production method includes connecting a tubular reactor of the second unit to the first heater of the first unit for MAP production.

[0016] Preferably, the first co-production method includes the following steps: C1: Add 20-30% dilute acid to the acid mixing tank, and then pump it into the neutralization tank at a rate of 6-9 m³ / h. C2: Liquid ammonia with a concentration of 70-90% is fed into the first ammonia evaporator for vaporization, and then fed into the neutralization tank at 0.6-1 MPa via the first buffer tank. Phosphoric acid and gaseous ammonia react in the neutralization tank, with the degree of neutralization controlled at 1.05-1.12 and the pH value controlled at 4.5-5, to generate slurry D. C3: Slurry D is separated in the gas-liquid separator and then enters the first heater, where it is heated at 110-120℃ for 5-10 minutes; C4: The slurry D after treatment by the first heater is fed into the static mixer at a flow rate of 1-2 m³ / h and fully mixed with the slurry C produced by the cross-tube reactor of the second device. The resulting mixed slurry E is sent to the drying soft tower and subjected to countercurrent flash drying with cold air from the bottom of the drying soft tower. It is dried at 50-60℃ for 5-10 min, and powder A is obtained at the bottom of the drying soft tower. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0017] Preferably, the second co-production method includes the following steps: D1: Phosphoric acid with a P2O5 concentration of 44.5-47% is fed into a tubular reactor; D2: Liquid ammonia with a concentration of 70-90% is sent to the second ammonia evaporator for vaporization, and then sent to the tubular reactor at 0.7-1 MPa through the second buffer tank; D3: Phosphoric acid and liquid ammonia undergo a neutralization reaction in a tubular reactor, with the degree of neutralization controlled between 0.95 and 1.0, and the pH controlled between 4.2 and 4.5, yielding a slurry F with a water content of 22-28%. D4: After the slurry F is fed from the tubular reactor into the first heater, the second heater and the third heater, the slurry F is heated, evaporated and concentrated to obtain slurry G; D5. After being pressurized by the first and third cylinder pumps and the second and third cylinder pumps, the slurry G is sprayed into the first drying tower at a temperature of 70-90℃ and the second drying tower at a temperature of 70-90℃ respectively, and dried for 5-15 minutes to obtain powdered monoammonium phosphate.

[0018] The beneficial effects of this invention are as follows: The method of this invention overcomes the limitations of existing production equipment processing capacity. The first and second devices can produce monoammonium phosphate independently. When they are used in coordinated production, a portion of the slurry can be introduced into the drying process of the second device, relieving pressure on the first device and thus increasing production load and output. Simultaneously, it optimizes indicators such as the moisture content of the monoammonium phosphate. Through proper processing in the drying process of the second device, the moisture content of the monoammonium phosphate product is further reduced and stabilized, improving the stability and consistency of monoammonium phosphate quality.

[0019] Furthermore, this linkage model can optimize energy utilization and resource allocation. The energy consumption and resource utilization of the first and second units differ at different stages. Linkage allows for better recovery and reuse of waste heat and other energy sources, reducing overall energy consumption, maximizing resource utilization, lowering production costs, and enhancing the company's economic efficiency and market competitiveness. Attached Figure Description

[0020] Figure 1 This is a schematic diagram of the structure of the first device of the present invention; Figure 2 This is a schematic diagram of the structure of the second device of the present invention; Figure 3 This is a schematic diagram of the production apparatus of the first co-production method of the present invention; Figure 4 This is a schematic diagram of the production apparatus of the second co-production method of the present invention; In the diagram: 1-Acid mixing tank, 2-Ammonia evaporator, 3-Buffer tank, 4-Neutralization tank, 5-Gas-liquid separator, 6-First heater, 7-Second heater, 8-Third heater, 9-First three-cylinder pump, 10-Second three-cylinder pump, 11-First drying tower, 12-Second drying tower, 13-Storage tank, 14-Second ammonia evaporator, 15-Second buffer tank, 16-Tube reactor, 17-Drying soft tower. Detailed Implementation

[0021] The technical solution of the present invention is further described below, but the scope of protection is not limited to what is described.

[0022] Example 1: like Figure 1 As shown, a method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: 30% phosphoric acid is fed into acid mixing tank 1 and then into neutralization tank 4 by a transfer pump at a rate of 9 m³ / h. A2: Liquid ammonia with a concentration of 90% is sent into ammonia evaporator 2 for vaporization, and then fed into neutralization tank 4 through buffer tank 3 at 0.9MPa; A3: Phosphoric acid and gaseous ammonia react in neutralization tank 4, with the degree of neutralization controlled at 0.98-1.03 and the pH value controlled at 4.6, generating dilute neutralized monoammonium slurry A at the MAP boiling point. Slurry A is then sent to gas-liquid separator 5 for separation. A4: After slurry A is fed into the first heater 6, the second heater 7 and the third heater 8 in sequence through the feed pipe, slurry A is heated, evaporated and concentrated to obtain slurry B with a specific gravity of 2g / cm³ and a pH value of 4.6, which has reached the endpoint concentration. A5. After being pressurized by the first three-cylinder pump 9 and the second three-cylinder pump 10, the slurry B is sprayed into the first drying tower 11 and the second drying tower 12 at a temperature of 130℃ respectively, and dried for 10 minutes to obtain powdered monoammonium phosphate.

[0023] Example 2: like Figure 1 As shown, a method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: 20% phosphoric acid is fed into acid mixing tank 1 and then into neutralization tank 4 by a transfer pump at a rate of 5 m³ / h. A2: Liquid ammonia with a concentration of 70% is sent to ammonia evaporator 2 for vaporization, and then fed into neutralization tank 4 at 0.1 MPa via buffer tank 3; A3: Phosphoric acid and gaseous ammonia react in neutralization tank 4, with the degree of neutralization controlled at 0.98-1.03 and the pH value controlled at 4, to generate dilute neutralized monoammonium slurry A at the MAP boiling point. Slurry A is then sent to gas-liquid separator 5 for separation. A4: After slurry A is fed into the first heater 6, the second heater 7 and the third heater 8 in sequence through the feed pipe, slurry A is heated, evaporated and concentrated to obtain slurry B with a specific gravity of 1g / cm³ and a pH value of 4, which has reached the endpoint concentration. A5. After being pressurized by the first three-cylinder pump 9 and the second three-cylinder pump 10, the slurry B is sprayed into the first drying tower 11 and the second drying tower 12 at a temperature of 120℃, respectively, and dried for 5 minutes to obtain powdered monoammonium phosphate.

[0024] Example 3: like Figure 1 As shown, a method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: 25% phosphoric acid is fed into acid mixing tank 1 and then into neutralization tank 4 by a transfer pump at a rate of 7.7 m³ / h. A2: Liquid ammonia with a concentration of 80% is sent into ammonia evaporator 2 for vaporization, and then fed into neutralization tank 4 through buffer tank 3 at 0.6MPa; A3: Phosphoric acid and gaseous ammonia react in neutralization tank 4, with the degree of neutralization controlled at 0.98-1.03 and the pH value controlled at 4.3, generating dilute neutralized monoammonium slurry A at the MAP boiling point. Slurry A is then sent to gas-liquid separator 5 for separation. A4: After slurry A is fed into the first heater 6, the second heater 7 and the third heater 8 in sequence through the feed pipe, slurry A is heated, evaporated and concentrated to obtain slurry B with a specific gravity of 1.58 g / cm³ and a pH value of 4.2, which has reached the endpoint concentration. A5. After being pressurized by the first three-cylinder pump 9 and the second three-cylinder pump 10, the slurry B is sprayed into the first drying tower 11 and the second drying tower 12 at a temperature of 125℃ respectively, and dried for 7 minutes to obtain powdered monoammonium phosphate.

[0025] Example 4: like Figure 2 As shown, a method for producing monoammonium phosphate using a second apparatus includes the following steps: B1. Phosphoric acid with a P2O5 concentration of 47% in storage tank 13 is fed into tubular reactor 16; B2. Liquid ammonia with a concentration of 90% is sent to the second ammonia evaporator 14 for vaporization, and then sent to the S1 tubular reactor 16 at 0.96 MPa via the second buffer tank 15. B3. Liquid ammonia and phosphoric acid are neutralized in tubular reactor 16 at 140℃ for 4 seconds, with the degree of neutralization controlled between 1 and 1.1 and the pH controlled at 5, to obtain slurry C with a water content of 30%. B4. The slurry C in the tubular reactor 16 is injected into the drying soft tower 17 through the tube nozzle by the pressure generated by its own reaction. The specific gravity of the slurry is controlled at 1.8 g / mL. It is then subjected to countercurrent flash drying with the cold air from the bottom of the drying soft tower 17. The drying is carried out at 70℃ for 10 min. Powder A is obtained at the bottom of the drying soft tower 17. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0026] Example 5: like Figure 2 As shown, a method for producing monoammonium phosphate using a second apparatus includes the following steps: B1. Phosphoric acid with a P2O5 concentration of 44.5% is sent from storage tank 13 into tubular reactor 16; B2. Liquid ammonia with a concentration of 70% is sent to the second ammonia evaporator 14 for vaporization, and then sent to the S1 tubular reactor 16 at 0.96 MPa via the second buffer tank 15. B3. Liquid ammonia and phosphoric acid are neutralized in tubular reactor 16 at 120°C for 1 second, with the degree of neutralization controlled between 1 and 1.1 and the pH controlled at 4.5, to obtain slurry C with a water content of 20%. B4. The slurry C in the tubular reactor 16 is injected into the drying soft tower 17 through the tube nozzle by the pressure generated by its own reaction. The specific gravity of the slurry is controlled at 1.3 g / mL. It is then subjected to countercurrent flash drying with the cold air from the bottom of the drying soft tower 17. The slurry is dried at 50°C for 5 min. Powder A is obtained at the bottom of the drying soft tower 17. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0027] Example 6: like Figure 2 As shown, a method for producing monoammonium phosphate using a second apparatus includes the following steps: B1. Phosphoric acid with a P2O5 concentration of 46% in storage tank 13 is fed into tubular reactor 16; B2. Liquid ammonia with a concentration of 80% is sent to the second ammonia evaporator 14 for vaporization, and then sent to the S1 tubular reactor 16 at 0.96 MPa via the second buffer tank 15. B3. Liquid ammonia and phosphoric acid are neutralized in tubular reactor 16 at 130°C for 2 seconds, with the degree of neutralization controlled between 1 and 1.1 and the pH controlled at 4.7, to obtain slurry C with a water content of 25%. B4. The slurry C in the tubular reactor 16 is injected into the drying soft tower 17 through the tube reverse nozzle by the pressure generated by its own reaction. The specific gravity of the slurry is controlled at 1.656 g / mL. It is then subjected to countercurrent flash drying with cold air from the bottom of the drying soft tower 17. The drying is carried out at 60℃ for 7 min. Powder A is obtained at the bottom of the drying soft tower 17. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0028] Example 7: like Figure 3 As shown, the co-production method of the monoammonium phosphate production unit includes a first co-production method, which includes the process of connecting the first heater 6 of the first unit to the drying soft tower 17 of the second unit to produce monoammonium phosphate.

[0029] The first co-production method includes the following steps: C1: 30% dilute acid is introduced into acid mixing tank 1 and then pumped into neutralization tank 4 at a rate of 9 m³ / h by a transfer pump; C2: 90% liquid ammonia is fed into the first ammonia evaporator 2 for vaporization, and then fed into the neutralization tank 4 at 1MPa via the first buffer tank 3. Phosphoric acid and gaseous ammonia react in the neutralization tank 4, with the degree of neutralization controlled at 1.05-1.12 and the pH value controlled at 5, to generate MAP dilute neutralized monoammonium slurry D at the boiling point. C3: The boiling slurry D is separated in the gas-liquid separator 5 and then enters the first heater 6, where it is heated at 120°C for 10 minutes; C4: The slurry D after treatment by the first heater 6 is fed into the static mixer 18 at a flow rate of 2 m³ / h, and is fully mixed with the slurry C produced by the cross-tube reactor 16 of the second device, which has a water content of 25% and a specific gravity of 1.656 g / cm³. The resulting mixed slurry E with a water content of 20% and a specific gravity of 1.681 g / cm³ is fed into the drying soft tower 17, where it is subjected to countercurrent flash drying with cold air from the bottom of the drying soft tower 17. The drying is carried out at 60°C for 10 min, and powder A is obtained at the bottom of the drying soft tower 17. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0030] Example 8: like Figure 3 As shown, the co-production method of the monoammonium phosphate production unit includes a first co-production method, which includes the process of connecting the first heater 6 of the first unit to the drying soft tower 17 of the second unit to produce monoammonium phosphate.

[0031] The first co-production method includes the following steps: C1: 20% dilute acid is introduced into acid mixing tank 1 and then pumped into neutralization tank 4 at a rate of 6 m³ / h by a transfer pump; C2: 70% liquid ammonia is fed into the first ammonia evaporator 2 for vaporization, and then fed into the neutralization tank 4 at 0.6 MPa via the first buffer tank 3. Phosphoric acid and gaseous ammonia react in the neutralization tank 4, with the degree of neutralization controlled at 1.05-1.12 and the pH value controlled at 4.5, generating MAP dilute neutralized monoammonium slurry D at the boiling point. C3: The boiling slurry D is separated in the gas-liquid separator 5 and then enters the first heater 6, where it is heated at 110°C for 5 minutes; C4: The slurry D after treatment by the first heater 6 is fed into the static mixer 18 at a flow rate of 1 m³ / h, and is fully mixed with the slurry C produced by the cross-tube reactor 16 of the second device, which has a water content of 25% and a specific gravity of 1.656 g / cm³. The resulting mixed slurry E with a water content of 20% and a specific gravity of 1.681 g / cm³ is fed into the drying soft tower 17, where it is subjected to countercurrent flash drying with cold air from the bottom of the drying soft tower 17. The drying is carried out at 50°C for 5 min, and powder A is obtained at the bottom of the drying soft tower 17. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0032] Example 9: like Figure 3 As shown, the co-production method of the monoammonium phosphate production unit includes a first co-production method, which includes the process of connecting the first heater 6 of the first unit to the drying soft tower 17 of the second unit to produce monoammonium phosphate.

[0033] The first co-production method includes the following steps: C1: 26% dilute acid is introduced into acid mixing tank 1 and then pumped into neutralization tank 4 at a rate of 7.7 m³ / h by a transfer pump; C2: 80% liquid ammonia is fed into the first ammonia evaporator 2 for vaporization, and then fed into the neutralization tank 4 at 0.8 MPa via the first buffer tank 3. Phosphoric acid and gaseous ammonia react in the neutralization tank 4, with the degree of neutralization controlled at 1.05-1.12 and the pH value controlled at 4.8, generating MAP dilute neutralized monoammonium slurry D at the boiling point. C3: The boiling slurry D is separated in the gas-liquid separator 5 and then enters the first heater 6, where it is heated at 115°C for 8 minutes; C4: The slurry D after treatment by the first heater 6 is fed into the static mixer 18 at a flow rate of 1.6 m³ / h, and is fully mixed with the slurry C produced by the cross-tube reactor 16 of the second device, which has a water content of 25% and a specific gravity of 1.656 g / cm³. The resulting mixed slurry E with a water content of 20% and a specific gravity of 1.681 g / cm³ is fed into the drying soft tower 17, where it is subjected to countercurrent flash drying using cold air from the bottom of the drying soft tower 17. The drying is carried out at 55°C for 9 min, and powder A is obtained at the bottom of the drying soft tower 17. After sieving and crushing, powdered monoammonium phosphate is obtained.

[0034] Example 10: like Figure 4 As shown, the co-production method of the monoammonium phosphate production unit includes a second co-production method, which includes the process of connecting the tubular reactor 16 of the second unit to the first heater 6 of the first unit to produce monoammonium phosphate.

[0035] The second co-production method includes the following steps: D1: Phosphoric acid with a P2O5 concentration of 44.5% is fed into tubular reactor 16; D2: Liquid ammonia with a concentration of 70% is sent to the second ammonia evaporator 14 for vaporization, and then sent to the tubular reactor 16 at 0.7MPa via the second buffer tank 15. D3: Phosphoric acid and liquid ammonia undergo a neutralization reaction in tubular reactor 16, with the degree of neutralization controlled between 0.95 and 1.0, and the pH controlled at 4.5, yielding a slurry F with a water content of 22-28%. D4: After the slurry F is fed from the tubular reactor 16 into the first heater 6, the second heater 7, and the third heater 8, the slurry F is heated, evaporated, and concentrated to obtain a slurry G with a specific gravity of 1-2 g / cm³ and a pH value of 4-4.6 that has reached the endpoint concentration. D5. After being pressurized by the first three-cylinder pump 9 and the second three-cylinder pump 10, the slurry G is sprayed into the first drying tower 11 at a temperature of 90℃ and the second drying tower 12 at a temperature of 90℃ respectively, and dried for 15 minutes to obtain powdered monoammonium phosphate.

[0036] Example 11: like Figure 4 As shown, the co-production method of the monoammonium phosphate production unit includes a second co-production method, which includes the process of connecting the tubular reactor 16 of the second unit to the first heater 6 of the first unit to produce monoammonium phosphate.

[0037] The second co-production method includes the following steps: D1: Phosphoric acid with a P2O5 concentration of 47% is fed into tubular reactor 16. D2: Liquid ammonia with a concentration of 90% is sent to the second ammonia evaporator 14 for vaporization, and then sent to the tubular reactor 16 at 1MPa via the second buffer tank 15. D3: Phosphoric acid and liquid ammonia undergo a neutralization reaction in tubular reactor 16, with the degree of neutralization controlled between 0.95 and 1.0, and the pH controlled at 4.2, yielding a slurry F with a water content of 28%. D4: After the slurry F is fed from the tubular reactor 16 into the first heater 6, the second heater 7, and the third heater 8, the slurry F is heated, evaporated, and concentrated to obtain a slurry G with a specific gravity of 2 g / cm³ and a pH value of 4.6 that has reached the endpoint concentration. D5. After being pressurized by the first three-cylinder pump 9 and the second three-cylinder pump 10, the slurry G is sprayed into the first drying tower 11 at a temperature of 70℃ and the second drying tower 12 at a temperature of 70℃, respectively, and dried for 5 minutes to obtain powdered monoammonium phosphate.

[0038] Example 12: like Figure 4 As shown, the co-production method of the monoammonium phosphate production unit includes a second co-production method, which includes the process of connecting the tubular reactor 16 of the second unit to the first heater 6 of the first unit to produce monoammonium phosphate.

[0039] The second co-production method includes the following steps: D1: Phosphoric acid with a P2O5 concentration of 45% is fed into tubular reactor 16. D2: Liquid ammonia with a concentration of 80% is sent to the second ammonia evaporator 14 for vaporization, and then sent to the tubular reactor 16 at 0.98 MPa via the second buffer tank 15. D3: Phosphoric acid and liquid ammonia undergo a neutralization reaction in tubular reactor 16, with the degree of neutralization controlled between 0.95 and 1.0, and the pH controlled at 4.3, yielding a slurry F with a water content of 25%. D4: After the slurry F is fed from the tubular reactor 16 into the first heater 6, the second heater 7 and the third heater 8, the slurry F is heated, evaporated and concentrated to obtain slurry G with a specific gravity of 1 g / cm³ and a pH value of 4, which has reached the endpoint concentration. D5. After being pressurized by the first three-cylinder pump 9 and the second three-cylinder pump 10, the slurry G is sprayed into the first drying tower 11 at a temperature of 80℃ and the second drying tower 12 at a temperature of 80℃ respectively, and dried for 10 minutes to obtain powdered monoammonium phosphate.

[0040] Among them, the first heater 6 and the second heater 7 are II-effect heaters, and the third heater 8 is a I-effect heater.

[0041] 1000 kg of 55-60% monoammonium phosphate was prepared using the methods described in Examples 1-12. The preparation details are shown in the table below.

[0042] As shown in the table above, the percentage of water-soluble phosphorus in monoammonium phosphate (MAP) prepared using the first and second devices is above 93.1%, while the percentage increases to above 96.8% using the first and second co-production methods. Furthermore, because the slurry introduced during the first co-production method has a lower moisture content, the fuel supply to the hot blast furnace can be automatically reduced, lowering the exhaust gas temperature to 95°C and achieving energy savings. Similarly, because the slurry introduced during the second co-production method has an even lower moisture content, the evaporation load decreases, reducing steam consumption and improving thermal energy utilization.

Claims

1. A production method for a monoammonium phosphate production apparatus, characterized in that: This includes the process of producing monoammonium phosphate by using a first unit and a second unit, respectively.

2. The production method of the monoammonium phosphate production apparatus as described in claim 1, characterized in that: The method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: Phosphoric acid is fed into the acid mixing tank (1) and then into the neutralization tank (4) by a transfer pump. A2: After the liquid ammonia is vaporized in the first ammonia evaporator (2), it is fed into the neutralization tank (4) at 0.60 MPa through the first buffer tank (3); A3: Phosphoric acid and ammonia gas react in a neutralization tank (4) to generate slurry A, which is then sent to a gas-liquid separator (5) for separation. A4: After slurry A is fed into the first heater (6), the second heater (7), and the third heater (8) in sequence through the feed pipe, slurry A is heated, evaporated, and concentrated to obtain slurry B; A5. After the slurry B is pressurized by the first three-cylinder pump (9) and the second three-cylinder pump (10), it is sprayed into the first drying tower (11) and the second drying tower (12) respectively, and dried to obtain powdered monoammonium phosphate.

3. The production method of the monoammonium phosphate production apparatus as described in claim 2, characterized in that: The method for producing monoammonium phosphate using the first apparatus includes the following steps: A1: Phosphoric acid with a concentration of 20-30% is fed into the acid mixing tank (1) and then fed into the neutralization tank (4) by a transfer pump at a rate of 5-9 m³ / h. A2: A liquid ammonia with a concentration of 70-90% is sent into the ammonia evaporator (2) and vaporized. After passing through the buffer tank (3), it is fed into the neutralization tank (4) at 0.1-0.9 MPa. A3: Phosphoric acid and ammonia gaseous react in a neutralization tank (4), with the degree of neutralization controlled at 0.98-1.03 and the pH value controlled at 4-4.6, to generate slurry A, which is then sent to a gas-liquid separator (5) for separation. A4: After slurry A is fed into the first heater (6), the second heater (7), and the third heater (8) in sequence through the feed pipe, slurry A is heated, evaporated, and concentrated to obtain slurry B; A5. After the slurry B is pressurized by the first three-cylinder pump (9) and the second three-cylinder pump (10), it is sprayed into the first drying tower (11) with a temperature of 120-130℃ and the second drying tower (12) with a temperature of 120-130℃ respectively, and dried for 5-10 minutes to obtain powdered monoammonium phosphate.

4. The production method of the monoammonium phosphate production apparatus as described in claim 3, characterized in that: In step A4, slurry A is heated, evaporated, and concentrated to obtain slurry B with a specific gravity of 1-2 g / cm³ and a pH value of 4-4.

6.

5. The production method of the monoammonium phosphate production apparatus as described in claim 1, characterized in that: The method for producing monoammonium phosphate using the second apparatus includes the following steps: B1. Send the phosphoric acid in the storage tank (13) into the tubular reactor (16). B2. Liquid ammonia with a concentration of 70-90% is sent to the second ammonia evaporator (14) for vaporization and then sent to the S1 tubular reactor (16) via the second buffer tank (15). B3. Liquid ammonia and phosphoric acid are neutralized in a tubular reactor (16) to obtain slurry C; B4. The slurry C in the tubular reactor (16) is sprayed into the drying soft tower (17) and flash-dried in a countercurrent manner with the cold air from the bottom of the drying soft tower (17). Powder A is obtained at the bottom of the drying soft tower (17), and powdered monoammonium phosphate is obtained after screening and crushing.

6. The production method of the monoammonium phosphate production apparatus as described in claim 5, characterized in that: The method for producing monoammonium phosphate using the second apparatus includes the following steps: B1. Phosphoric acid with a P2O5 concentration of 44.5-47% in the storage tank (13) is sent into the tubular reactor (16). B2. Liquid ammonia with a concentration of 70-90% is sent to the second ammonia evaporator (14) for vaporization and then sent to the S1 tubular reactor (16) at 0.96MPa via the second buffer tank (15). B3. Liquid ammonia and phosphoric acid are neutralized in a tubular reactor (16) at a temperature of 120-140℃ for 1-4 seconds, with the degree of neutralization controlled between 1 and 1.1 and the pH controlled between 4.5 and 5, to obtain a slurry C with a water content of 20-30%. B4. The slurry C in the tubular reactor (16) is sprayed into the drying soft tower (17) and flash-dried in a countercurrent manner with the cold air from the bottom of the drying soft tower (17). It is dried at 50-70℃ for 5-10 minutes and powder A is obtained at the bottom of the drying soft tower (17). After screening and crushing, powdered monoammonium phosphate is obtained.

7. The production method of the monoammonium phosphate production apparatus as described in claim 6, characterized in that: In step B4, the specific gravity of the sprayed slurry is controlled to be 1.3-1.8 g / mL.

8. The co-production method of the monoammonium phosphate production unit according to any one of claims 1-7, characterized in that: The method includes a first co-production method and a second co-production method. The first co-production method includes a process of connecting the first heater (6) of the first device to the drying soft tower (17) of the second device to produce monoammonium phosphate. The second co-production method includes a process of connecting the tubular reactor (16) of the second device to the first heater (6) of the first device to produce monoammonium phosphate.

9. The co-production method of the monoammonium phosphate production unit as described in claim 8, characterized in that: The first co-production method includes the following steps: C1: 20-30% dilute acid is introduced into the acid mixing tank (1) and then pumped into the neutralization tank (4) at a rate of 6-9 m³ / h by a transfer pump. C2: Liquid ammonia with a concentration of 70-90% is sent to the first ammonia evaporator (2) and vaporized. After being sent to the first buffer tank (3) at 0.6-1MPa, it is sent to the neutralization tank (4). Phosphoric acid and gaseous ammonia react in the neutralization tank (4). The degree of neutralization is controlled at 1.05-1.12 and the pH value is controlled at 4.5-5 to generate slurry D. C3: Slurry D is separated in the gas-liquid separator (5) and then enters the first heater (6) and is heated at 110-120℃ for 5-10 minutes; C4: The slurry D after being treated by the first heater (6) is fed into the static mixer (18) at a flow rate of 1-2 m³ / h and fully mixed with the slurry C generated by the cross-tube reactor (16) of the second device. The resulting mixed slurry E is sent to the drying soft tower (17) and subjected to countercurrent flash drying with cold air from the bottom of the drying soft tower (17). The drying is carried out at 50-60℃ for 5-10 min, and powder A is obtained at the bottom of the drying soft tower (17). After sieving and crushing, powdered monoammonium phosphate is obtained.

10. The co-production method of the monoammonium phosphate production unit as described in claim 8, characterized in that: The second co-production method includes the following steps: D1: Phosphoric acid with a P2O5 concentration of 44.5-47% is fed into a tubular reactor (16). D2: Liquid ammonia with a concentration of 70-90% is sent to the second ammonia evaporator (14) for vaporization, and then sent to the tubular reactor (16) at 0.7-1MPa through the second buffer tank (15). D3: Phosphoric acid and liquid ammonia undergo a neutralization reaction in a tubular reactor (16), with the degree of neutralization controlled between 0.95 and 1.0, and the pH controlled between 4.2 and 4.5, to obtain a slurry F with a water content of 22-28%. D4: After the slurry F is fed from the tubular reactor (16) to the first heater (6), the second heater (7), and the third heater (8), the slurry F is heated, evaporated, and concentrated to obtain slurry G; D5. After the slurry G is pressurized by the first three-cylinder pump (9) and the second three-cylinder pump (10), it is sprayed into the first drying tower (11) with a temperature of 70-90℃ and the second drying tower (12) with a temperature of 70-90℃ respectively, and dried for 5-15 minutes to obtain powdered monoammonium phosphate.

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