CN112225380B - Resource intensive phosphorus-containing wastewater treatment method - Google Patents
Resource intensive phosphorus-containing wastewater treatment method Download PDFInfo
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- CN112225380B CN112225380B CN202011118006.0A CN202011118006A CN112225380B CN 112225380 B CN112225380 B CN 112225380B CN 202011118006 A CN202011118006 A CN 202011118006A CN 112225380 B CN112225380 B CN 112225380B
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/02—Treatment of water, waste water, or sewage by heating
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- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
Abstract
A method for treating phosphorus-containing wastewater comprises the following steps: (1) Ammonia water or ammonia gas is adopted to adjust the pH value of the raw material of the phosphorus-containing wastewater, organic phosphorus compounds in the phosphorus-containing wastewater are oxidized into orthophosphate ions, and COD in the wastewater is oxidized and removed; (2) Carrying out gas-liquid separation on the wastewater oxidized in the step (1), and introducing a part of separated oxidation liquid into an ammonia nitrogen heat stripping device to strip ammonia nitrogen; (3) And (3) introducing the liquid subjected to ammonia nitrogen stripping in the step (2) into an evaporation system, crystallizing, and separating by using solid-liquid separation equipment to obtain solid-phase ammonium phosphate. The ammonia nitrogen gas blown off in the step (2) is returned to a wastewater pretreatment link for adjusting the pH of the phosphorus-containing wastewater raw material or for post-treatment of finally recycling salt; and (4) after-treatment, the ammonium phosphate in the step (3) can be used as a catalyst for an upstream acetic anhydride cracking process for recycling. The method can avoid the adverse effect of the byproduct ammonium sulfate on the economic evaluation of the whole process.
Description
Technical Field
The invention belongs to the technical field of chemical environmental protection, and relates to a treatment process of phosphorus-containing wastewater under a strong acid condition, in particular to a treatment method of phosphorus-containing wastewater generated in a production process of preparing acetic anhydride by an acetic acid cracking method.
Background
In the process of preparing acetic anhydride by cracking acetic acid, inorganic phosphate is generally used as a catalyst, so that phosphorus-containing wastewater is generated in the high-temperature cracking production process. The phosphorus-containing wastewater is wastewater which is difficult to treat, and especially the organic phosphorus has the characteristics of high toxicity, difficult biodegradation and the like. In recent years, an advanced oxidation process used industrially is effective for the treatment of organic phosphorus, but the catalyst is somewhat intolerant to acid-containing wastewater with a low pH, so it is common practice to maintain the catalytic effect by adjusting the pH to about 6 by adding NaOH before the wastewater enters the catalytic tower. The wastewater is subjected to catalytic oxidation, ammonia nitrogen stripping, evaporative crystallization, and separation of sodium hydrogen phosphate, so as to realize resource utilization of phosphorus from conversion of organic phosphorus into inorganic phosphate, please refer to fig. 1. For example, the final product of patent CN103864040B, a process for preparing disodium hydrogen phosphate from glyphosate mother liquor, and patent CN104098074A, a process for preparing disodium hydrogen phosphate from N, N' -phosphonomethyl iminodiacetic acid wastewater is disodium hydrogen phosphate. Patent CN102616914B, a method for treating phosphorus-containing waste in pesticide production and a product obtained by the method, converts phosphorus-containing pesticide production waste liquid into substances such as pyrophosphate, polyphosphate, metaphosphate, orthophosphate and the like. The final products of patent CN104118854A, a method for producing tripolyphosphate and hexametaphosphate products from by-product pyrophosphate, are tripolyphosphate and hexametaphosphate.
The ammonia nitrogen which is usually blown off is absorbed by dilute sulphuric acid solution, and finally ammonium sulphate salt by-products are formed. The economic value of ammonium sulfate is influenced by the product components and the market supply and demand relationship, and has larger uncertainty.
Disclosure of Invention
In order to fully realize the circular economy and avoid waste, the invention aims to provide a resource-intensive phosphorus-containing wastewater treatment process, which overcomes the defects in the prior art.
In order to achieve the purpose of the invention, the invention adopts the following solution:
a method for treating phosphorus-containing wastewater comprises the following steps:
(1) Ammonia water or ammonia gas is adopted to adjust the pH value of the raw material of the phosphorus-containing wastewater, then the raw material enters a catalytic system, organic phosphorus compounds in the phosphorus-containing wastewater are oxidized into orthophosphate ions, and COD in the wastewater is oxidized and removed;
(2) Gas-liquid separation is realized on the wastewater oxidized in the step (1), and the oxidized liquid is completely returned to a catalytic system for re-catalysis so as to improve the reaction efficiency; or, introducing the separated partial oxidation liquid into an ammonia nitrogen hot stripping device to strip ammonia nitrogen;
(3) The liquid after ammonia nitrogen stripping in the step (2) enters an evaporation system for further concentration; and (4) the concentrated solution which is evaporated and exceeds the saturation concentration of ammonium phosphate enters a crystallization device, and after crystallization, solid-liquid separation equipment is used for separating to obtain solid-phase ammonium phosphate.
Further, optionally, the ammonia nitrogen gas blown off in the step (2) is returned to the wastewater pretreatment link for adjusting the pH value of the phosphorus-containing wastewater raw material.
Optionally, the ammonia nitrogen gas blown off in the step (2) is used for the final post-treatment for recovering salt.
Optionally, the ammonium phosphate in the step (3) can be reused as the catalyst of the upstream acetic anhydride cracking process through post-treatment.
Optionally, the liquid phase after solid-liquid separation in step (3) is returned to the evaporation system for continuous concentration, so as to fully recover salt.
Optionally, in the step (1), ammonia water or ammonia gas is used for adjusting the pH value of the phosphorus-containing wastewater raw material to 5.0-6.5.
Optionally, in the step (1), the phosphorus-containing wastewater with the adjusted pH value is preheated and then enters a catalytic reactor through a booster pump, and stays for 3-30min under the action of a catalyst at the temperature of 150-350 ℃ and the pressure of 2-20 MPa.
Optionally, in the step (2), the phosphorus-containing wastewater oxidized in the step (1) directly enters a flash tower, and at the moment, the high-temperature and high-pressure wastewater is subjected to gas-liquid separation in the flash tower.
Optionally, the gas phase separated in step (2) is used to heat the vaporization system feed; the separated liquid phase is collected to an oxidation liquid collecting tank.
Optionally, all the discharged materials of the oxidation liquid collecting tank are returned to the catalytic preheater and enter a catalytic system; alternatively, the first and second electrodes may be,
the discharge of the oxidation liquid collecting tank completely enters an ammonia nitrogen stripping device, or,
the discharge of the oxidation liquid collecting tank is divided into two parts, one part returns to the catalytic system, and the other part enters the ammonia nitrogen hot blowing device.
Optionally, in the step (2), monitoring the concentration change of organic phosphorus in the oxidation liquid, returning 0-10% of the total amount of the oxidation liquid to the catalytic system when the removal rate of the organic phosphorus reaches 90-100%, and allowing the rest of the oxidation liquid to enter an ammonia nitrogen hot blowing device to blow off ammonia nitrogen therein.
Optionally, the ammonium phosphate salt post-treatment method is to dissolve the ammonium phosphate salt in water, add ammonia to the ammonium phosphate salt, and then recrystallize to obtain high-purity diammonium phosphate.
Optionally, ammonia gas or ammonia water is added thereto, the pH value is adjusted to 7.9-8.1, and then recrystallization is carried out to obtain high-purity diammonium hydrogen phosphate.
Specifically, the resource-intensive phosphorus-containing wastewater treatment process provided by the invention comprises two process routes, wherein the two process routes can be used respectively or simultaneously.
For clarity, the two process routes are separately described below.
A process route which separately introduces the invention comprises the following steps:
(1) Ammonia water or ammonia gas is adopted to adjust the pH value of the raw material of the phosphorus-containing wastewater to 5.0-6.5, then the raw material enters a catalytic system, the raw material enters a catalytic reactor through a booster pump after being preheated, the raw material stays for 3-30min under the action of a catalyst at the temperature of 150-350 ℃ and the pressure of 2-20MPa, an organic phosphorus compound in the phosphorus-containing wastewater is oxidized into orthophosphate ions, and COD in the wastewater is simultaneously oxidized and greatly removed;
(2) And (2) directly feeding the wastewater oxidized in the step (1) into a flash tower, and performing gas-liquid separation on the high-temperature and high-pressure wastewater in the flash tower. The separated gas phase is used for heating the feeding material of the evaporation system; the separated liquid phase is collected to an oxidation liquid collecting tank. The discharge of the oxidation liquid collecting tank can completely return to the catalytic preheater and enter a catalytic system, or can completely enter an ammonia nitrogen stripping device, or is divided into two parts, one part returns to the catalytic system, and the other part enters the ammonia nitrogen hot stripping device. At the beginning, the oxidizing liquid is completely returned to the catalytic system for re-catalysis so as to improve the reaction efficiency. Monitoring the concentration change of organic phosphorus in the oxidizing solution, when the removal rate of the organic phosphorus reaches 90-100%, returning 0-10% of the total amount of the oxidizing solution to a catalytic system, and feeding the rest part of the oxidizing solution to an ammonia nitrogen hot-blowing device to blow off ammonia nitrogen in the oxidizing solution, wherein the ammonia nitrogen gas blown off returns to the wastewater pretreatment step to be used for adjusting the pH value of the wastewater, and simultaneously, the consumption of ammonia water or ammonia gas consumed for adjusting the pH value of the raw material can be reduced;
(3) The liquid after ammonia nitrogen blowing-off in the step (2) enters an evaporation system for further concentration; and (3) the concentrated solution which is evaporated and exceeds the saturation concentration of ammonium phosphate enters a crystallization device, after crystallization, solid-liquid separation equipment is used for separating to obtain solid-phase ammonium phosphate, and the ammonium phosphate can be reused as a catalyst of the upstream acetic anhydride cracking process through post-treatment. And returning the liquid phase after solid-liquid separation to an evaporation system for continuous concentration so as to fully recover salt.
The main steps of the other process route of the invention are basically the same as those of the first process route, and the main difference is that in the step (2), the ammonia nitrogen gas blown off is used for the post-treatment of finally recovering salt, so that the consumption of ammonia water or ammonia gas required by the post-treatment can be reduced.
The catalytic system comprises a preheater, a fixed bed catalytic reactor, an oxidant supply device and a matched high-pressure pump.
The catalyst in the fixed bed catalytic reactor is one of ruthenium catalyst, rhodium catalyst or ruthenium-rhodium mixed catalyst, and has high catalytic activity on organic phosphorus.
The oxidant is one of oxygen, ozone or hydrogen peroxide.
The evaporation system comprises a preheater, an evaporator, a gas-liquid separator and a matched delivery pump. One of single-effect, multi-effect evaporation and MVR evaporation processes is adopted.
The solid-phase ammonium phosphate obtained by the solid-liquid separation is ammonium dihydrogen phosphate, diammonium hydrogen phosphate and the like.
The operations of evaporation, crystallization, solid-liquid separation and recrystallization can be realized by adopting known and conventional technologies, and are not described in detail.
By adopting the technical scheme, the ammonia nitrogen blown off in the process is reasonably utilized, and on one hand, the ammonia nitrogen can be used for adjusting the pH of the raw material, so that Na ions are prevented from being introduced, and the salt obtained by final evaporative crystallization can be ensured to be an inorganic ammonium phosphate mixture; on the other hand, it can be used for the final post-treatment of the recovered salt, so that the ammonium phosphate salt mixture is completely converted into diammonium phosphate. Meanwhile, after the blown-off ammonia nitrogen is absorbed in the original process, the byproduct ammonium sulfate can be avoided, and the adverse effect possibly caused by the economic evaluation of the whole process can be further avoided.
Drawings
FIG. 1 is a schematic diagram of a conventional catalytic oxidation process for phosphorus-containing wastewater.
FIG. 2 is a schematic view of the resource-intensive phosphorus-containing wastewater treatment process and system of the present invention.
The labels in the figure are: 21-wastewater pretreatment; 22-catalytic oxidation; 23-collecting an oxidation liquid; 24-ammonia nitrogen hot stripping; 25-evaporating; 26-crystallization; 27-solid-liquid separation; 28-ammonia nitrogen absorption; 29-steam condensation;
1-wastewater pretreatment; 2-preheating catalytic feeding; 3, a booster pump; 4-collecting the oxidation liquid; 5-a catalytic reactor; 6-a flash column; 7-ammonia nitrogen hot stripping; 8-preheating of evaporation feed; 9-an evaporation device; 10-a steam condenser; 11-crystallization; 12-solid-liquid separation; 13-post-treatment.
Detailed Description
The invention is further described with reference to the following figures and examples.
Example one
1000kg of phosphorus-containing wastewater generated in the production process of preparing acetic anhydride by an acetic acid cracking method is treated, and the initial pH value is about 2.5. The total phosphorus content is about 60000ppm, with 45% organic phosphorus. In the wastewater pretreatment tank, ammonia water is added to adjust the pH value to 5.6, and then the ammonia water is pumped to a catalytic system. In the catalytic system, the wastewater is heated by a preheater to 240 ℃, then enters a fixed bed catalytic reactor through a booster pump, the pressure of the fixed bed catalytic reactor is 10Mpa, hydrogen peroxide is used as an oxidant, and the retention time of the wastewater is about 3min. And the oxidized wastewater enters a flash tower, a part of water is removed in the flash tower, and the slightly concentrated wastewater enters an oxidizing liquid collecting tank. When the concentration of the organic phosphorus is monitored to be reduced to 4.5 percent of the initial feeding quality, 6 percent of the total amount of the oxidizing solution flows back to the catalytic system, and the rest part enters the ammonia nitrogen hot blowing device. And returning the ammonia nitrogen gas blown off to a wastewater preprocessor for adjusting the pH value. And the oxidation liquid after ammonia nitrogen stripping enters a four-effect evaporation system, is further concentrated and then enters a crystallization device. And (3) performing solid-liquid separation after crystallization, wherein the solid phase is a mixture of diammonium hydrogen phosphate and ammonium dihydrogen phosphate, and the solid phase is about 125kg after dehydration, wherein the ammonium dihydrogen phosphate accounts for 91 percent of the mass ratio. And dissolving the ammonium phosphate solid in deionized water, adding ammonia water to adjust the pH value to 8.0, and recrystallizing to obtain diammonium hydrogen phosphate with the purity of 98.5%, wherein the diammonium hydrogen phosphate can be used as a catalyst for an acetic acid cracking process. And pumping the liquid phase after solid-liquid separation into an evaporation system for continuous concentration, and fully recovering salt.
Example two
The initial pH value of the phosphorus-containing wastewater generated in the production process of preparing acetic anhydride by using an acetic acid cracking method is about 2.8. The total phosphorus is about 80000ppm, with organic phosphorus 40% by weight. In the wastewater pretreatment tank, ammonia gas is directly introduced to adjust the pH value to 6.5, and then the ammonia gas is conveyed to a catalytic system by a pump. In the catalytic system, the wastewater is heated by a preheater to 350 ℃, then enters a fixed bed catalytic reactor through a booster pump, the pressure of the fixed bed catalytic reactor is 2Mpa, ozone is used as an oxidant, and the retention time of the wastewater is about 15min. And (3) removing a part of moisture in the oxidized wastewater flash tower, and feeding the slightly concentrated wastewater into an oxidizing liquid collecting tank. When the concentration of the organic phosphorus is monitored to be reduced to 2.5 percent of the initial feeding quality, 3 percent of the total amount of the oxidizing solution flows back to the catalytic system, and the rest part enters an ammonia nitrogen hot blowing device. And the oxidation liquid after ammonia nitrogen stripping enters an MVR evaporation system, is further concentrated and then enters a crystallization device. And performing solid-liquid separation after crystallization, wherein the solid phase is a mixture of diammonium hydrogen phosphate and ammonium dihydrogen phosphate, and the solid phase is about 65kg after dehydration, wherein the ammonium dihydrogen phosphate accounts for 95 percent of the mass ratio. Dissolving ammonium phosphate salt solid in deionized water, introducing blown ammonia nitrogen gas to adjust the pH value to 7.9, and recrystallizing to obtain diammonium phosphate with the purity of more than 99%, wherein the diammonium phosphate can be used as a catalyst for an acetic acid cracking process. And pumping the liquid phase after solid-liquid separation into an evaporation system for continuous concentration, and fully recovering salt.
EXAMPLE III
Treating phosphorus-containing wastewater generated in the production process of preparing acetic anhydride by an acetic acid cracking method with the initial pH value of about 2.3. The total phosphorus is about 70000ppm, and the organic phosphorus accounts for 50 percent. In the wastewater pretreatment tank, ammonia gas is directly introduced to adjust the pH value to 5.2, and then the ammonia gas is conveyed to a catalytic system by a pump. In the catalytic system, the waste water is heated by a preheater and preheated to 180 ℃ to enter a fixed bed catalytic reactor, the pressure of the fixed bed catalytic reactor is 20Mpa, oxygen is used as an oxidant, and the retention time of the waste water is about 30min. And the oxidized wastewater enters a flash tower, a part of water is removed in the flash tower, and the slightly concentrated wastewater enters an oxidizing liquid collecting tank. When the concentration of the organic phosphorus is monitored to be reduced to 5% of the initial feeding quality, 10% of the total amount of the oxidizing solution flows back to the catalytic system, and the rest part of the oxidizing solution enters an ammonia nitrogen hot blowing device. And the oxidized liquid after ammonia nitrogen stripping enters a triple-effect evaporation system, is further concentrated and then enters a crystallization device. And (3) performing solid-liquid separation after crystallization, wherein the solid phase is a mixture of diammonium hydrogen phosphate and ammonium dihydrogen phosphate, and the solid phase is about 110kg after dehydration, wherein the mass ratio of the ammonium dihydrogen phosphate is 96%. The ammonia nitrogen gas blown off is divided into two parts, and one part is returned to the wastewater preprocessor to be used for adjusting the pH value of the wastewater. And dissolving ammonium phosphate salt solid in deionized water, introducing the other part of blown ammonia nitrogen gas for post-treatment, adjusting the pH value to 8.1, recrystallizing to obtain diammonium phosphate with the purity of over 99.5 percent, and using the diammonium phosphate as a catalyst for an acetic acid cracking process. And pumping the liquid phase after solid-liquid separation into an evaporation system for continuous concentration, and fully recovering salt.
Example four
750kg of phosphorus-containing wastewater generated in the production process of preparing acetic anhydride by an acetic acid cracking method is treated, and the initial pH value is about 3. The total phosphorus content is about 50000ppm, and the organic phosphorus content is 55%. In the wastewater pretreatment tank, ammonia gas is directly introduced to adjust the pH value to 6.0, and then the ammonia gas is conveyed to a catalytic system by a pump. In the catalytic system, the waste water is heated by a preheater and preheated to 150 ℃ to enter a fixed bed catalytic reactor, the pressure of the fixed bed catalytic reactor is 15Mpa, oxygen is used as an oxidant, and the retention time of the waste water is about 22min. And the oxidized wastewater enters a flash tower, a part of water is removed in the flash tower, and the slightly concentrated wastewater enters an oxidizing liquid collecting tank. When the concentration of the organic phosphorus is monitored to be reduced to 5% of the initial feeding quality, 5% of the total amount of the oxidizing solution flows back to the catalytic system, and the rest part of the oxidizing solution enters an ammonia nitrogen hot blowing device. And the oxidized liquid after ammonia nitrogen stripping enters a triple-effect evaporation system, is further concentrated and then enters a crystallization device. And (3) performing solid-liquid separation after crystallization, wherein the solid phase is a mixture of diammonium hydrogen phosphate and ammonium dihydrogen phosphate, and the solid phase is about 85kg after dehydration, wherein the ammonium dihydrogen phosphate accounts for 96 percent of the mass ratio. The ammonia nitrogen gas blown off is divided into two parts, and one part is returned to the wastewater preprocessor to be used for adjusting the pH value of the wastewater. And dissolving ammonium phosphate salt solid in deionized water, introducing the other part of blown ammonia nitrogen gas for post-treatment, adjusting the pH value to 7.9, recrystallizing to obtain diammonium hydrogen phosphate with the purity of more than 99.5%, and using the diammonium hydrogen phosphate as a catalyst for an acetic acid cracking process. And pumping the liquid phase after solid-liquid separation into an evaporation system for continuous concentration, and fully recovering salt.
The foregoing description and description of the embodiments are provided to facilitate the understanding and appreciation of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications can be made to these teachings and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above description and the description of the embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.
Claims (11)
1. The method for treating the phosphorus-containing wastewater is characterized by comprising the following steps of:
(1) Ammonia water or ammonia gas is adopted to adjust the pH value of the raw material of the phosphorus-containing wastewater, then the raw material enters a catalytic system, organic phosphorus compounds in the phosphorus-containing wastewater are oxidized into orthophosphate ions, and COD in the wastewater is oxidized and removed;
(2) Gas-liquid separation is realized on the wastewater oxidized in the step (1), and the oxidized liquid is completely returned to a catalytic system for re-catalysis so as to improve the reaction efficiency; or, the separated partial oxidation liquid enters an ammonia nitrogen heat stripping device to strip ammonia nitrogen;
(3) The liquid after ammonia nitrogen blowing-off in the step (2) enters an evaporation system for further concentration; after evaporation, the concentrated solution exceeding the saturated concentration of ammonium phosphate enters a crystallization device, and after crystallization, solid-liquid separation equipment is used for separation to obtain solid-phase ammonium phosphate;
in the step (1), ammonia water or ammonia gas is adopted to adjust the pH value of the raw material of the phosphorus-containing wastewater to 5.0-6.5;
in the step (1), the phosphorus-containing wastewater with the adjusted pH value is preheated and then enters a catalytic reactor through a booster pump, and stays for more than 3min and less than 30min under the action of a catalyst at the temperature of 150-350 ℃ and under the pressure of 2-20 MPa.
2. The method for treating phosphorus-containing wastewater according to claim 1, wherein:
and (3) returning the ammonia nitrogen gas blown off in the step (2) to a wastewater pretreatment link for adjusting the pH value of the phosphorus-containing wastewater raw material.
3. The method for treating phosphorus-containing wastewater according to claim 1, wherein:
and (3) the ammonia nitrogen gas blown off in the step (2) is used for final post-treatment for recovering salt.
4. The method for treating phosphorus-containing wastewater according to claim 1, wherein:
and (4) after-treatment of the ammonium phosphate in the step (3), the ammonium phosphate can be reused as a catalyst of an upstream acetic anhydride cracking process.
5. The method for treating phosphorus-containing wastewater according to claim 1, wherein:
and (4) returning the liquid phase subjected to solid-liquid separation in the step (3) to an evaporation system for continuous concentration so as to fully recover salt.
6. The method for treating phosphorus-containing wastewater according to claim 1, wherein:
in the step (2), the phosphorus-containing wastewater oxidized in the step (1) directly enters a flash tower, and the high-temperature and high-pressure wastewater is subjected to gas-liquid separation in the flash tower.
7. The method for treating phosphorus-containing wastewater according to claim 1, wherein:
the gas phase separated in the step (2) is used for heating the feeding material of the evaporation system; the separated liquid phase is collected to an oxidation liquid collecting tank.
8. The phosphorus-containing wastewater treatment method according to claim 7, characterized in that:
all discharged materials of the oxidizing solution collecting tank return to the catalytic preheater and enter a catalytic system; alternatively, the first and second electrodes may be,
the discharged material of the oxidation liquid collecting tank completely enters an ammonia nitrogen stripping device, or,
the discharge of the oxidation liquid collecting tank is divided into two parts, one part returns to the catalytic system, and the other part enters the ammonia nitrogen hot blowing device.
9. The phosphorus-containing wastewater treatment method according to claim 7, characterized in that:
in the step (2), monitoring the concentration change of organic phosphorus in the oxidation liquid, returning 0-10% of the total amount of the oxidation liquid to the catalytic system when the removal rate of the organic phosphorus reaches 90-100%, and allowing the rest of the oxidation liquid to enter an ammonia nitrogen hot-blowing device to blow off the ammonia nitrogen.
10. The method for treating phosphorus-containing wastewater according to claim 4, wherein:
the ammonium phosphate salt post-treatment method comprises the steps of dissolving ammonium phosphate salt in water, adding ammonia into the water, and then recrystallizing to obtain high-purity diammonium hydrogen phosphate.
11. The method for treating phosphorus-containing wastewater according to claim 10, wherein: adding ammonia gas or ammonia water into ammonium phosphate salt solution, adjusting the pH value to 7.9-8.1, and then recrystallizing to obtain high-purity diammonium hydrogen phosphate.
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