CN110615571A - Ammonia removal method for metallurgical waste residue - Google Patents

Ammonia removal method for metallurgical waste residue Download PDF

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Publication number
CN110615571A
CN110615571A CN201910907455.4A CN201910907455A CN110615571A CN 110615571 A CN110615571 A CN 110615571A CN 201910907455 A CN201910907455 A CN 201910907455A CN 110615571 A CN110615571 A CN 110615571A
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China
Prior art keywords
slurry
ammonia
steam
rectifying tower
stage
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CN201910907455.4A
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Chinese (zh)
Inventor
孙宁磊
刘苏宁
秦丽娟
彭建华
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China ENFI Engineering Corp
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China ENFI Engineering Corp
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Priority to CN201910907455.4A priority Critical patent/CN110615571A/en
Publication of CN110615571A publication Critical patent/CN110615571A/en
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F2001/46133—Electrodes characterised by the material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes

Abstract

The invention provides an ammonia removal method for metallurgical waste residues. The ammonia removal method comprises the following steps: step S1, pulping the metallurgical waste residue to obtain pulping liquid; step S2, causticizing the slurry by lime milk to obtain the slurry containing NH3Causticizing the slurry; and step S3, performing deamination treatment on the causticized slurry by adopting steam to obtain separated ammonia-containing steam and slurry. The method utilizes the reaction of the alkaline lime milk and ammonium ions in the slurry to obtain the slurry containing NH3To causticize the slurry. The causticized slurry is further heated by steam to release ammonia from the slurry and the free ammonia is taken out by the airflow of the steam, so that the waste residue is deaminatedMeanwhile, the step of respectively treating the slag and the liquid with ammonia is omitted, and the cost is saved, so that the energy consumption for removing the ammonia from the waste slag is reduced.

Description

Ammonia removal method for metallurgical waste residue
Technical Field
The invention relates to the field of metallurgical waste residue treatment, in particular to an ammonia removal method for metallurgical waste residues.
Background
In recent years, the metallurgical industry is continuously developed, a large amount of metallurgical waste slag is generated every year in the smelting process, and a large amount of waste slag is accumulated. If the waste residues are piled up for a long time, the soluble harmful substances in the residues can be dissolved out through sunshine, wind and rain, enter the soil and flow into rivers, so that serious environmental pollution is caused, and meanwhile, the waste of land resources is caused. Therefore, the non-harmful treatment and comprehensive utilization of the nonferrous metallurgy waste slag are research hotspots in the metallurgical industry.
The hydrometallurgical process often employs ammonia liquor as a leaching agent and a precipitating agent, and thus high concentrations of ammonia ions are often present in the waste slag produced by the process. Currently, few researches and related patents are provided for ammonia ion disposal in waste residues. The ion exchange method, the microbiological method and the breakpoint chlorination method for removing ammonia from common wastewater are not applicable to waste residue treatment, and a large amount of water is required to be added for treating ammonia ions in waste residue by adopting the stripping method, and the energy consumption is high due to evaporation of water along with stripping.
Disclosure of Invention
The invention mainly aims to provide an ammonia removal method for metallurgical waste residues, which aims to solve the problem of high energy consumption in ammonia removal of the waste residues in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a method for removing ammonia from metallurgical slag. The ammonia removal method comprises the following steps: step S1, pulping the metallurgical waste residue to obtain pulping liquid; step S2, causticizing the slurry by lime milk to obtain the slurry containing NH3Causticizing the slurry; and step S3, performing deamination treatment on the causticized slurry by adopting steam to obtain separated ammonia-containing steam and slurry.
Further, in the step S1, the metallurgical slag is slurried with water, and preferably, the solid content of the slurrying liquid is 15-40%.
Further, the step S2 includes mixing the lime milk and the slurry under stirring to causticize, preferably, the lime milk has a mass concentration of 10-25%, preferably, the causticizing temperature is 15-80 ℃, and preferably, the pH of the causticized slurry is 10-12.
Further, the above step S3 includes passing the causticized slurry into a stripping rectification tower for deamination, and preferably step S3 includes: introducing the causticized slurry into a gas stripping rectifying tower from an inlet at the top of the gas stripping rectifying tower, introducing steam into the gas stripping rectifying tower from the bottom of the gas stripping rectifying tower, carrying out gas stripping separation on the causticized slurry by utilizing the steam, obtaining ammonia-containing steam at the top of the tower, and obtaining slag slurry at the bottom of the tower.
Further, in the step S3, M stages of gas stripping rectifying towers connected in series are used for deamination, wherein the slurry of the N-1 th stage of gas stripping rectifying tower is taken as the causticized slurry of the N stage of gas stripping rectifying tower and is introduced into the gas stripping rectifying tower from the tower top inlet of the N stage of gas stripping rectifying tower, M is an integer greater than or equal to 2, and N is a positive integer less than or equal to M and greater than or equal to 2.
Further, the steam of each stage of the gas stripping rectifying tower is new steam, and preferably, at least part of the ammonia-containing steam obtained from the last stage of the gas stripping rectifying tower is returned to the step S2 to be used as a heat source for heating the slurry liquid.
Further, the steam of each stage of the stripping rectifying tower is new steam, and before introducing the causticized slurry into the first stage of the stripping rectifying tower, the step S3 further includes a process of preheating the causticized slurry, preferably, at least part of the preheated heat source comes from the ammonia-containing steam obtained from the last stage of the stripping rectifying tower.
Further, the ammonia-containing steam of the Nth stage stripping and rectifying tower enters from the bottom of the tower as part of steam of the Nth-1 stage stripping and rectifying tower.
Further, when the pH value of the slurry of the stripping and rectifying tower of the Nth stage is less than 10, the slurry is returned to the step S2 for causticization, wherein N is less than M.
Further, the ammonia removal method further comprises the following steps: and (3) carrying out acid absorption or ammonia water concentration on the ammonia-containing steam, and/or filtering the slurry.
Further, the metallurgical waste residue is ammonium sulfate-containing metallurgical waste residue.
By applying the technical scheme of the invention, firstly, the metallurgical waste residue is slurried to obtain slurrying liquid, and then the slurrying liquid is causticized in lime milk to obtain the slurry containing NH3To causticize the slurry. Then directly carrying out deamination treatment on the causticized slurry by steam, further heating the causticized slurry by the steam to release ammonia from the slurry and carrying out free ammonia by using the airflow of the steam, thereby compacting the waste residuesThe purpose of deamination now, and then make solid deamination back discharge up to standard, above-mentioned in-process water consumption is lower, and steam deamination efficiency is higher, and the consumption of steam is less, and this process has saved the filtering step to the thick liquid after the causticization, saves a process, has removed the step that still will handle the ammonia respectively to sediment and liquid simultaneously, saves the cost, has consequently reduced the energy consumption that the waste residue removed the ammonia.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
As described in the background of the present application, the deamination of waste residue in the prior art has high energy consumption, and in order to solve the problem, the present application provides a method for removing ammonia from waste residue.
In an exemplary embodiment of the present application, a method for removing ammonia from metallurgical slag is provided. The ammonia removal method comprises the following steps: step S1, pulping the metallurgical waste residue to obtain pulping liquid; step S2, causticizing the slurry by lime milk to obtain the slurry containing NH3Causticizing the slurry; and step S3, performing deamination treatment on the causticized slurry by adopting steam to obtain separated ammonia-containing steam and slurry.
The ammonia removal method adopts a wet ammonia removal method, namely firstly pulping the metallurgical waste residue to obtain pulping liquid, and then causticizing the pulping liquid in lime milk to obtain the ammonia removal method containing NH3To causticize the slurry. The causticized slurry is directly subjected to deamination treatment by steam, ammonia is released from the slurry and free ammonia is taken out by steam through further heating the causticized slurry by steam, so that the waste residue is deaminated, and then the solid is discharged after deamination to reach the standard.
In an embodiment of the application, in step S1, the metallurgical slag is slurried with water, and preferably, the solid content of the slurry is 15 to 40%. Firstly, the metallurgical waste residue is slurried in water to obtain slurrying liquid, so that substances such as inorganic salt and the like dissolved in water in the waste residue are dissolved in the water and are uniformly mixed with alkaline substances in a causticizing step, and the slurrying liquid is promoted to be fully causticized. The solid content of the slurry is controlled to be in the range, so that on one hand, the phenomenon that the slurry is too thin to cause the increase of energy consumption in the post-treatment is avoided, and on the other hand, the method is favorable for the high-efficiency causticization in the next step.
In another embodiment of the present application, the step S2 includes mixing the lime milk and the slurry under stirring to causticize, where a mass concentration of the lime milk is preferably 10 to 25%, a temperature of causticization is preferably 15 to 80 ℃, and a pH of the causticized slurry is preferably 10 to 12.
The stirring aims to ensure that the lime milk is more fully contacted with the slurry liquid, so that ammonium ions and hydroxide ions are more fully reacted to convert the ammonium ions into ammonia gas. The temperature condition and the pH condition are controlled to ensure that ammonium ions can be efficiently converted into free ammonia gas without causing unnecessary energy consumption.
In another embodiment of the present application, the step S3 includes introducing the causticized slurry into a stripping and rectifying tower for deamination, and preferably, the step S3 includes: introducing the causticized slurry into a gas stripping rectifying tower from an inlet at the top of the gas stripping rectifying tower, introducing steam into the gas stripping rectifying tower from the bottom of the gas stripping rectifying tower, carrying out gas stripping separation on the causticized slurry by utilizing the steam, obtaining ammonia-containing steam at the top of the tower, and obtaining slag slurry at the bottom of the tower. The method adopts a mode of introducing the causticized slurry from the gas stripping rectifying tower from top to bottom and a mode of introducing steam from bottom to top, so that the causticized slurry is in reverse contact with the steam, the gravity action of the causticized slurry is fully utilized, and the characteristics of low density and fluidity of the steam are utilized, so that the energy consumption of feeding is saved, the steam is in more full contact with the causticized slurry, and the causticized slurry is better heated to release ammonia gas in the steam. Wherein the function of the steam is as follows: on one hand, the ammonia dissolved in the causticized slurry is heated and released, and on the other hand, the pressure and the fluidity of the steam are utilized to drive the free ammonia to flow together and be released from the gas stripping rectifying tower.
In order to increase the removal rate of ammonia gas in the causticized slurry, preferably, in step S3, M-stage serially connected gas stripping rectifying towers are used for deamination, wherein the slurry from the N-1 st stage gas stripping rectifying tower is introduced into the gas stripping rectifying tower from the inlet at the top of the N th stage gas stripping rectifying tower as the causticized slurry from the N th stage gas stripping rectifying tower, M is an integer not less than 2, and N is a positive integer not less than M and not more than 2.
In addition, in order to improve the deamination efficiency of each stage of gas stripping rectifying tower, the steam of each stage of gas stripping rectifying tower is preferably new steam. The new steam is introduced into each stage of the gas stripping rectifying tower, the ammonia-containing steam obtained by separating the new steam introduced into the Nth stage of the gas stripping rectifying tower is directly subjected to the ammonia-containing steam removal treatment, the ammonia-containing steam obtained by separating the new steam introduced into the (N + 1) th stage of the gas stripping rectifying tower is also directly subjected to the ammonia-containing steam removal treatment, and the like, along with the deamination process of the slag slurry by the new steam at each stage, less and less ammonia is contained in the slag slurry, and less ammonia is contained in the steam obtained by deaminating the slag slurry after multistage deamination treatment by introducing the new steam into the last stage of the gas stripping rectifying tower.
Further, in order to improve the comprehensive utilization efficiency of heat in the ammonia removal method of the present application, it is preferable that the ammonia-containing vapor obtained from the last stage of the stripping and rectifying tower is returned to step S2 as a heat source to heat the slurry.
In another embodiment, the steam of each of the stripping rectification towers is new steam, and before introducing the causticized slurry into the first stripping rectification tower, the step S3 further includes a process of preheating the causticized slurry, preferably at least part of the preheated heat source comes from the ammonia-containing steam obtained from the last stripping rectification tower. The causticized slurry is preheated, so that the gas stripping efficiency is improved, and in addition, ammonia-containing steam obtained by the last stage of gas stripping rectifying tower is used as at least part of heat source for preheating the causticized slurry, so that the comprehensive utilization of heat is realized, and the economic benefit of the ammonia removal method is improved.
In still another embodiment of the present application, the ammonia-containing vapor of the stripping and rectifying tower of the Nth stage enters from the bottom of the tower as part of the vapor of the stripping and rectifying tower of the Nth-1 stage.
Namely, multistage gas stripping rectifying towers connected in series are used for deaminating the causticized slurry step by step, the slurry obtained after the N-1 th stage deamination treatment of the gas stripping rectifying towers is used as the causticized slurry of the N-th stage gas stripping rectifying tower, and the slurry subjected to deamination treatment again at the N-th stage is used as the causticized slurry of the (N + 1) th stage gas stripping rectifying tower for continuous deamination treatment. And the deamination steam obtained after the deamination is carried out from the (N + 1) th stage enters the Nth stage to further heat and deaminate the slurry, the deamination steam obtained after the deamination is carried out from the Nth stage enters the (N-1) th stage to further heat and deaminate the slurry, and so on, the ammonia contained in the slurry obtained after the causticization slurry is deaminated by the multistage gas stripping rectifying tower is less and less, and the ammonia concentration contained in the deamination steam is greater and greater, and on the basis of utilizing less new steam, the better deamination effect on the slurry is realized, and further the cost for removing ammonia is reduced.
In addition, in order to improve the thoroughness of removing ammonia from the metallurgical waste residue, when the pH value of the slurry of the stripping and rectifying tower of the Nth stage is less than 10, the slurry is returned to the step S2 for causticization, wherein N is less than M.
Because the ammonium ions and the ammonia gas have a thermochemical equilibrium reaction in the slurry, when the pH value of the slurry is less than 10, the ammonia gas can be promoted to be dissolved in the slurry again and converted into the ammonium ions, so that the ammonia gas cannot escape easily. Therefore, in order to improve the deamination effect on the slurry, the slurry with the pH value less than 10 in the N-th stage gas stripping rectifying tower is returned to the step S2 for causticization and then deamination treatment.
In another embodiment of the present application, the method for removing ammonia further comprises: and (3) carrying out acid absorption or ammonia water concentration on the ammonia-containing steam, and/or filtering the slurry.
The ammonia gas has good water solubility and certain alkalinity, and the ammonia-containing steam is absorbed by acid, so that on one hand, part of the ammonia gas is dissolved in the water of the acid solution, and the other part of the ammonia gas and the acid have neutralization reaction and are converted into ammonium salt, thereby removing the ammonia gas in the steam. Ammonia concentration is generally achieved by multiple absorption of ammonia-containing vapors by the ammonia solution to increase the concentration of ammonia. Whether the slurry is filtered or not is selected according to actual needs. The ammonia water or ammonium salt obtained by the treatment can be used or sold as a byproduct, so that the overall economic benefit is improved.
The metallurgical waste residue of the application can be commonly used metallurgical waste residue in the prior art, and preferably, the metallurgical waste residue used in the method is the metallurgical waste residue containing ammonium sulfate. The ammonia removal method has outstanding ammonia removal efficiency on the metallurgical waste residue containing ammonium sulfate.
The following will further explain the beneficial effects of the present application in conjunction with the specific examples.
Example 1
Pulping certain smelting waste residue (containing ammonium sulfate) by using water to obtain pulping liquid with the solid content of 30 percent; mixing the slurry liquid with lime milk with the mass concentration of 20% at the temperature of 20-30 ℃ to perform causticization, wherein the causticization time is 1h, and the end point pH value is about 11 to obtain causticized slurry liquid; deaminating the causticized slurry by adopting three-stage series-connected gas stripping rectifying towers, controlling the evaporation temperature in each stage of gas stripping rectifying tower to be near 100 ℃, preheating the causticized slurry to 70-80 ℃, then introducing the heated slurry into the first-stage gas stripping rectifying tower from the tower top inlet of the gas stripping rectifying tower, reversely introducing steam into the first-stage gas stripping rectifying tower from the tower bottom of the first-stage gas stripping rectifying tower to deaminate the causticized slurry, obtaining first-stage ammonia-containing steam at the tower top, obtaining first-stage slag slurry at the tower bottom, introducing the first-stage slag slurry into the second-stage gas stripping rectifying tower from the tower top inlet to serve as the causticized slurry of the second-stage gas stripping rectifying tower, obtaining second-stage ammonia-containing steam at the tower top and obtaining second; and in the process, fresh steam at 120-170 ℃ is introduced into the tower bottom of the third gas stripping rectifying tower, tertiary ammonia-containing steam is introduced into the tower bottom of the second gas stripping rectifying tower, secondary ammonia-containing steam is introduced into the tower bottom of the first gas stripping rectifying tower, and when the tertiary ammonia-containing steam is redundant, the third gas stripping rectifying tower can be used as a heat source to preheat the causticized slurry which is about to enter the first gas stripping rectifying tower.
Controlling the pH value of the slurry of each stage of gas stripping rectifying tower to be between 10 and 11.5, if the pH value of the slurry is less than 10, causticizing the slurry by using lime milk with the mass concentration of 20 percent until the pH value of the causticized slurry is about 11 (the left and right represent that the fluctuation is 0.1, the same is used below), and carrying out deamination to obtain ammonia-containing steam and slurry; filtering the slag slurry, piling up the filter residue after reaching the standard, and removing sulfuric acid and absorbing by ammonia vapor, wherein the removal rate of the smelting waste slag ammonia is 98.06 percent through the process.
Example 2
Example 2 differs from example 1 in that the solid content of the slurry was 15% and the removal rate of ammonia from the smelting slag was 99.1%.
Example 3
Example 3 differs from example 1 in that the solid content of the slurry was 40% and the removal rate of ammonia from the smelting slag was 97.5%.
Example 4
Example 4 differs from example 1 in that the solid content of the slurry was 5% and the removal rate of ammonia from the smelting slag was 90.7%.
Example 5
The difference between the embodiment 5 and the embodiment 1 is that lime milk with the mass concentration of 20 percent is added into the slurry liquid for causticization at the temperature of 15 ℃, the causticization time is 1h, the end point pH value is about 11, and the removal rate of the smelting waste residue ammonia is 98.04 percent.
Example 6
The difference between the embodiment 6 and the embodiment 1 is that lime milk with the mass concentration of 20 percent is added into the slurry liquid at the temperature of 80 ℃ for causticization, the causticization time is 0.5h, the end point pH value is about 11, and the ammonia removal rate of the smelting waste residue is 98.08 percent.
Example 7
The difference between the embodiment 7 and the embodiment 1 is that lime milk with the mass concentration of 20 percent is added into the slurry liquid at the temperature of 5 ℃ for causticization, the causticization time is 2 hours, the end point pH value is about 11, and the removal rate of the smelting waste residue ammonia is 98.05 percent.
Example 8
The difference between the embodiment 8 and the embodiment 1 is that the causticization time is 70min, the pH of the causticized slurry is 10-10.5, and the removal rate of the smelting waste residue ammonia is 95.5%.
Example 9
The difference between the embodiment 9 and the embodiment 1 is that the pH of the causticized slurry is about 12 within 80min of causticization time, and the ammonia removal rate of the smelting waste residue is 98.8%.
Example 10
The difference between the embodiment 10 and the embodiment 1 is that the causticization time is 45min, the pH value of the causticized slurry is about 10, and the ammonia removal rate of the smelting waste residue is 83.3%.
Example 11
The difference between the embodiment 11 and the embodiment 1 is that fresh steam is introduced into each stage, and the ammonia-containing steam obtained from each stage is directly subjected to ammonia-containing steam absorption treatment, and the ammonia removal rate of the smelting waste residue is 99.2%.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
the ammonia removal method adopts a wet ammonia removal method, namely firstly pulping the metallurgical waste residue to obtain pulping liquid, and then causticizing the pulping liquid in lime milk to obtain the ammonia removal method containing NH3To causticize the slurry. The causticized slurry is directly subjected to deamination treatment by steam, ammonia is released from the slurry and free ammonia is taken out by steam through further heating the causticized slurry by steam, so that the waste residue is deaminated, and then the solid is discharged after deamination to reach the standard.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (11)

1. A method for removing ammonia from metallurgical waste residue is characterized by comprising the following steps:
step S1, pulping the metallurgical waste residue to obtain pulping liquid;
step S2, causticizing the slurry by lime milk to obtain the slurry containing NH3Causticizing the slurry; and
and step S3, performing deamination treatment on the causticized slurry by adopting steam to obtain separated ammonia-containing steam and slurry.
2. The method for removing ammonia according to claim 1, wherein the metallurgical slag is pulped with water in step S1, and the solid content of the pulping liquid is preferably 15-40%.
3. The ammonia removal method of claim 1, wherein the step S2 includes mixing the lime milk and the slurry under stirring conditions to causticize, preferably the mass concentration of the lime milk is 10-25%, preferably the causticizing temperature is 15-80 ℃, and preferably the pH value of the causticized slurry is 10-12.
4. The method for removing ammonia according to claim 1, wherein the step S3 comprises passing the causticized slurry into a stripping rectification tower for deamination, and preferably the step S3 comprises:
and introducing the causticized slurry into the gas stripping rectifying tower from the tower top inlet of the gas stripping rectifying tower, introducing the steam into the gas stripping rectifying tower from the tower bottom of the gas stripping rectifying tower, performing gas stripping separation on the causticized slurry by using the steam, obtaining ammonia-containing steam at the tower top, and obtaining slag slurry at the tower bottom.
5. The ammonia removal method of claim 4, wherein in the step S3, M stages of gas stripping rectifying towers connected in series are used for the ammonia removal treatment, wherein the slurry of the N-1 stage of gas stripping rectifying tower is taken as the causticized slurry of the N stage of gas stripping rectifying tower and is introduced into the gas stripping rectifying tower from the tower top inlet of the N stage of gas stripping rectifying tower, M is an integer greater than or equal to 2, and N is a positive integer less than or equal to M and greater than or equal to 2.
6. The method for removing ammonia according to claim 5, wherein the steam of each stage of the stripping and rectifying tower is fresh steam, and preferably at least part of the ammonia-containing steam obtained from the last stage of the stripping and rectifying tower is returned to the step S2 to be used as a heat source for heating the slurry.
7. The method of claim 5, wherein the steam of each stage of the stripping and rectifying tower is new steam, and the step S3 further comprises a process of preheating the causticized slurry before introducing the causticized slurry into the first stage of the stripping and rectifying tower, preferably at least part of the heat source for preheating comes from the ammonia-containing steam obtained from the last stage of the stripping and rectifying tower.
8. The method for removing ammonia according to claim 5, wherein the ammonia-containing steam of the stripping and rectifying tower of the Nth stage enters from the bottom of the tower as part of the steam of the stripping and rectifying tower of the N-1 st stage.
9. The method of claim 5, wherein when the pH value of the slurry in the stripping and rectifying tower of the Nth stage is less than 10, the slurry is returned to the step S2 for causticization, wherein N is less than M.
10. The method of removing ammonia according to any one of claims 1 to 9, further comprising: and (3) carrying out acid absorption or ammonia water concentration on the ammonia-containing steam, and/or filtering the slurry.
11. The method of any one of claims 1 to 9, wherein the metallurgical slag is a metallurgical slag containing ammonium sulfide.
CN201910907455.4A 2019-09-24 2019-09-24 Ammonia removal method for metallurgical waste residue Pending CN110615571A (en)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080132588A1 (en) * 2003-12-03 2008-06-05 Rentech, Inc. Apparatus and methods for the production of ammonia and fischer-tropsch liquids
CN101264948A (en) * 2008-04-25 2008-09-17 北京化工大学 Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method
CN106734073A (en) * 2016-12-12 2017-05-31 武汉大学 A kind of electrolytic manganese waste residue deamination disappears manganese processing method and processing device

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080132588A1 (en) * 2003-12-03 2008-06-05 Rentech, Inc. Apparatus and methods for the production of ammonia and fischer-tropsch liquids
CN101264948A (en) * 2008-04-25 2008-09-17 北京化工大学 Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method
CN106734073A (en) * 2016-12-12 2017-05-31 武汉大学 A kind of electrolytic manganese waste residue deamination disappears manganese processing method and processing device

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