System and method for separating ions in spent acid

Abstract

The application discloses a system and method for separating ions in waste acid, and the system comprises a reaction tower, a waste acid inlet for feeding waste acid is arranged at the top of the reaction tower, and a hydrogen sulfide inlet for feeding hydrogen sulfide is arranged at the bottom of the reaction tower; a plurality of reaction units are arranged in the reaction tower along the height direction of the reaction tower; different sulfides generated by the reaction of the waste acid and the hydrogen sulfide are precipitated in different reaction units respectively; and a precipitation separation device is connected to each reaction unit with sulfide precipitation. By using the tower gas absorption reaction process, the different elements in the waste acid are separated by using the characteristics of the step-by-step dissolution of the hydrogen sulfide gas in the waste acid and the difference of the solubility product of different sulfides, the controllability of the process is improved, the resource recovery efficiency of the waste acid is improved, the resource waste is reduced, and the discharge amount of solid waste is further reduced.

Description

Technical Field

[0001] The present invention relates to the technical field of waste acid treatment, and in particular to a system and method for separating ions in waste acid. Background Art

[0002] During the acid production and purification process, flue gas scrubbing produces waste acid at a concentration of approximately 10%. Arsenic, zinc, cadmium, lead, and other ions in the flue gas enter this waste acid, creating what is known as "dirty acid." As the scrubbing cycle progresses, these pollutants gradually accumulate. To prevent impurity accumulation and impact on purification and subsequent acid production, a certain amount of dirty acid must be regularly discharged for treatment and disposal. Certain elements in dirty acid, such as arsenic, are highly toxic, posing serious hazards to plants and animals and damaging the ecological environment. Direct discharge also results in a significant waste of dilute acid resources, heavy metals, and other elements. Therefore, this waste acid must be rigorously treated before discharge.

[0003] At present, the main methods for treating acid wastewater in China include sulfidation + gypsum + neutralization method, sulfidation + neutralization method, neutralization method and other methods.

[0004] 1. Sulfurization + gypsum + neutralization method

[0005] like Figure 1 As shown, the process first adds waste acid and sodium sulfide (or sodium hydrosulfide) solution to the sulfidation reaction tank, causing most of the impurity ions in the waste acid to react with the sulfide ions to form an insoluble sulfide precipitate, which is then removed. A small amount of hydrogen sulfide overflows during the reaction (generally less than 0.1% by volume). After liquid-solid separation, limestone milk or lime is added to the clear liquid in the gypsum process to control the pH to 2.5-4.0, producing gypsum (CaSO4·2H2O). After further liquid-solid separation, lime milk and iron salt are further added to the clear liquid in the neutralization process to neutralize the pH to 7-11. After liquid-solid separation, neutralized slag is produced. The clear liquid is sent to a deep treatment station for treatment to meet standards before discharge or reuse. The neutralized slag produced by this process is generally classified as Class II general industrial solid waste, while the gypsum can be sold as a by-product.

[0006] The main disadvantages of this process are: 1. The price of sodium sulfide or sodium hydrosulfide is relatively high, and the operating cost of waste acid treatment is high; 2. The process is difficult to control, and excessive addition of sodium sulfide or sodium hydrosulfide is usually required. Sodium sulfide or sodium hydrosulfide also contains a large amount of impurities, which introduce a large amount of sodium ions into the wastewater, easily forming crystals and causing blockage or corrosion of pipeline equipment, increasing the treatment cost of zero wastewater discharge; 3. The removal rate of Cu and As in the sulfidation process is low, resulting in a large amount of neutralization slag produced in the subsequent neutralization process.

[0007] 2. Vulcanization + neutralization method

[0008] like Figure 2As shown in the figure, the process first adds dirty acid and sodium sulfide (or sodium hydrosulfide) solution to the sulfidation reaction tank to remove most of the heavy metal ions. After liquid-solid separation, lime milk and iron salt are added to the clear liquid in the neutralization process to control the pH value to 7-11. Liquid-solid separation is performed again to produce a large amount of neutralized slag. The clear liquid is sent to a deep treatment station for treatment to meet the standards and then discharged or reused.

[0009] The main disadvantages of this process are: 1. The price of sodium sulfide or sodium hydrosulfide is relatively high, and the operating cost of waste acid treatment is high; 2. Sodium sulfide or sodium hydrosulfide contains a large amount of impurities. The addition of traditional vulcanizing agents will bring a large amount of sodium ions into the wastewater, which is easy to form crystals and cause blockage or corrosion of pipeline equipment, increasing the treatment cost of zero wastewater discharge; 3. There is no gypsum process, resulting in the output of neutralization slag being hazardous waste.

[0010] 3. Neutralization method

[0011] In order to alleviate the problem of sodium salt enrichment, some copper smelting enterprises have changed the waste acid treatment process to a two-stage neutralization method, such as Figure 3 As shown, instead of adding sulfiding agent, a large amount of lime milk and iron salt are directly added to the waste acid to control the pH value to 7-11.

[0012] While the traditional neutralization method is simple and has low reagent costs, it produces a large amount of gypsum-containing neutralized residue, which is a hazardous waste. Due to the lack of a sulfidation process, the amount of hazardous waste produced is far higher than that of similar enterprises. Furthermore, the arsenic content of this gypsum-containing neutralized residue exceeds 5%. According to GB18598-2019, the "Hazardous Waste Landfill Pollution Control Standard," this gypsum-containing neutralized residue must be disposed of in a rigid landfill, making this treatment method unsustainable.

[0013] Moreover, the various impurity ions contained in the waste acid are also important resources. The "neutralization method" introduced above cannot achieve resource recovery. The sulfiding agent added in the "sulfurization + gypsum + neutralization method" and the "sulfurization + neutralization method" is sodium sulfide. The process is not easy to control and usually requires excessive addition of sodium sulfide or sodium hydrosulfide. The generated sulfide precipitate is a mixed precipitate of various elemental sulfides, which makes subsequent resource separation more difficult. Moreover, sodium sulfide or sodium hydrosulfide contains a large amount of impurities and brings a large amount of sodium ions into the wastewater, which easily forms crystals and causes blockage or corrosion of pipeline equipment, increasing the treatment cost of zero wastewater discharge. Therefore, in order to solve the problem of difficulty in separating and recovering various ions in waste acid, it is necessary to develop a process that can separate various ions in waste acid in steps. Summary of the Invention

[0014] The present invention provides a method for separating various impurity ions in waste acid in a step-by-step manner to solve the problem of difficulty in effectively recovering impurity ions in waste acid. The present invention is achieved through the following technical solutions:

[0015] A system for separating ions in waste acid comprises a reaction tower, wherein a waste acid inlet is provided at the top of the reaction tower for introducing waste acid, and a hydrogen sulfide inlet is provided at the bottom of the reaction tower for introducing hydrogen sulfide;

[0016] The reaction tower is provided with a plurality of reaction units along the height direction of the reaction tower; the waste acid passes through each reaction unit from top to bottom;

[0017] Each reaction unit with sulfide precipitation is connected to a precipitation separation device; the precipitation separation device is used to remove the sulfide precipitate in the dirty acid from the reaction tower.

[0018] The system of the present invention pumps waste acid into the top of the reaction tower and introduces hydrogen sulfide gas from the bottom. The two materials engage in countercurrent contact within the reaction tower for gas-liquid mass transfer. The hydrogen sulfide gas dissolves stepwise into the waste acid on each reaction unit, ionizing to produce negative divalent sulfur ions, which react with ions in the waste acid to form a precipitate. Because hydrogen sulfide dissolves stepwise, the ions in the waste acid are precipitated and enriched in batches on different trays based on the solubility products of the sulfides formed. Side-line extraction is performed on each reaction unit where sulfide is enriched and precipitated, and the extracted material enters a solid-liquid separation system to produce a liquid and a sulfide precipitate of the corresponding element.

[0019] Optionally, the number of the precipitation separation devices is the same as the number of ion species that can generate sulfides in the waste acid.

[0020] Optionally, the reaction unit is a tower plate or a packing unit.

[0021] Optionally, the reaction unit is a tower plate.

[0022] Optionally, the reaction tower is provided with 20 to 40 reaction units;

[0023] Optionally, 20 to 30 reaction units are provided inside the reaction tower.

[0024] Optionally, a liquid collector is provided below the reaction unit with sulfide precipitation, and the liquid collector is connected to a precipitation separation device through a side discharge pipe; the precipitation separation device refluxes the waste acid after separation of sulfide precipitation to the next reaction unit in the reaction tower through a side reflux pipe.

[0025] For example, HgS is precipitated and enriched on the 5th reaction unit, and the solid-liquid mixture of the 5th reaction unit enters the precipitation separation device through the side discharge pipe. After the precipitation separation device separates the HgS precipitate, the liquid flows back to the 6th reaction unit through the side reflux pipe.

[0026] Optionally, a side line discharge pump is provided on the side line discharge pipe; and a side line reflux pump is provided on the side line reflux pipe.

[0027] Optionally, the number of side discharge pumps, sedimentation separation devices, and side return pumps is determined by the number of sulfide precipitate types that need to be separated. For example, if the waste acid to be treated contains four ions that generate sulfide precipitates, four sets of side discharge pumps, sedimentation separation devices, and side return pumps are installed in the corresponding reaction units where sulfide precipitation occurs. If the waste acid to be treated contains six ions that generate sulfide precipitates, six sets of side discharge pumps, sedimentation separation devices, and side return pumps are installed in the corresponding reaction units where sulfide precipitation occurs.

[0028] Optionally, a tail gas outlet is provided at the top of the reaction tower, and the tail gas outlet is connected to a tail gas treatment system;

[0029] Optionally, a waste acid outlet is provided at the bottom of the reaction tower, and the waste acid outlet is connected to a waste acid concentration system.

[0030] Optionally, the ion is Hg 2+ 、Hg + 、Cu 2+ 、Cu + 、As 3+ , Pb 2+ 、Cd 2+ 、Zn 2+ 、Co 2+ 、Fe 2+ 、Mn 2+ At least one of .

[0031] The present invention also proposes a method for separating ions in waste acid, wherein the waste acid is countercurrently contacted with hydrogen sulfide gas in a reaction vessel to generate a reaction, and the sulfide precipitate generated by the reaction is promptly removed from the reaction vessel to obtain at least one single sulfide.

[0032] Optionally, the reaction vessel is a plate tower.

[0033] Optionally, the pressure in the reaction vessel is 0.1 MPa to 0.6 MPa;

[0034] Optionally, the pressure in the reaction vessel is 0.1 MPa to 0.3 MPa.

[0035] Optionally, the reaction temperature of each reaction unit in the reaction container is 0-40°C.

[0036] Optionally, the reaction temperature of each reaction unit in the reaction vessel is 20-30°C.

[0037] Optionally, the mass flow ratio of the dirty acid and hydrogen sulfide introduced into the reaction tower per unit time is 1:10 to 3:1.

[0038] Optionally, the separation system adopts centrifugal separation or belt separation.

[0039] Furthermore, the separation system adopts centrifugal separation.

[0040] According to another aspect of the present invention, the present invention provides a system for step-by-step separation of impurity ions in waste acid, comprising: a reaction tower feed pump, a reaction tower, a side discharge pump, a separation system, and a side reflux pump connected in sequence by pipelines, wherein the reaction tower feed pump is used to pump the waste acid into the reaction tower; the reaction tower is used to step-by-step separate and precipitate impurity elements in the waste acid; the side discharge pump is used to output a liquid-solid mixture on a certain impurity sulfide precipitation and enrichment tray in the reaction tower; the separation system is used to perform liquid-solid separation on the liquid-solid mixture output by the side discharge pump; and the side reflux pump is used to reflux the liquid separated by the separation system to the next tray corresponding to the side discharge pump.

[0041] Optionally, the reaction tower is a plate tower or a packed tower.

[0042] Furthermore, the reaction tower is a plate tower.

[0043] Optionally, the reaction tower is equipped with a cooling system or each separation system is equipped with a cooling system for cooling the material. Further, the reaction tower is equipped with a cooling system.

[0044] The technical solution of the present invention has the following advantages:

[0045] 1. The system for separating ions in the waste acid of the present invention uses a reaction tower gas absorption reaction process, and utilizes the characteristics of the graded and gradual dissolution of hydrogen sulfide gas in the waste acid and the difference in the solubility product of the sulfides of the impurity elements to perform graded separation of the impurity elements in the waste acid, thereby improving the controllability of the process, improving the resource recovery efficiency of the waste acid, reducing resource waste, and reducing the emission of solid waste.

[0046] 2. The method of the present invention has a simple process flow, strong operability and good market benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0047] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the specific embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0048] Figure 1 It is a flow chart of sulfide + gypsum + neutralization method;

[0049] Figure 2 This is the flow chart of the sulfidation + neutralization method;

[0050] Figure 3 It is a flow chart of the neutralization method;

[0051] Figure 4 is a schematic diagram of the system for separating ions in dirty acid in Example 1;

[0052] Figure 5 This is a schematic diagram of the side line extraction reflux.

[0053] Figure 6 Schematic diagram of the system for separating ions in dirty acid in Example 2.

[0054] The reference numerals represent the following meanings:

[0055] Figure 4 Middle: reaction tower feed pump (1), reaction tower (2), side line discharge pump (a), separation system (b), side line reflux pump (c);

[0056] Figure 5 Middle: tray (21), liquid collector (22), side discharge pump (a), separation system (b), side reflux pump (c).

[0057] Figure 6 In: reaction tower feed pump (1), reaction tower (2), first side line discharge pump (3), first separation system (4), first side line reflux pump (5), second side line discharge pump (6), second separation system (7), second side line reflux pump (8), third side line discharge pump (9), third separation system (10), third side line reflux pump (11), fourth side line discharge pump (12), fourth separation system (13), fourth side line reflux pump (14) DETAILED DESCRIPTION

[0058] Various exemplary embodiments of the present invention are now described in detail. This detailed description should not be considered as a limitation of the present invention, but should be understood as a more detailed description of certain aspects, features, and embodiments of the present invention. It should be understood that the terms used in the present invention are only for describing specific embodiments and are not intended to limit the present invention.

[0059] In addition, for numerical ranges in the present invention, it is understood that each intervening value between the upper and lower limits of the range is also specifically disclosed. Each smaller range between any stated value or stated range, and any other stated value or intervening value in the stated range, is also included in the present invention. The upper and lower limits of these smaller ranges may independently be included or excluded in the range.

[0060] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which the invention pertains. Although preferred methods and materials have been described herein, any methods and materials similar or equivalent to those described herein can also be used in the practice or testing of the present invention.

[0061] The words “include,” “including,” “have,” “contain,” etc. used in this document are open-ended terms, meaning including but not limited to.

[0062] Example 1

[0063] like Figure 1 The system for separating ions from waste acid shown in the figure includes a reaction tower 2, the top of which is provided with a waste acid inlet for introducing waste acid, which is introduced through a reaction tower feed pump 1. The bottom of the reaction tower is provided with a hydrogen sulfide inlet for introducing hydrogen sulfide.

[0064] The reaction tower is provided with a plurality of reaction units along the height direction of the reaction tower. The reaction tower 2 of this embodiment is a plate tower, and the reaction units are trays. In this embodiment, the number of trays is 30, and each tray is equipped with a cooling system to maintain the reaction temperature of each reaction unit in the reaction tower at 0-40°C.

[0065] The waste acid is pumped into the reaction tower from the top, and hydrogen sulfide gas is introduced from the bottom. The two materials are in countercurrent contact within the reaction tower for gas-liquid mass transfer. The hydrogen sulfide gas dissolves step by step into the waste acid on each reaction unit, ionizing to produce negative divalent sulfur ions, which react with various ions in the waste acid to form precipitates. Since hydrogen sulfide undergoes a step-by-step dissolution reaction, as shown in the table below, the ions in the waste acid will be precipitated and enriched in batches on different plates based on the solubility products of the sulfides they form. A precipitation separation device should be installed on each plate where sulfide precipitation is generated to separate the precipitate from the waste acid. The separated waste acid then flows back into the next plate to continue the reaction. In this way, each precipitation separation device achieves the step-by-step separation of different ions.

[0066] Table 1 Solubility products of metal sulfides (temperature: 25°C)

[0067] Metal sulfides <![CDATA[溶度积K sp ]]> <![CDATA[pK sp ]]> Metal sulfides <![CDATA[溶度积K sp ]]> pK sp ]]> HgS <![CDATA[4.0×10 -53 ]]> 52.40 CdS <![CDATA[8.0×10 -27 ]]> 26.10 <![CDATA[Cu2S]]> <![CDATA[2.5×10 -48 ]]> 47.60 ZnS <![CDATA[2.93×10 -25 ]]> 23.80 <![CDATA[Hg2S]]> <![CDATA[1.0×10 -45 ]]> 45.00 CoS 7.9 x 10 -21 ]]> 20.40 CuS <![CDATA[6.3×10 -36 ]]> 35.20 FeS <![CDATA[6.3×10 -18 ]]> 17.50 <![CDATA[As2S3]]> <![CDATA[4.1×10 -35 ]]> 34.39 MnS <![CDATA[2.5×10 -13 ]]> 12.60 PbS <![CDATA[8.0×10 -28 ]]> 27.00

[0068] Different sulfides generated by the reaction of waste acid and hydrogen sulfide are precipitated in different reaction units respectively; the solid-liquid mixture in each reaction unit with sulfide precipitation enters the precipitation separation device through the side discharge pipe, and the precipitation separation device returns the liquid after precipitation separation to the next reaction unit in the reaction tower through the side reflux pipe. Figure 5As shown, sulfide precipitates on tray 21. A liquid collector 22 is located below tray 21. This liquid collector 22 is connected to a sedimentation separation device b via a side discharge pipe, which is equipped with a side discharge pump a. After the sulfide is separated in sedimentation separation device b, the remaining liquid flows back to the next tray in the reaction tower via a side reflux pipe, which is equipped with a side reflux pump c. The number of side discharge pumps a, sedimentation separation devices b, and side reflux pumps c is determined by the types of impurity elements to be separated.

[0069] In addition, the solid discharge ports of each precipitation separation device are also connected to a recovery system (not shown in the figure), the tail gas outlet at the top of the reaction tower is also connected to a tail gas treatment system (not shown in the figure), and the bottom purified dirty acid discharge port of the reaction tower (2) is also connected to a concentration system (not shown in the figure).

[0070] Example 2

[0071] A method for separating various ions in waste acid by a system for separating ions in waste acid, comprising the following steps:

[0072] The waste acid in this embodiment contains Hg 2+ 、As 3+ , Pb 2+ 、Cd 2+ The four precipitable ions have contents of 40 mg / l, 2000 mg / l, 50 mg / l and 30 mg / l respectively. Figure 6 As shown, 4 sets of side discharge pumps, precipitation separation devices, and side reflux pumps are used. The dirty acid is introduced into the top of reaction tower 2 through the reaction tower feed pump, and hydrogen sulfide gas is introduced into the bottom of reaction tower 2. The operating pressure in the reaction tower is 0.3MPa. Each tower plate is equipped with a cooling system to maintain the reaction temperature of each reaction unit in the reaction tower at 25°C. The two materials are in countercurrent contact in the reaction tower for gas-liquid mass transfer, and the ratio of the mass flow rate of dirty acid and hydrogen sulfide per unit time is 1:3. Hydrogen sulfide gas dissolves step by step into the dirty acid on each tower plate, ionizes to produce negative divalent sulfur ions, and reacts with the ions in the dirty acid to form precipitates. Since hydrogen sulfide is a step-by-step dissolution reaction, the ions in the dirty acid will be precipitated and enriched in batches on different tower plates according to the difference in the solubility product of the sulfide formed:

[0073] The HgS precipitate is concentrated on the fifth tray. The liquid-solid mixture on the fifth tray is withdrawn from the side by a first side-line discharge pump 3. The withdrawn material enters the first separation system 4 for centrifugal separation to produce a purified reflux liquid and an HgS precipitate. The purified reflux liquid is returned to the sixth tray of the reaction tower 2 by a first side-line reflux pump 5, and the HgS precipitate is collected and sent to a recovery system.

[0074] As2S3 precipitates and accumulates on the 10th tray. The liquid-solid mixture on the 10th tray is withdrawn from the side by a second side-line discharge pump 6. The withdrawn material enters a second separation system 7 for centrifugal separation to produce a purified reflux liquid and As2S3 precipitate. The liquid is returned to the 11th tray of the reaction tower 2 by a second side-line reflux pump 8, and the As2S3 solid is collected and sent to a recovery system.

[0075] The PbS precipitate is concentrated on the 18th tray. The liquid-solid mixture on the 18th tray is withdrawn by a third side-line discharge pump 9. The withdrawn material enters the third separation system 10 for centrifugal separation to produce a purified reflux liquid and a PbS precipitate. The liquid is returned to the 19th tray of reaction tower 2 by a third side-line reflux pump 11, and the PbS solid is collected and sent to a recovery system.

[0076] The CdS precipitate is concentrated on the 25th tray. The liquid-solid mixture on the 25th tray is withdrawn from the side by a fourth side-line discharge pump 12. The withdrawn material enters the fourth separation system 13 for centrifugal separation to produce a purified reflux liquid and CdS precipitate. The liquid is returned to the 26th tray of the reaction tower 2 by a fourth side-line reflux pump 14, and the CdS solid is collected and sent to the recovery system.

[0077] After the whole tower is reacted and separated step by step, the tail gas discharged from the top of the tower is sent to the tail gas treatment system. The purified Hg in the waste acid is obtained at the bottom of the tower. 2+ 、As 3+ , Pb 2+ 、Cd 2+ The contents of the four ions are 0.2mg / l, 0.3mg / l, 0.1mg / l and 0.4mg / l respectively. Most of the ions are recovered in the form of sulfide precipitation. The purified dirty acid is obtained at the bottom of the tower.

[0078] Obviously, the above embodiments are merely examples for clarity of explanation and are not intended to limit the implementation methods. Those skilled in the art will readily appreciate that other variations or modifications based on the above descriptions are possible. It is not necessary and impossible to enumerate all implementation methods here. Obvious variations or modifications arising therefrom remain within the scope of protection of the present invention.

Claims

1. A system for separating ions from polluted acid, characterized in that: The reactor comprises a reaction tower, wherein a waste acid inlet is provided at the top of the reaction tower for introducing waste acid, and a hydrogen sulfide inlet is provided at the bottom of the reaction tower for introducing hydrogen sulfide; The reaction tower is provided with a plurality of reaction units along the height direction of the reaction tower; the waste acid passes through each reaction unit in sequence from top to bottom; the reaction tower is provided with 20 to 40 reaction units; Each reaction unit with sulfide precipitation is connected to a precipitation separation device; the precipitation separation device is used to remove the sulfide precipitate in the waste acid from the reaction tower; A liquid collector is provided below the reaction unit with sulfide precipitation, and the liquid collector is connected to the precipitation separation device through a side line discharge pipe; the precipitation separation device refluxes the waste acid after separation of sulfide precipitation to the next reaction unit in the reaction tower through a side line reflux pipe; The side line discharge pipe is provided with a side line discharge pump; the side line return pipe is provided with a side line return pump.

2. The system for separating ions in dirty acid according to claim 1, characterized in that: The reaction unit is a filler unit.

3. The system for separating ions in dirty acid according to claim 1, characterized in that: The reaction unit is a tower plate.

4. The system for separating ions in dirty acid according to claim 1, characterized in that: The reaction tower is provided with 20 to 30 reaction units.

5. The system for separating ions in dirty acid according to claim 1, characterized in that: The top of the reaction tower is provided with an exhaust gas outlet, which is connected to an exhaust gas treatment system; and / or A waste acid outlet is provided at the bottom of the reaction tower, and the waste acid outlet is connected to a waste acid concentration system.

6. A method for separating ions in dirty acid, characterized in that: The system for separating ions in waste acid according to any one of claims 1 to 5 is used to bring waste acid into countercurrent contact with hydrogen sulfide gas in a reaction tower to generate a reaction, and the sulfide precipitate generated by the reaction is promptly removed from the reaction tower to obtain at least one single sulfide.

7. The method for separating ions in dirty acid according to claim 6, wherein: The pressure in the reaction tower is 0.1 MPa to 0.6 MPa.

8. The method for separating ions in dirty acid according to claim 7, wherein: The pressure in the reaction tower is 0.1 MPa to 0.3 MPa.

9. The method for separating ions in dirty acid according to claim 6, wherein: The reaction temperature of each reaction unit in the reaction tower is 0-40°C.

10. The method for separating ions in dirty acid according to claim 6, characterized in that: The mass flow ratio of the dirty acid and hydrogen sulfide introduced into the reaction tower per unit time is 1:10~3:1.

Images