Method for treating acid-making tail gas and waste acid to recover antimony by using antimony-containing waste liquid

Abstract

The invention belongs to the technical field of comprehensive utilization of resources, and relates to a method for treating acid-making tail gas and waste acid to recover antimony by using antimony-containing waste liquid, which comprises the following steps: (1) primary treatment of the antimony-containing waste liquid; (2) treatment of antimony-containing precipitation slag; and (3) mixing the antimony-deposited solution with a washing solution. The technological process is simple, the flue gas acid-making waste tail gas, the waste acid and the antimony-containing waste liquid are fully utilized, antimony precipitation and antimony-precipitated liquid recycling are performed through a three-stage treatment technology, zero emission of the antimony-containing waste liquid is achieved, meanwhile, harmless treatment of the acid-making tail gas, antimony precipitation of the antimony-containing waste liquid and comprehensive utilization of the antimony-precipitated liquid are truly achieved, and the method is suitable for industrial production. The antimony-containing waste liquid and waste gas treated by the method provided by the invention greatly reduce the pollution hazard to the surrounding environment, achieve the purposes of energy conservation, economy and environmental protection, and improve the economic benefits of enterprises.

Description

Technical Field

[0001] The invention belongs to the technical field of comprehensive resource utilization, and in particular relates to a method for treating acid production tail gas and waste acid using antimony-containing waste liquid to recover antimony. Background Art

[0002] Although over 120 antimony-bearing minerals have been discovered in the Earth's crust, only 10 contain more than 20 wt% antimony, suitable for industrial smelting under current conditions. These include stibnite (71.4 wt% Sb), stybauite (83.3 wt% Sb), antimony ochre (74-79 wt% Sb), stybauite (74.5 wt% Sb), pyroxenite (75.2 wt% Sb), native antimony (100 wt% Sb), pyroxenite (51.6 wt% Sb), pyroxenite (35.5 wt% Sb), and tetrahedrite (25 wt% Sb). Among these, stibnite is the primary raw material for antimony smelting.

[0003] Antimony-gold ore, a significant component of my country's antimony ore resources, is primarily distributed in southern and western my country. These ores are often associated with arsenopyrite and pyrite. The gold in the ore is primarily bound to metallic sulfides, and most of the gold is embedded in the stibnite, pyrite, and arsenopyrite in the form of microparticles. If a two-stage roasting and subsequent cyanidation process is used, the low-melting-point antimony oxide will encapsulate the gold and consume a certain amount of cyanide, resulting in low leaching rates and insufficient antimony content to meet pyrometallurgical smelting requirements. Currently, conventional methods for extracting gold from arsenic- and antimony-containing gold ores have low gold recovery rates.

[0004] Chinese invention patent CN104278154A discloses a method for pretreating antimony-containing gold concentrate, designed to improve gold and silver recovery. The process involves leaching antimony from the antimony-containing gold concentrate using a solution of Na2S and NaOH. After solid-liquid separation, the antimony-containing leachate and a gold concentrate filter cake are obtained. The antimony-containing leachate is then pH-adjusted to precipitate antimony to obtain an antimony concentrate. Lime milk is added to the filtrate after the precipitation to neutralize the regenerated NaOH. Sulfate ions in the filtrate form calcium sulfate precipitates for cement production. While this patent's technical solution utilizes H2SO4 to control the pH between 0 and 8 for antimony precipitation, it consumes sulfuric acid, resulting in high costs. Furthermore, the toxic hydrogen sulfide gas produced by the precipitated antimony is subjected to three-stage scrubbing and absorption using a NaOH solution, with negative pressure ventilation and a single-stage load. This makes the process complex and inevitably impacts the surrounding environment.

[0005] Chinese invention patent CN103937977A discloses a comprehensive recovery process for arsenic-antimony gold concentrate, comprising the following steps: 1) arsenic-antimony gold concentrate is first watered to form a slurry, which is then pre-alkaline leached with a leaching agent. The alkaline leachate is then reduced with a reducing agent to recover antimony; 2) the leached residue is washed and then subjected to a two-stage roasting process to recover arsenic and sulfur. The first stage is roasted at a temperature of 550-600°C to oxidize the arsenic in the mineral to As2O3, which is then recovered by wet arsenic recovery; the second stage is roasted at a temperature of 650°C to oxidize the sulfur in the mineral to SO2, which is then recovered by an acid production process; 3) the roasted residue is acid-leached and washed, then ground and leached with cyanide to recover gold. The technical solution of this invention patent involves reducing the alkaline leachate with a sulfuric acid reducing agent to recover antimony, and the claims specify a strict sulfuric acid dosage of 10 kg / t. The reduced solution formed after the reduction is returned to the alkaline leaching unit for recycling as the leachate. The technical solutions of the above two invention patents both use sulfuric acid as a reagent for precipitating antimony from antimony-containing waste liquid, and both have the problems of complex production processes, high costs, and impact on the surrounding environment.

[0006] The main alkaline leaching processes for antimony-containing minerals include pressurized alkaline leaching, sodium hydroxide alkaline leaching, sodium sulfide alkaline leaching, and alkaline leaching using a mixture of sodium hydroxide and sodium sulfide reagents. In the process of recovering antimony from antimony-containing wastewater, sulfuric acid, ferric chloride, hydrogen peroxide, and other reagents are often used as precipitation reagents. This not only results in large reagent usage and high processing costs, but also incomplete antimony precipitation. Furthermore, the discharge and treatment of the liquid after antimony precipitation requires a large amount of treatment costs. Therefore, the barren liquid after alkaline leaching and antimony precipitation is basically returned to the system for recycling. The accumulation of impurity ions formed during the recycling process, especially the presence of sulfate ions, has a serious impact on the leaching of antimony and the crystallization of production equipment and pipelines. Therefore, the antimony-containing wastewater must be treated in a process to meet emission standards before it can be discarded to avoid environmental pollution.

[0007] At the same time, the process of producing sulfuric acid from roasting flue gas produces a large amount of low-concentration waste acid (dilute acid) and flue gas exhaust, the main components of which are SO2 and SO3. Currently, low-concentration waste acid (dilute acid) is mainly treated separately by acid-base neutralization technology, while flue gas exhaust is mainly treated by electrostatic demisting technology. However, both the treatment of waste acid (dilute acid) and flue gas exhaust separately faces high costs and low comprehensive utilization value.

[0008] Therefore, it is particularly important to research and develop a technical solution that can utilize the advantages of existing resources to simultaneously solve the comprehensive recovery and utilization of antimony-containing waste liquid and the efficient purification and treatment of waste acid (dilute acid) and flue gas, so as to achieve the purpose of reducing costs and improving the comprehensive utilization of hazardous waste. Summary of the Invention

[0009] In view of the shortcomings of the above-mentioned prior art, the present invention provides a method for treating acid production tail gas and waste acid using antimony-containing waste liquid to recover antimony. The specific technical solution is as follows:

[0010] A method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid comprises the following steps:

[0011] (1) Primary treatment of antimony-containing waste liquid: The antimony-containing waste liquid is pumped to the top of an absorption tower and the acid production waste tail gas enters the bottom of the absorption tower, and the gas and liquid are countercurrently contacted and reacted fully. After the reaction, tail gas and a slurry containing precipitated solids are obtained, and the pH of the slurry is 3-4. The slurry is filtered to obtain an antimony-containing precipitated residue filter cake and an antimony-precipitated liquid;

[0012] (2) Treatment of antimony-containing precipitate residue: The filter cake of the antimony-containing precipitate residue is mixed with waste acid having a concentration of 1-3 wt%, stirred and washed, and filtered to obtain the antimony product and washing liquid;

[0013] (3) Mixing treatment of the antimony precipitation liquid and the washing liquid: The antimony precipitation liquid obtained in step (1) and the washing liquid obtained in step (2) are mixed and stirred, and sodium hydroxide is added to carry out neutralization reaction. After the reaction is completed, a final treated liquid with a pH of 7-8 is obtained.

[0014] The present invention utilizes acid production tail gas, waste acid (dilute acid) and antimony-containing waste liquid, and carries out antimony precipitation and reuse of the liquid after antimony precipitation through a three-stage treatment technology. The first-stage treatment technology is to carry out a neutralization reaction between the antimony-containing waste liquid and the acid production tail gas, to generate antimony precipitate during the reaction, and to filter and recover the antimony precipitate residue; the second-stage treatment technology is to wash the antimony precipitate residue with waste acid and filter to obtain high-quality antimony precipitate residue; the tertiary treatment technology is to use NaOH to adjust the pH of the liquid after the neutralization reaction to 7-8, thereby truly realizing the harmless treatment of the acid production tail gas, the precipitation of antimony in the antimony-containing waste liquid and comprehensive utilization.

[0015] Furthermore, in step (1), the antimony content of the antimony-containing waste liquid is 10-30 g / L, and the sodium content is 50-200 g / L.

[0016] Furthermore, in the step (1), the antimony-containing waste liquid is obtained by subjecting a mineral containing 0.5 to 1.5 wt% of antimony to an alkaline leaching process.

[0017] Furthermore, in step (1), the acid-producing tail gas is waste gas containing a total amount of SO2 and SO3 of 0.05-0.15v%.

[0018] Furthermore, in the step (1), the ratio of the liquid flow of the antimony-containing waste liquid to the gas flow of the acid-making waste tail gas is 1:(20-170).

[0019] Furthermore, in the step (2), the mass ratio of the antimony-containing precipitated residue filter cake to the waste acid with a concentration of 1-3 wt% is 1:1-5, and the stirring and washing time is 10-60 minutes.

[0020] Furthermore, in the step (3), the mixing and stirring speed is 20-30 rpm, and the total reaction time is 2-4 hours.

[0021] Furthermore, in step (1), the specific method for producing the antimony-containing waste liquid is as follows: adjusting the slurry concentration of a mineral containing 0.5-1.5 wt% antimony to 10-70 wt%, leaching with an alkaline reagent at a leaching temperature of 15-60° C. for 10-90 minutes, and filtering after leaching to obtain the antimony-containing waste liquid and leaching residue. The antimony-containing waste liquid can also be partially returned to the production system for recycling, and part can be sent to waste liquid treatment.

[0022] Furthermore, the alkaline reagent is sodium hydroxide, sodium sulfide or a mixed reagent of sodium hydroxide and sodium sulfide.

[0023] Furthermore, the alkaline reagent is a mixed reagent of sodium hydroxide and sodium sulfide, the amount of sodium hydroxide used is 10-100 kg / t antimony ore, and the amount of sodium sulfide used is 10-200 kg / t antimony ore.

[0024] Furthermore, the acid-making tail gas in step (1) and the waste acid in step (2) are derived from the roasting acid-making process of gold and silver concentrate, specifically: the gold and silver concentrate containing 15-50wt% sulfur and 100-1000g / t silver is adjusted to a pulp concentration of 50-70wt%, and roasted through the roasting acid-making process to produce roasted solid minerals, roasted flue gas and dust-containing flue gas; the roasted flue gas and dust-containing flue gas are subjected to SO2 purification, SO2 drying, two-stage SO2 conversion, and secondary absorption to produce 98wt% sulfuric acid product and acid-making tail gas containing a total amount of SO2+SO3 of 0.05-0.07v% and sulfuric acid waste acid (dilute acid) with a concentration of 1-3wt%.

[0025] Furthermore, the final treated liquid in step (2) is used in the slurry adjustment process of the roasting and acid-making process of gold and silver concentrates.

[0026] The final treated liquid is used to adjust the ore pulp in the roasting and acid-making process of gold and silver concentrates, which can achieve zero discharge of antimony-containing waste liquid and fully utilize the sodium ions in the liquid after antimony precipitation and the washing liquid, improve the silver recovery rate (sodium sulfate can be used as a roasting additive to improve the silver recovery rate), and realize the recycling of production liquid.

[0027] Furthermore, the roasted solid mineral is subjected to a gold and silver extraction process, specifically comprising the following steps: acid leaching and washing the solid mineral roasting residue obtained by roasting, followed by grinding, and the cyanide leaching process using soda ash to adjust the pH to 8-10, controlling the mass percentage concentration of sodium cyanide to 0.10-0.50%, the pulp concentration to 10-40wt%, the cyanidation time to 20-50 hours, the silver content of the cyanide residue to 10-50g / t, and the silver leaching rate to 80-95wt%.

[0028] Furthermore, in step (1), the tail gas is used in the roasting and acid-making process of gold and silver concentrates, and the small amount of hydrogen sulfide gas contained in the tail gas is fully utilized by generating sulfur dioxide during the roasting process.

[0029] The beneficial effects of the present invention are:

[0030] The present invention has a simple process flow and fully utilizes flue gas acidification waste gas, waste acid (dilute acid), and antimony-containing waste liquid. Antimony precipitation and subsequent liquid recycling are achieved through a three-stage treatment technology, achieving zero discharge of antimony-containing waste liquid. Simultaneously, the present invention truly achieves harmless treatment of acidification waste gas, antimony precipitation of antimony-containing waste liquid, and comprehensive utilization of the subsequent liquid. Furthermore, the cyanide-containing lean liquid and waste gas treated by the present invention significantly reduce pollution hazards to the surrounding environment, achieving the goals of energy conservation, economic development, and environmental protection, and improving the economic benefits of the enterprise. DETAILED DESCRIPTION

[0031] The principles and features of the present invention are described below in conjunction with embodiments. The examples given are only used to explain the present invention and are not used to limit the scope of the present invention.

[0032] Example 1:

[0033] A method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid comprises the following steps:

[0034] 1) Slurry roasting, generation of acid-making tail gas and waste acid: A gold-silver concentrate containing 15wt% sulfur and 100g / t silver is adjusted to a slurry concentration of 50wt%. The roasted solid mineral is produced through a roasting and acid-making process. The roasting flue gas and dust-containing flue gas are subjected to SO2 purification, SO2 drying, two-stage SO2 conversion, and two-stage absorption to produce 98wt% sulfuric acid product and acid-making tail gas containing a total of 0.08v% SO2+SO3 and waste acid (dilute acid) with a sulfuric acid concentration of 1wt%. The acid-making tail gas enters the tail gas absorption system, and the waste acid (dilute acid) enters the dilute acid storage tank;

[0035] 2) Generation of antimony-containing waste liquid: A mineral containing 0.5 wt% antimony is subjected to an alkaline leaching process, with a leached slurry concentration of 10 wt%. The alkaline reagent is a mixture of sodium hydroxide and sodium sulfide, with a sodium hydroxide dosage of 10 kg / t of antimony ore and a sodium sulfide dosage of 10 kg / t of antimony ore. The leaching temperature is 15° C., and the leaching time is 10 minutes. After the leaching is completed, the antimony-containing waste liquid and leaching residue are filtered to obtain the antimony content of the antimony-containing waste liquid and the leaching residue. The antimony content of the antimony-containing waste liquid is 20 g / L and the sodium content is 50 g / L. Part of the antimony-containing waste liquid is returned to the production system for utilization, and part is subjected to primary treatment of the antimony-containing waste liquid.

[0036] 3) Primary treatment of antimony-containing waste liquid: The antimony-containing waste liquid is pumped to the top of the absorption tower and the acid waste gas enters the bottom of the absorption tower. The gas and liquid are countercurrently contacted and reacted fully. The liquid flow rate is 1m 3 / h, gas flow rate is 100m 3 / h, after the reaction, tail gas and a slurry with a pH of 3 containing precipitated solids are obtained, and the tail gas is transported to the roasting acid-making process through a fan. The small amount of hydrogen sulfide gas contained in the tail gas is fully utilized by generating sulfur dioxide during the roasting process. After filtering, the slurry is obtained to obtain a precipitated residue filter cake containing 30wt% antimony and a liquid after precipitation of antimony;

[0037] 4) Treatment of antimony-containing precipitate residue: The filter cake of the antimony-containing precipitate residue was mixed with waste acid (dilute acid) having a concentration of 1 wt% sulfuric acid at a mass ratio of 1:1 for 10 minutes, and filtered to obtain an antimony product containing 40 wt% antimony and a washing liquid. The antimony product was sold to an antimony refinery;

[0038] 5) Mixing treatment of the antimony precipitation liquid and the washing liquid: The antimony precipitation liquid and the washing liquid are mixed and fed into two series-connected stirring reaction tanks at a stirring speed of 20 rpm and a total reaction time of 2 hours. Sodium hydroxide is added to each stirring tank for neutralization reaction, and the pH is controlled to 7. After the reaction is completed, the final treated liquid is obtained and applied to the roasting and slurrying process to fully utilize the sodium ions in the antimony precipitation liquid and the washing liquid, and realize the production recycling of the liquid;

[0039] 6) Gold and silver extraction process of roasted solid minerals: The roasted solid mineral slag obtained in step 1) is subjected to acid leaching and washing, and then ground. In the cyanide leaching process, soda ash is used to adjust the pH to 8, the sodium cyanide concentration is controlled to 0.10wt%, the slurry concentration is 10wt%, the cyanidation time is 20 hours, the silver content of the cyanide slag is 10g / t, and the silver leaching rate reaches 90%.

[0040] Example 2:

[0041] A method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid comprises the following steps:

[0042] 1) Slurry preparation, roasting, generation of acid-making tail gas and waste acid: A gold-silver concentrate containing 30 wt% sulfur and 520 g / t silver is added to the final treated liquid of step 5) to prepare a slurry concentration of 62 wt%. The roasting flue gas and dust-containing flue gas are roasted through a roasting and acid-making process. After SO2 purification, SO2 drying, SO2 conversion twice, and two-stage absorption, 98 wt% sulfuric acid product, acid-making tail gas containing a total of 0.10 v% SO2 + SO3, and waste acid (dilute acid) with a sulfuric acid concentration of 2 wt% are produced. The acid-making tail gas enters the tail gas absorption system, and the waste acid (dilute acid) enters the dilute acid storage tank.

[0043] 2) Generation of antimony-containing waste liquid: A mineral containing 1.5 wt% antimony is subjected to an alkaline leaching process, with a leached slurry concentration of 30 wt%. The alkaline reagent is a mixture of sodium hydroxide and sodium sulfide, with a sodium hydroxide dosage of 20 kg / t antimony mineral and a sodium sulfide dosage of 50 kg / t antimony mineral. The leaching temperature is 30° C., and the leaching time is 30 minutes. After the leaching is completed, the antimony-containing waste liquid and the leaching residue are filtered. The antimony content of the antimony-containing waste liquid is 50 g / L, and the sodium content is 100 g / L.

[0044] 3) Primary treatment of antimony-containing waste liquid: The antimony-containing waste liquid is pumped to the top of the absorption tower and the acid waste gas enters the bottom of the absorption tower. The gas and liquid are countercurrently contacted and reacted fully. The liquid flow rate is 2m 3 / h, gas flow rate is 120m 3 / h, after the reaction, tail gas and a slurry with a pH of 3 containing precipitated solids are obtained, and the tail gas is transported to the roasting acid-making process through a fan. The small amount of hydrogen sulfide gas contained in the tail gas is fully utilized by generating sulfur dioxide during the roasting process. After filtering, the slurry is obtained to obtain a precipitated residue filter cake containing 35wt% antimony and a liquid after precipitation of antimony;

[0045] 4) Treatment of antimony-containing precipitate residue: The filter cake of the antimony-containing precipitate residue was mixed with waste acid (dilute acid) having a concentration of 1 wt% sulfuric acid in a ratio of 1:3 by mass for 30 minutes. The mixture was filtered to obtain an antimony product containing 50 wt% antimony and a washing liquid. The antimony product was sold to an antimony refinery.

[0046] 5) Mixing treatment of the antimony precipitation liquid and the washing liquid: The antimony precipitation liquid and the washing liquid are mixed and fed into two series-connected stirring reaction tanks at a stirring speed of 30 rpm and a total reaction time of 3 hours. Sodium hydroxide is added to each stirring tank for neutralization reaction, and the pH is controlled to be 7.5. After the reaction is completed, the final treated liquid is obtained and applied to the roasting and slurrying process to fully utilize the sodium ions in the antimony precipitation liquid and the washing liquid, and realize the production recycling of the liquid.

[0047] 6) Gold and silver extraction process from roasted solid minerals: The roasted solid mineral slag obtained in step 1) is subjected to acid leaching and washing, and then ground. In the cyanide leaching process, soda ash is used to adjust the pH to 8, the sodium cyanide concentration is controlled to 0.30wt%, the slurry concentration is 30wt%, the cyanidation time is 30 hours, the cyanide slag contains 62g / t of silver, and the silver leaching rate reaches 88%.

[0048] Example 3:

[0049] A method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid comprises the following steps:

[0050] 1) Slurry preparation, roasting, acid production tail gas and waste acid generation: A gold and silver concentrate containing 50wt% sulfur and 1000g / t silver is added to the final treated liquid of step 5) to adjust the slurry concentration to 70wt%. The roasting flue gas and dust-containing flue gas are roasted through the roasting and acid production process. After SO2 purification, SO2 drying, SO2 conversion twice, and secondary absorption, 98wt% sulfuric acid product and acid production tail gas containing a total of 0.12v% SO2+SO3 and waste acid (dilute acid) with a sulfuric acid concentration of 2wt% are produced. The acid production tail gas enters the tail gas absorption system, and the waste acid (dilute acid) enters the dilute acid storage tank. The solid mineral obtained by roasting enters the gold and silver extraction process.

[0051] 2) Generation of antimony-containing waste liquid: A mineral containing 1.5 wt% antimony is subjected to an alkaline leaching process with a leached slurry concentration of 70 wt%, an alkaline reagent sodium hydroxide dosage of 100 kg / t antimony mineral, a sodium sulfide dosage of 200 kg / t antimony mineral, a leaching temperature of 60° C., and a leaching time of 90 minutes. After the leaching is completed, the antimony-containing waste liquid and a leaching residue are filtered to obtain an antimony content of 100 g / L and a sodium content of 200 g / L.

[0052] 3) Primary treatment of antimony-containing waste liquid: The antimony-containing waste liquid is pumped to the top of the absorption tower and enters the bottom of the absorption tower with the acid production waste gas. The gas and liquid are countercurrently contacted and reacted fully. The liquid flow rate is 4.9m 3 / h, gas flow rate is 170m 3 / h, after the reaction, tail gas and a slurry with a pH of 4 containing precipitated solids are obtained, and the tail gas is transported to the roasting acid-making process through a fan. The small amount of hydrogen sulfide gas contained in the tail gas is fully utilized by generating sulfur dioxide during the roasting process. After filtering, the slurry is obtained to obtain a precipitated residue filter cake containing 40wt% antimony and a liquid after antimony precipitation;

[0053] 4) Treatment of antimony-containing precipitate residue: The filter cake of the antimony-containing precipitate residue was mixed with waste acid (dilute acid) having a concentration of 3 wt% sulfuric acid at a mass ratio of 1:5 for 60 minutes, and filtered to obtain an antimony product containing 60 wt% antimony and a washing liquid. The antimony product was sold to an antimony refinery;

[0054] 5) Mixing treatment of the antimony precipitation liquid and the washing liquid: The antimony precipitation liquid and the washing liquid are mixed and fed into two series-connected stirring reaction tanks at a stirring speed of 30 rpm and a total reaction time of 4 hours. Sodium hydroxide is added to each stirring tank for neutralization reaction, and the pH is controlled at 8. After the reaction is completed, the final treated liquid is obtained and applied to the roasting and slurrying process to fully utilize the sodium ions in the antimony precipitation liquid and the washing liquid, and realize the production recycling of the liquid;

[0055] 6) Gold and silver extraction process from roasted solid minerals: The roasted solid mineral slag obtained in step 1) is subjected to acid leaching and washing, and then ground. In the cyanide leaching process, soda ash is used to adjust the pH to 10, the sodium cyanide concentration is controlled to 0.50 wt%, the slurry concentration is 40 wt%, the cyanidation time is 50 hours, the silver content of the cyanide slag is 50 g / t, and the silver leaching rate reaches 95%.

[0056] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A method for recovering antimony by treating acid production tail gas and waste acid using antimony-containing waste liquid, characterized in that: The steps include: (1) Primary treatment of antimony-containing waste liquid: the antimony-containing waste liquid is sent to the top of the absorption tower, and the acid production waste tail gas enters the bottom of the absorption tower. The gas and liquid are countercurrently contacted and reacted fully. After the reaction, tail gas and slurry containing precipitated solids are obtained. The pH of the slurry is 3-4. The slurry is filtered to obtain antimony-containing precipitated residue filter cake and antimony-precipitated liquid; (2) Treatment of antimony-containing precipitate residue: The filter cake of the antimony-containing precipitate residue is mixed, stirred and washed with waste acid having a concentration of 1-3 wt%, and filtered to obtain an antimony product and a washing liquid; (3) Mixing treatment of the antimony precipitation liquid and the washing liquid: The antimony precipitation liquid obtained in step (1) and the washing liquid obtained in step (2) are mixed and stirred, and sodium hydroxide is added to carry out neutralization reaction. After the reaction is completed, a final treated liquid with a pH of 7-8 is obtained.

2. The method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid according to claim 1, characterized in that: In the step (1), the antimony content of the antimony-containing waste liquid is 10-30 g / L, and the sodium content is 50-200 g / L.

3. The method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid according to claim 1, characterized in that: In the step (1), the acid-producing tail gas is waste gas containing a total amount of SO2 and SO3 of 0.05-0.15v%.

4. The method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid according to claim 1, characterized in that: In the step (1), the ratio of the liquid flow rate of the antimony-containing waste liquid to the gas flow rate of the acid-making waste tail gas is 1:(20-170).

5. The method for recovering antimony by treating acid-making tail gas and waste acid using antimony-containing waste liquid according to claim 1, characterized in that: In the step (2), the mass ratio of the antimony-containing precipitated slag filter cake to the waste acid with a concentration of 1-3 wt% is 1:1-5, and the stirring and washing time is 10-60 minutes.

6. The method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid according to claim 1, characterized in that: In the step (3), the rotation speed of the mixing and stirring is 20-30 rpm, and the total reaction time is 2-4 hours.

7. The method for recovering antimony by treating acid-making tail gas and waste acid using antimony-containing waste liquid according to claim 2, characterized in that: In the step (1), the antimony-containing waste liquid is obtained by subjecting a mineral containing 0.5-1.5 wt% of antimony to an alkaline leaching treatment process.

8. The method for recovering antimony by treating acid-making tail gas and waste acid using antimony-containing waste liquid according to claim 1, characterized in that: The acid-making tail gas in step (1) and the waste acid in step (2) are derived from the acid-making process of roasting gold and silver concentrates.

9. The method for treating acid production tail gas and waste acid to recover antimony by utilizing antimony-containing waste liquid according to claim 8, characterized in that: The final treated liquid in step (2) is used in the slurry adjustment process of the roasting and acid-making process of the gold and silver concentrate.

10. The method for recovering antimony by treating acid-making tail gas and waste acid using antimony-containing waste liquid according to claim 1, characterized in that: In the step (1), the tail gas is used in the roasting and acid-making process of gold and silver concentrate.