WO2017113882A1 - 污酸资源回收与深度处理方法及装置 - Google Patents

污酸资源回收与深度处理方法及装置 Download PDF

Info

Publication number
WO2017113882A1
WO2017113882A1 PCT/CN2016/098594 CN2016098594W WO2017113882A1 WO 2017113882 A1 WO2017113882 A1 WO 2017113882A1 CN 2016098594 W CN2016098594 W CN 2016098594W WO 2017113882 A1 WO2017113882 A1 WO 2017113882A1
Authority
WO
WIPO (PCT)
Prior art keywords
arsenic
acid
copper
sulfide
slag
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2016/098594
Other languages
English (en)
French (fr)
Inventor
柴立元
王庆伟
蒋国民
周成赟
李青竹
杨志辉
高伟荣
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Central South University
Original Assignee
Central South University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Central South University filed Critical Central South University
Priority to US16/066,902 priority Critical patent/US10662075B2/en
Publication of WO2017113882A1 publication Critical patent/WO2017113882A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/10—Vacuum distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/145—One step being separation by permeation
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0084—Treating solutions
    • C22B15/0089—Treating solutions by chemical methods
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B61/00—Obtaining metals not elsewhere provided for in this subclass
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/046—Treatment of water, waste water, or sewage by heating by distillation or evaporation under vacuum produced by a barometric column
    • 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
    • C02F1/048—Purification of waste water by 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
    • C02F1/26—Treatment of water, waste water, or sewage by extraction
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • 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
    • C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
    • 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
    • C02F2101/101—Sulfur compounds
    • 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
    • C02F2101/103—Arsenic compounds
    • 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
    • C02F2101/106—Selenium compounds
    • 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
    • C02F2101/12—Halogens or halogen-containing compounds
    • C02F2101/14—Fluorine or fluorine-containing compounds
    • 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
    • C02F2101/20—Heavy metals or heavy metal compounds
    • C02F2101/203—Iron or iron compound
    • 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
    • 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
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the invention relates to a method and a device for recycling and deep processing of a sewage acid resource, belonging to the field of metallurgical chemical environmental protection.
  • it relates to a method and a device for recovering and deepening the flue gas scrubbing acid resource of a sulfuric acid system for color smelting.
  • the pollutants have the highest arsenic concentration and the greatest harm, and also contain heavy metal ions such as lead, cadmium, zinc and copper; mercury and arsenic in the sulphuric acid wastewater produced by lead and zinc smelting
  • heavy metal ions such as lead, cadmium, zinc and copper
  • the anions are mainly fluorine and chloride ions.
  • Sewage acid wastewater has the characteristics of complex composition, high concentration of heavy metals, large fluctuation, complex form of heavy metals and high acidity. It is a difficult point in the treatment of heavy metal wastewater in nonferrous smelting enterprises.
  • domestic methods for treating sulphuric acid wastewater mainly include neutralization method, vulcanization method - neutralization method, neutralization - Iron salt co-precipitation, membrane technology treatment and other methods, but they all have their own defects, and the treatment effect is not satisfactory.
  • the neutralization method has lower processing cost, but the amount of slag is large, and it is difficult to achieve stable compliance after wastewater treatment; the sulfide neutralization method reduces the amount of slag compared with the neutralization precipitation method, but there is still a large amount of neutralized slag, and
  • Neutralization iron salt precipitation method is widely used.
  • the main problems are the large amount of slag generated, the lack of effective use of resources, the high disposal cost of the later slag, and the risk of secondary environmental pollution.
  • the membrane technology can be applied to the treatment of sewage acid wastewater. Low consumption, small footprint, relatively low cost, etc. The hot spot of research in the year. Recovery of the acid in the wastewater by a selective ion exchange membrane facilitates subsequent further processing of heavy metals in the wastewater.
  • the methods for treating heavy metal wastewater by membrane technology mainly include diffusion dialysis, electrodialysis, and nanofiltration.
  • Patent( 201310501529.7 The method and device for recycling heavy metal sewage acid wastewater disclose a method for recovering waste acid by electrodialysis and heavy metal vulcanization device, which mainly has problems of low acid recovery, fluorine and chloride ions in the recovered acid, and reuse of acid; ( 201410786969.6
  • a method for smelting and smelting acid purification discloses a method for purifying sulphuric acid by diffusion dialysis and ion exchange and multi-effect evaporation. Although the problem of low acidity recovery is solved, a large amount of new water needs to be added during the diffusion dialysis process, and the pollution is increased.
  • the invention aims at the problems existing in the prior process of the sewage acid treatment process, and proposes a method and a device for deep recovery of valuable elements in the waste water wastewater and separate opening of harmful elements, and solves the problem of price in the process of the sewage acid treatment. Resources cannot be recovered, the amount of slag is large, and there are secondary pollution problems.
  • a method for recycling and deep processing of a dirty acid resource comprising the following steps:
  • the sewage wastewater first filters the suspended matter through a precision filter, and then enters the selective adsorption tank to selectively adsorb the rare metal including strontium and selenium;
  • the electrodialysis equipment concentrate enters the evaporation concentration device to continue acid concentration, and evaporates the condensed water for reuse;
  • the method for recycling and deep processing of the sulphuric acid resource of the present invention may further include the following steps:
  • the sewage wastewater first filters the suspended matter through a precision filter, and then enters the selective adsorption tank to selectively adsorb the rare metal including strontium and selenium;
  • the filtrate is deeply desulfurized by a vulcanizing agent, and the obtained arsenic sulfide is returned to the step (2).
  • the arsenic sulfide slag used in the first separation of copper arsenic is derived from the arsenic sulfide slag obtained by the smelting enterprise by adding sulfide to the dirty acid or electrolytic waste liquid.
  • arsenic slag electrolytic waste arsenic slag and so on.
  • the sewage acid wastewater is an acidic wastewater generated by the flue gas generated by the smelting of non-ferrous metals in the acid purification process, and the concentration of sulfuric acid in the contaminated acid is 2%-8%.
  • concentration of sulfuric acid in the contaminated acid is 2%-8%.
  • Step (1) The pore size of the filter material during precision filtration is 0.5-10 ⁇ m.
  • Step (1) The selective adsorption tank is filled with a selective adsorption filler, which is a nitrogen heterocyclic compound functionalized ion exchange material.
  • a selective adsorption filler which is a nitrogen heterocyclic compound functionalized ion exchange material.
  • the preparation method is first to carry out a polymer such as polypropylene-styrene or styrene-divinylbenzene.
  • the chloromethylation reaction is carried out by immersing the reaction product in a solution containing a functional monomer of a heterocyclic compound, and the reaction product is dried to obtain a reaction product.
  • Step (2) When the copper and arsenic are separated, the arsenic sulfide or the sulfide residue is 1-5:1 according to the As/Cu molar ratio. The proportion is added to (after treatment with the adsorption tank) the sewage acid wastewater. The reaction is carried out at 40-80 ° C for 1-3 h, and after filtration, copper-rich slag (i.e., copper sulfide slag) and an arsenic-rich solution (i.e., copper removal filtrate) are obtained.
  • copper-rich slag i.e., copper sulfide slag
  • an arsenic-rich solution i.e., copper removal filtrate
  • the vulcanizing agent used is one or more of sodium sulfide, sodium hydrosulfide, calcium sulfide, barium sulfide, and hydrogen sulfide.
  • the hydrogen sulfide used may be produced by reacting sulfide or sulfuric acid or sulfur or one or more of hydrogen, methanol, natural gas, and coke oven gas.
  • Step 4 The electrodialysis equipment adopts a splint type or a coil type, and the membrane used is a non-polluting and corrosion-resistant homogeneous ion exchange membrane or a bipolar membrane, and the power source used is an inverted pole or a frequent reverse polarity method, and the preconcentration is a sulfuric acid mass fraction. Concentrate to 10 ⁇ 20%.
  • the evaporative concentration device of step (5) is concentrated by two-effect or three-effect evaporation or membrane distillation, and the acid is concentrated from 10 to 20% of the acid having a sulfuric acid mass fraction of 30 to 60%, and the second or third effect evaporation evaporation chamber
  • the heat exchanger adopts one or several kinds of graphite, PP, PVDF, PTFE
  • the membrane distillation running temperature is 60-90 °C
  • the vacuum is realized by a water circulation vacuum pump or a plunger vacuum pump, and the running vacuum is -0.05--0.09 MPa
  • the membrane module is operated by submerged vacuum membrane distillation or multi-effect membrane distillation
  • membrane distillation filter pore size is 0.2-0.5 ⁇ m
  • flux is 3-5 L/m 2 .
  • Step (6) evaporating to obtain a fluorine-containing chlorine concentrated acid solution, removing fluorine chlorine by a blow-off analytical method, and obtaining a fluorochloro mixed acid, wherein the hot air stripping temperature is At 110-120 °C, the stripping time is 1-2 h.
  • the device matched with the above-mentioned sewage acid resource recovery and deep treatment method is formed by sequentially connecting a precision filter, a selective adsorption tank, a copper-arsenic separation device, a vulcanization device, an electrodialysis device, an evaporation concentration device, and a stripping device.
  • the selective adsorption method is used to adsorb and accumulate rare metal ions from the sewage acid wastewater, and the high value-added components in the waste acid are fully recovered in a relatively simple manner, and a high concentration of the enriched solution is obtained without bringing the solution. Secondary pollution is conducive to the subsequent treatment and utilization of waste acid.
  • the sewage wastewater is often treated by lime neutralization and vulcanization, which produces a large amount of sulfide arsenic slag (also known as arsenic filter cake).
  • sulfide arsenic slag also known as arsenic filter cake.
  • the elements such as copper, arsenic and sulfur are hazardous wastes, and the separation of copper and arsenic is difficult.
  • Alkali leaching is often used to recover valuable metals in arsenic filter cakes, but the consumption of alkali is large.
  • the subsequent treatment of arsenic-containing strong alkali solution is still a problem.
  • the pressure oxidative leaching method has the leaching rate of copper and arsenic. More than 90%, but there are problems with high equipment requirements and high cost.
  • the inventor was surprised to find out if The filtrate after separation of copper and arsenic removes arsenic by a vulcanizing agent, and the obtained arsenic sulfide is returned to copper and arsenic separation.
  • the leaching separation has the following advantages: high-efficiency separation of copper and arsenic is achieved during the treatment of the sulphuric acid, and high-grade copper sulphide slag is obtained at the same time, thereby avoiding a large amount of arsenic filter cake.
  • the recovery of copper is guaranteed, which provides conditions for the deep purification of arsenic.
  • the method of combining electrodialysis and evaporation is used for the treatment of sewage acid wastewater, which minimizes the running cost.
  • the pre-concentration is carried out by electrodialysis under the condition of lower acid concentration, at a higher acid concentration condition. Concentration is continued with multi-effect evaporation or membrane distillation.
  • the enrichment of chlorofluorocarbon by membrane distillation technology and evaporation concentration provides conditions for the separation of chlorofluorocarbon.
  • the separation of chlorofluorochloride by the stripping analytical method and further concentration of the acid can obtain a higher concentration of fluorochloric acid and low fluorosulfuric acid. Sulfuric acid can be returned to the system for use, and chlorohydrate can be opened from the system.
  • the invention can realize the resource utilization and recycling of the sewage acid wastewater, can fully recover the rare metal, realize the high-efficiency separation of copper and arsenic, deep purification of arsenic in the contaminated acid, recover high-grade copper slag, separately open the arsenic slag; Enrichment and openness, concentration and reuse of sulfuric acid.
  • the process purification is efficient, the comprehensive resource recovery effect is good, the impact load is strong, the treatment cost is low, the amount of arsenic slag is small, the risk of secondary pollution is small, and the economic and environmental benefits are good.
  • Figure 1 is a process flow diagram of the present invention
  • Figure 2 is a device diagram of the present invention
  • 1 is a precision filter
  • 2 is a selective adsorption tank
  • 3 is a copper-arsenic separation equipment
  • 4 is a vulcanization equipment
  • 5 is an electrodialysis equipment
  • 7 is the blowing off equipment.
  • the invention firstly filters the suspended sewage through the precision filter 1 and then enters the selective adsorption tank 2 Selective adsorption of rare metals including antimony and selenium; reuse of arsenic sulfide or arsenic sulfide slag in copper and arsenic separation equipment 3 for copper and arsenic separation; copper and arsenic separation after filtration in vulcanization equipment 4
  • the vulcanizing agent is used to remove arsenic in depth, and the obtained arsenic sulfide slag is reused for copper and arsenic separation; after separating the arsenic slag, the filtrate enters the electrodialysis device 5 preconcentrates the acid and separates and concentrates the fluorine and chlorine; the electrodialysis equipment concentrate enters the evaporation concentration device 6 Continue to carry out acid concentration, evaporate the condensed water for reuse; after evaporation and concentration, the acid is stripped off the device 7 to remove the fluorine and chlorine, and the
  • the first sulphide sulphide slag is obtained by adding sulphide to the sulphuric acid to vulcanize most of the copper and arsenic in the sulphuric acid to obtain a mixed slag of copper sulphide and arsenic sulfide.
  • the partially mixed slag is proportionally added to the unvulcanized slag.
  • the arsenic sulfide in the mixed slag is used to replace the copper in the sulphuric acid to form copper slag, to obtain a copper-rich slag and an arsenic-rich solution with higher grade, and then to precipitate the arsenic-rich sulphide by using a sulphide-precipitated arsenic sulphide.
  • Slag can be used in the steps of the process of the invention 2 copper displacement separation process.
  • the smelting waste water of a smelting enterprise is homogenized by water quality, and the granules and colloidal impurities are removed through a precision filter (the filter material is an organic porous material PP, the pore size is 10 ⁇ m, and the filter form is a bag filter), and then enters the selective adsorption tank.
  • the effluent from the sorbent tank is added with arsenic sulfide slag according to the ratio of As/Cu 2:1, and reacted at 80 °C for 1.5h to separate copper arsenic.
  • the copper slag (copper sulphide slag) and arsenic-rich solution are obtained by filtration, according to hydrogen sulfide.
  • the current density is 40 mA/cm 2
  • the high-fluorine-chloride high acid liquid (dope) and the low-fluorine chlorine low-acid wastewater (light liquid, large Part of the water and a small amount of heavy metals)
  • high-fluorine-chlorine high-acid wastewater is concentrated by three-effect evaporation, the acid is concentrated to 50%, and the low-fluorine condensate can be reused.
  • the concentrated acid was removed by hot air stripping, and the hot air stripping temperature was 120 °C, and the stripping time was 2 h.
  • the sulfuric acid can be returned to the smelting system for reuse.
  • the fluorine chlorine is removed, the gas is condensed and absorbed to obtain a high-fluorine-chlorine mixed acid, and the hydrofluoric acid and hydrochloric acid can be separated and reused as a by-product.
  • the recovery rate of ruthenium in the wastewater can reach more than 95%, and the adsorption rate of arsenic is less than 1%. It can achieve efficient separation of bismuth and arsenic.
  • the copper recovery rate is greater than 99% after separation of copper and arsenic, and the copper grade in the copper sulfide slag is 58% and the arsenic content is 3.2%.
  • the arsenic removal rate of the arsenic-rich solution after the vulcanization reaction is 99.9%, the arsenic content in the solution is 0.3 mg/L, and the arsenic content in the arsenic slag is 55%.
  • the acid After preconcentration separation by electrodialysis, the acid is concentrated from 3% to 12%, while the separation rate of chlorofluorocarbon is 85% and 90% respectively; the concentration of acid is concentrated from 12% to 50% by concentrated acid evaporation by three-effect evaporation, and the acidity can reach 70% after removal by chlorofluorocarbon removal.
  • the content of chlorofluorochloride in the acid is 150mg/L and 120mg/L, respectively, and the concentration of chlorofluoro in the chlorofluoro mixed acid solution can reach 30g/L.
  • sulfuric acid after removing fluorine chlorine, sulfuric acid can be returned to the processes of electrolysis and acid production, and the resources are utilized to the maximum, and the goal of recycling waste water wastewater is realized.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Molecular Biology (AREA)
  • Electrochemistry (AREA)
  • Medicinal Chemistry (AREA)

Abstract

一种污酸资源回收与深度处理方法及装置，该方法的主要步骤如下，(1)选择性吸附铼和硒等稀贵金属；(2)铜砷分离回收铜；(3)高效硫化深度除砷；(4)电渗析预浓缩酸；(5)蒸发浓缩酸；(6)吹脱法除氟氯。污酸处理装置主要包括精密过滤罐、选择性吸附罐、铜砷分离设备、硫化设备、电渗析设备、蒸发浓缩设备及吹脱设备。该方法及装置可以实现污酸废水中价元素的高效回收及有害元素的单独开路，经济、社会和环境效益明显，具有广阔的应用前景。

Description

污酸资源回收与深度处理方法及装置
技术领域
本发明涉及一种污酸资源回收与深度处理方法及装置，属于冶金化工环保领域。特别是涉及一种有色冶炼制硫酸系统烟气洗涤污酸资源回收与深度处理方法及装置。
背景技术
中国是有色金属生产大国，有色金属产量连续 11 年位居世界第一位。有色金属的冶炼过程产生大量夹杂铅、砷、汞等重金属烟尘的 SO2 烟气，烟气在制硫酸过程中采用湿法除杂会产生大量的酸性废水，即为有色重金属冶炼烟气洗涤污酸废水。铜、镍、黄金冶炼产生的污酸废水中，污染物以砷浓度最高、危害最大，同时还含有铅、镉、锌、铜等重金属离子；铅锌冶炼产生的污酸废水中以汞和砷为主要污染物，还含有高浓度的锌和铅，阴离子主要为氟、氯离子。污酸废水具有成分复杂、重金属浓度高、波动大、重金属形态复杂及酸度高等特点，是目前有色冶炼企业重金属废水处理的难点。
目前国内处理污酸废水的方法主要有中和法、硫化法 - 中和法、中和 - 铁盐共沉淀、膜技术处理等方法，但都存在各自的缺陷，而且处理效果不理想。其中中和法处理成本较低，但产生渣量大、废水处理后难以稳定达标；硫化中和法，相比中和沉淀法虽然减少了渣量，但任然存在大量的中和渣，且处理过程中钙和钠离子等进入系统造成硬度高、盐分累积，不利于废水回用。中和铁盐沉淀法，应用较普遍，主要存在问题为产生渣量大、资源没有有效利用，后期渣的处置费用高，有二次环境污染风险等；膜技术应用于污酸废水处理具有能耗低、占地面积小、成本相对较低等特点，已成为近几 年研究的热点。通过具有选择性的离子交换膜回收废水中的酸，有利于后续进一步处理废水中的重金属。通过膜技术处理重金属废水的方法主要有扩散渗析、电渗析、纳滤等方法。专利（ 201310501529.7 ）重金属污酸废水资源化回收方法及装置公开了采用电渗析和重金属硫化装置回收废酸的方法，主要存在回收酸度低，回收酸中含有氟、氯离子限制了酸的回用等问题；专利（ 201410786969.6 ）一种冶炼污酸净化的方法公开了采用扩散渗析和离子交换、多效蒸发净化污酸的方法，虽然解决了回收酸度低的问题，但是扩散渗析过程中需要补充大量新水，增加了污酸的处理量，低酸含氟氯及重金属的废水仍然需要中和处理，不利于回用。 因此，开发一种高效的冶炼烟气洗涤污酸废水循环利用新工艺是我国有色行业环境治理领域的重要课题。
发明内容
本发明针对现有方法污酸废水处理过程中存在的问题，提出了一种污酸废水中有价元素的深度回收及有害元素的单独开路的方法及装置，解决了污酸处理过程中有价资源无法回收、渣量大、存在二次污染等难题。
一种污酸资源回收与深度处理方法，包括以下步骤：
（ 1 ）预处理与选择性吸附，污酸废水先通过精密过滤器过滤悬浮物，然后进入选择性吸附罐选择性吸附包括铼和硒在内的稀贵金属；
（ 2 ）再利用硫化砷或者硫化砷渣进行铜砷分离；
（ 3 ）铜砷分离后滤液采用硫化剂深度除砷，得到的硫化砷渣回用于步骤（ 2 ）；
（ 4 ）分离砷渣后滤液进入电渗析设备预浓缩酸并分离富集氟氯；
（ 5 ）电渗析设备浓缩液进入蒸发浓缩设备继续进行酸浓缩，蒸发冷凝水回用；
（ 6 ）蒸发浓缩后的酸液采用吹脱析出法除氟氯后回用于工艺或硫酸制酸系统，高浓度氟氯混酸外售或进一步资源化。
本发明的一种污酸资源回收与深度处理方法，其方案还可以包括以下步骤：
（ 1 ）预处理与选择性吸附，污酸废水先通过精密过滤器过滤悬浮物，然后进入选择性吸附罐选择性吸附包括铼和硒在内的稀贵金属；
（ 2 ）再利用硫化砷渣进行铜砷分离；
（ 3 ）铜砷分离后滤液采用硫化剂深度除砷，得到的硫化砷渣回用于步骤（ 2 ）。
步骤（ 2 ）中，在对铜砷进行首次分离时采用的硫化砷渣来源于治炼企业用向污酸或电解废液中投加硫化物所得的硫化砷渣。如污酸砷渣、电解废液砷渣等。
步骤（ 1 ）所述的污酸废水是有色金属冶炼产生的烟气在制酸净化工艺过程中产生的酸性废水，污酸中硫酸质量浓度在 2%-8% 之间，含有铜、铅、锌、镉、砷、镍、钴、锰、锡、锑、硒、汞、铟、铼离子中的一种或几种，以及氟、氯、硫酸根和氢离子。
步骤（ 1 ）精密过滤时过滤材料的孔径为 0.5-10μm 。
步骤（ 1 ） 选择性吸附罐内填充选择性吸附填 料，该填料为氮杂环化合物功能化离子交换材料。其 制备方法是首先将聚丙烯 - 苯乙烯或 苯乙烯 - 二乙烯苯等聚合物进行 Blanc 氯甲基化反应，然后将反应产物浸泡在含杂环化合物功能单体的溶液中反应，反应产物经干燥后，即得。
步骤（ 2 ）铜砷分离时硫化砷或者 硫化渣按照 As/Cu 摩尔比为 1-5:1 的比例加入至（经吸附罐处理后）污酸废水中。在 40-80 ℃ 下反应 1-3h ，过滤后得到富铜渣（即硫化铜渣）和富砷溶液（即除铜滤液）。
步骤（ 3 ）所采用硫化剂为硫化钠、硫氢化钠、硫化钙、硫化钡、硫化氢中的一种或几种。所采用硫化氢可采用硫化物和硫酸制得或硫磺和氢气、甲醇、天然气、焦炉煤气中一种或几种反应产生。
步骤（ 4 ）的电渗析设备采用夹板式或卷式，所用膜为抗污染耐腐蚀的均相离子交换膜或双极膜，所用电源采用倒极或频繁倒极方式，所述预浓缩为将硫酸质量分数浓缩至 10 ～ 20% 。
步骤（ 5 ）的蒸发浓缩设备采用二效或三效蒸发或膜蒸馏方式进行浓缩，酸将由硫酸质量分数 10 ～ 20% 的酸浓缩至 30 ～ 60% ，所述二效或三效蒸发蒸发室和换热器采用石墨、 PP 、 PVDF 、 PTFE 中一种或几种，所述膜蒸馏运行温度为 60-90 ℃ ，真空采取水循环真空泵或柱塞真空泵实现，运行真空度为 -0.05--0.09MPa ，膜组件采用浸没式减压膜蒸馏或多效膜蒸馏运行；膜蒸馏 过滤孔径为0.2-0.5μ m , 通量为3-5L/m2。
步骤（ 6 ）蒸发得到含氟氯浓缩酸液采用吹脱解析法脱除氟氯，并得到氟氯混酸，所述的热风吹脱温度为 110-120 ℃ ，吹脱时间为 1-2 h 。
与上述的污酸资源回收与深度处理方法配套的装置，由精密过滤器、选择性吸附罐、铜砷分离设备、硫化设备、电渗析设备、蒸发浓缩设备及吹脱设备依次连接而成。
本发明具有以下有益效果
1 、采用选择性吸附的方法从污酸废水中吸附富集稀贵金属离子，以相对简单的方式充分回收了废酸中的高附加值成分，并得到高浓度的富集溶液且没有给溶液带来二次污染，有利于废酸的后续处理与利用。
2 、 目前污酸废水常采用石灰中和、硫化法处理，产生大量硫化砷渣（也称砷滤饼），铜砷硫等元素赋存其中为危险废物，且铜砷分离难度大。碱浸法常用于回收砷滤饼中的有价金属，但耗碱量大，后续含砷的强碱液处理仍是难题；加压氧化浸出法，铜砷的浸出率均达 90% 以上，但存在对设备要求较高、成本高的问题。 针对传统污酸硫化过程所产生砷滤饼中铜砷分离的难题，发明人惊喜的发现若将 铜砷分离后的滤液通过硫化剂深度除砷，得到的硫化砷渣回用于铜砷分离 ，较砷滤饼产生后再进行浸出分离存在以下优势：在污酸的处理过程中即实现了铜与砷的高效分离，同时得到高品位的硫化铜渣，避免了砷滤饼的大量产生，保障了铜的回收，为砷的深度净化提供了条件。
3 、采用电渗析与蒸发结合的方法用于污酸废水处理，最大程度降低了运行成本，根据污酸废水的特点，在较低酸浓度条件下采用电渗析进行预浓缩，在较高酸浓度条件下采用多效蒸发或膜蒸馏继续进行浓缩。
4 、通过膜蒸馏技术和蒸发浓缩实现氟氯的富集为氟氯分离提供条件，采用吹脱解析法分离氟氯并进一步浓缩酸，可得到较高浓度的氟氯混酸和低氟氯的硫酸，硫酸可以返回系统使用，氟氯混酸可以从系统开路。
5 、本发明能实现污酸废水的资源化和循环利用，可充分回收稀贵金属；实现铜砷的高效分离，污酸中砷的深度净化，回收高品位铜渣，单独开路砷渣；实现氟氯的富集与开路，硫酸的浓缩与回用。工艺净化高效，资源综合回收效果好，抗冲击负荷强，处理成本低，产生砷渣量少，二次污染风险小，具有良好的经济和环境效益。
附图说明
图 1 为本发明工艺流程图；
图 2 为本发明装置图；
1 为 精密过滤器， 2 为选择性吸附罐， 3 为铜砷分离设备， 4 为硫化设备， 5 为电渗析设备， 6 为蒸发浓缩设备， 7 为吹脱设备。
本发明将污酸废水先通过精密过滤器 1 过滤悬浮物，然后进入选择性吸附罐 2 选择性吸附包括铼和硒在内的稀贵金属；再利用硫化砷或者硫化砷渣在铜砷分离设备 3 中进行铜砷分离；铜砷分离后滤液在硫化设备 4 中采用硫化剂深度除砷，得到的硫化砷渣回用于铜砷分离；分离砷渣后滤液进入电渗析设备 5 预浓缩酸并分离富集氟氯；电渗析设备浓缩液进入蒸发浓缩设备 6 继续进行酸浓缩，蒸发冷凝水回用；蒸发浓缩后酸采用吹脱设备 7 除氟氯，分离浓缩液回用于工艺或硫酸制酸系统，高浓度氟氯混酸外售或进一步资源化。
具体实施方式
以下结合实施例旨在进一步说明本发明，而非限制本发明。
首次硫化砷渣的取得为：在污酸中投入硫化物使污酸中铜和砷大部分硫化，得到硫化铜和硫化砷的混合渣，将该部分混合渣按比例投加到未硫化的污酸中，利用混合渣里的硫化砷置换污酸中的铜生成硫化铜渣，得到品位较高的富铜渣和富砷溶液，再采用硫化物沉淀富砷溶液得到硫化砷渣，该硫化砷渣可用于本发明工艺中步骤 2 的铜的置换分离过程。
将某冶炼企业的污酸废水经水质均化，通过 精密过滤器（ 过滤材料为有机多孔材料 PP ，孔径为 10μm ，过滤形式为袋式过滤器）去除颗粒和胶体杂质后进入选择性吸附罐，吸附罐出水 按照 As/Cu 摩尔比为 2:1 的比例加硫化砷渣，在 80 ℃ 下反应 1.5h 进行铜砷分离，过滤得到富铜渣（硫化铜渣）和富砷溶液， 根据硫化氢与砷反应生成硫化砷沉淀理论量的 1.1 倍往富砷溶液中通入硫化氢，在气液强化硫化设备中反应 30min ，反应后液进行固液分离，得到 硫化砷渣，将所述的硫化砷渣回用于前述的铜砷分离过程 。深度除砷后液进入电渗析设备进行酸浓缩和氟氯分离浓缩，电流密度为 40mA/cm2, 得到高氟氯高酸液（浓液）和低氟氯低酸废水（淡液，含大部分水和少量重金属），高氟氯高酸废水采用三效蒸发进行酸浓缩，将酸浓缩至 50% ， 同时得到低氟氯冷凝水可回用。浓缩酸采用热风吹脱进行氟氯脱除，热风吹脱温度为 120 ℃ ，吹脱时间为 2 h 。脱除氟氯后硫酸可返回冶炼系统回用，脱除氟氯后气体经过冷凝吸收后得到高氟氯混酸，可分离得到氢氟酸和盐酸作为副产品回用或外售。
通过选择吸附处理后污酸废水中铼的回收率可以达到 95% 以上，砷的吸附率小于 1% ，可以实现铼和砷的高效分离。通过硫化砷渣的回用，可使得铜砷分离后，铜的回收率大于 99% ，得到硫化铜渣中铜的品位为 58% ，砷含量为 3.2% ；富砷溶液经硫化反应后砷的脱除率为 99.9% ，溶液中砷的含量为 0.3mg/L ，砷渣中砷的品位为 55% 。经电渗析进行预浓缩分离后，酸由 3% 浓缩至 12% ，同时氟氯的分离率分别为 85% 和 90% ；通过三效蒸发浓缩酸，将酸的质量浓度由 12% 浓缩至 50% ，经过氟氯脱除处理后，酸度可达到 70% ，酸中氟氯的含量分别为 150mg/L 和 120mg/L ，得到氟氯混酸溶液氟氯浓度可达到 30g/L 以上，脱除氟氯后硫酸可以返回电解、制酸等工序使用，最大限度利用了资源，实现了污酸废水循环利用的目标。

Claims (16)

1 、一种污酸资源回收与深度处理方法，其特征在于，包括以下步骤：
（ 1 ）预处理与选择性吸附，污酸废水先通过精密过滤器过滤悬浮物，然后进入选择性吸附罐选择性吸附包括铼和硒在内的稀贵金属；
（ 2 ）再利用硫化砷或者硫化砷渣铜砷分离；
（ 3 ）铜砷分离后滤液采用硫化剂深度除砷，得到的硫化砷渣回用于步骤（ 2 ）；
（ 4 ）分离砷渣后滤液进入电渗析设备预浓缩酸并分离富集氟氯；
（ 5 ）电渗析设备浓缩液进入蒸发浓缩设备继续进行酸浓缩，蒸发冷凝水回用；
（ 6 ）蒸发浓缩后的酸液采用吹脱析出法除氟氯后回用于工艺或硫酸制酸系统，高浓度氟氯混酸外售或进一步资源化。
2 、根据权利要求 1 所述的方法，其特征在于，步骤（ 1 ）所述的污酸废水是有色金属冶炼产生的烟气在制酸净化工艺过程中产生的酸性废水，污酸中硫酸质量浓度在 2%-8% 之间，含有铜、铅、锌、镉、砷、镍、钴、锰、锡、锑、硒、汞、铟、铼离子中的一种或几种，以及氟、氯、硫酸根和氢离子。
3 、根据权利要求 1 所述的方法，其特征在于，步骤（ 1 ）精密过滤时过滤材料的孔径为 0.5-10μm 。
4 、根据权利要求 1 所述的 方法， 其特征在于， 步骤（ 1 ） 选择性吸附罐内填充选择性吸附填 料，该填料为氮杂环化合物功能化离子交换材料。
5 、根据权利要求 1 所述的 方法 ，其特征在于，步骤（ 2 ）铜砷分离时，硫化砷或者 硫化渣的用量按照 As/Cu 摩尔比为 1-5:1 的比例加入至经吸附罐处理后的污酸废水中。
6 、 根据权利要求 5 所述的 方法 ，其特征在于，步骤（ 2 ）铜砷分离是 在 40-80 ℃ 下反应，过滤后得到富铜渣和富砷溶液。
7 、 根据权利要求 6 所述的 方法 ，其特征在于，步骤（ 2 ）铜砷分离 反应时间为 1-3h 。
8 、 根据权利要求 1 所述的 方法 ，其特征在于，步骤（ 3 ）所采用硫化剂为硫化钠、硫氢化钠、硫化钙、硫化钡、硫化氢中的一种或几种。
9 、根据权利要求 1 所述的 方法 , 其特征在于，步骤（ 4 ）的电渗析设备采用夹板式或卷式，所用膜为抗污染耐腐蚀的均相离子交换膜或双极膜，所用电源采用倒极或频繁倒极方式，所述预浓缩为将硫酸质量分数浓缩至 10 ～ 20% 。
10 、根据权利要求 1 所述的 方法， 其特征在于，步骤（ 5 ）的蒸发浓缩设备采用二效或三效蒸发或膜蒸馏方式进行浓缩，酸将由硫酸质量分数 10 ～ 20% 的酸浓缩至 30 ～ 60% ，所述二效或三效蒸发蒸发室和换热器采用石墨、 PP 、 PVDF 、 PTFE 中一种或几种，所述膜蒸馏运行温度为 60-90 ℃ ，真空采取水循环真空泵或柱塞真空泵实现，运行真空度为 -0.05--0.09MPa ，膜组件采用浸没式减压膜蒸馏或多效膜蒸馏运行；膜蒸馏 过滤孔径为0.2-0.5μ m , 通量为3-5L/m2。
11 、根据权利要求 1 所述的 方法， 其特征在于，步骤（ 6 ）蒸发得到含氟氯浓缩酸液采用吹脱解析法脱除氟氯，并得到氟氯混酸，所述的热风吹脱温度为 110-120 ℃ ，吹脱时间为 1-2 h 。
12 、与权利要求 1-11 任一项所述的 污酸资源回收与深度处理方法配套的装置 ，其特征在于，由 精密过滤器（ 1 ）、选择性吸附罐（ 2 ）、铜砷分离设备（ 3 ）、硫化设备（ 4 ）、电渗析设备（ 5 ）、蒸发浓缩设备（ 6 ）及吹脱设备（ 7 ）依次连接而成。
13 、一种 污酸资源回收与深度处理方法，其特征在于，包括以下步骤：（ 1 ）预处理与选择性吸附，污酸废水先通过精密过滤器过滤悬浮物，然后进入选择性吸附罐选择性吸附包括铼和硒在内的稀贵金属；
（ 2 ）再利用硫化砷渣进行铜砷分离；
（ 3 ）铜砷分离后滤液采用硫化剂深度除砷，得到的硫化砷渣回用于步骤（ 2 ）。
14 、根据权利要求 13 所述的方法，其特征在于，步骤（ 2 ）中，对铜砷进行第一次分离时采用的硫化砷渣来源于治炼企业向污酸或电解废液中投加硫化物除砷而得到的硫化砷渣。
15 、根据权利要求 13 所述的方法，其特征在于， 步骤（ 2 ）中的铜砷分离时， 硫化渣的用量按照 As/Cu 摩尔比为 1-5:1 的比例加入至经吸附罐处理后的污酸废水中。
16 、根据权利要求 13 或 14 所述的方法，其特征在于，步骤（ 1 ）所述的污酸废水是有色金属冶炼产生的烟气在制酸净化工艺过程中产生的酸性废水，污酸中硫酸质量浓度在 2%-8% 之间，含有铜、铅、锌、镉、砷、镍、钴、锰、锡、锑、硒、汞、铟、铼离子中的一种或几种，以及氟、氯、硫酸根和氢离子。
PCT/CN2016/098594 2015-12-28 2016-09-09 污酸资源回收与深度处理方法及装置 Ceased WO2017113882A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US16/066,902 US10662075B2 (en) 2015-12-28 2016-09-09 Method and apparatus for the recovery and deep treatment of polluted acid

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201510992841.X 2015-12-28
CN201510992841.XA CN105439355B (zh) 2015-12-28 2015-12-28 污酸资源回收与深度处理方法及装置

Publications (1)

Publication Number Publication Date
WO2017113882A1 true WO2017113882A1 (zh) 2017-07-06

Family

ID=55550068

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2016/098594 Ceased WO2017113882A1 (zh) 2015-12-28 2016-09-09 污酸资源回收与深度处理方法及装置

Country Status (3)

Country Link
US (1) US10662075B2 (zh)
CN (1) CN105439355B (zh)
WO (1) WO2017113882A1 (zh)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107162305A (zh) * 2017-07-07 2017-09-15 金川集团股份有限公司 一种酸性废水处理装置及其使用方法
CN107445379A (zh) * 2017-08-25 2017-12-08 金川集团股份有限公司 一种酸性废水蒸发减排的装置及方法
CN113354171A (zh) * 2021-05-13 2021-09-07 西北矿冶研究院 一种从铜冶炼废酸中深度脱砷的工艺方法
CN115057568A (zh) * 2022-06-08 2022-09-16 厦门钨业股份有限公司 仲钨酸铵结晶母液的处理方法
CN115156298A (zh) * 2022-07-25 2022-10-11 泰州海陵液压机械股份有限公司 一种平整机轧辊冷却用喷淋装置

Families Citing this family (44)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105439355B (zh) * 2015-12-28 2018-05-25 中南大学 污酸资源回收与深度处理方法及装置
CN105803208B (zh) * 2016-04-20 2017-11-28 武汉长海高新技术有限公司 一种硫酸废液中铼的分离回收方法
US10239770B2 (en) * 2016-04-29 2019-03-26 Kookmin University Industry Academy Cooperation Foundation Multi-stage submerged membrane distillation water treatment apparatus
CN105833729A (zh) * 2016-05-12 2016-08-10 浙江赛特膜技术有限公司 双极膜电渗析系统及采用其制备高纯度四甲基氢氧化铵的方法
CN106007045A (zh) * 2016-08-09 2016-10-12 成都虹华环保科技股份有限公司 一种回收湿法冶金废水中酸的装置及回收方法
CN106086426B (zh) * 2016-08-15 2018-03-06 郴州金山冶金化工有限公司 一种硫化砷渣高压氧连续浸出资源化利用工艺
CN107673539B (zh) * 2017-11-17 2021-07-09 云南省环境科学研究院(中国昆明高原湖泊国际研究中心) 一种酸性废水处理设备及处理方法
CN108570559A (zh) * 2018-05-16 2018-09-25 江西铜业股份有限公司 一种从高酸溶液中深度硫化分离铜镍砷的方法
CN108950200B (zh) * 2018-08-21 2020-02-14 紫金矿业集团股份有限公司 一种载金高砷铜精矿脱砷回收伴生金的方法
CN109078351B (zh) * 2018-09-17 2023-09-05 杭州东日节能技术有限公司 一种脱氟氯塔以及采用该塔脱除硫酸中氟氯的工艺及装置
CN110563021B (zh) * 2019-10-16 2023-04-07 大冶有色金属有限责任公司 一种无害化处理回收碱式氯化铜的方法及装置
CN110759394B (zh) * 2019-10-31 2022-01-25 昆明理工大学 一种利用生物碳和铜渣处理有色冶炼污酸中砷的方法
CN110790441A (zh) * 2019-12-10 2020-02-14 中国工程物理研究院动力部 一种从含铜废液中回收铜的装置和方法
CN111072206B (zh) * 2019-12-16 2022-03-15 昆明理工大学 一种酸性污水的处理方法
CN110981014A (zh) * 2019-12-17 2020-04-10 南京大学常高新国际环保产业技术研究院 一种含铁废硫酸资源化回收工艺
CN111056675B (zh) * 2019-12-19 2022-03-29 北京矿冶科技集团有限公司 一种污酸资源化和回收方法
CN111018221B (zh) * 2019-12-25 2021-02-26 长沙华时捷环保科技发展股份有限公司 一种冶炼污酸废水资源化处理的方法
CN113105013B (zh) * 2020-01-09 2022-10-18 湖南中金岭南康盟环保科技有限公司 一种锌冶炼电解液中氟氯的脱除方法
CN111661971A (zh) * 2020-06-29 2020-09-15 株洲冶炼集团科技开发有限责任公司 一种铅锌冶炼烟气洗涤高浓度污酸零排放工艺
CN111661972A (zh) * 2020-06-29 2020-09-15 株洲冶炼集团科技开发有限责任公司 一种铅锌冶炼烟气洗涤污酸治理及资源化利用的工艺
CN111792776A (zh) * 2020-07-13 2020-10-20 矿冶科技集团有限公司 一种重金属废水处理后浓水深度处理资源化方法
CN112645483A (zh) * 2020-11-10 2021-04-13 常熟市电热合金材料厂有限公司 一种电热合金丝酸洗产生的废酸液的回收处理系统及方法
CN112458292A (zh) * 2020-11-17 2021-03-09 湖南仁发材料科技有限公司 一种污酸中有价金属分类回收工艺
CN112759162B (zh) * 2020-12-30 2021-11-19 武汉飞博乐环保工程有限公司 一种污酸资源化处理方法及系统
CN113061463A (zh) * 2021-01-04 2021-07-02 刘国平 一种矿物质油生产用过滤蒸馏装置及方法
CN113354014B (zh) * 2021-05-06 2023-04-14 浦恩远 一种方便操作的水样汞蒸气吹脱浓缩装置
CN113249582B (zh) * 2021-05-06 2022-03-29 中南大学 一种铝冶金固废的处理方法
CN113354015B (zh) * 2021-05-06 2022-09-16 浦恩远 一种自动化水样汞蒸气吹脱浓缩装置
CN113528846A (zh) * 2021-06-18 2021-10-22 广西壮族自治区环境保护科学研究院 一种含砷废渣资源化利用的处理方法
CN113666530A (zh) * 2021-07-19 2021-11-19 铜陵有色金属集团股份有限公司 铜冶炼烟气净化污酸的除硒方法
CN114044575A (zh) * 2021-10-15 2022-02-15 浙江大学 一种中低砷污染水体的植物修复治理方法
CN114230054B (zh) * 2021-12-06 2024-01-30 国投金城冶金有限责任公司 一种含氯铜、砷的酸性废水中有价元素的综合回收方法
CN114057167A (zh) * 2021-12-15 2022-02-18 南通三圣石墨设备科技股份有限公司 硫酸法钛白粉一洗稀废酸膜集成资源化零排处理方法
CN114455771B (zh) * 2022-03-18 2022-09-20 北京中科瑞升资源环境技术有限公司 污酸的处理系统和方法
CN115490306B (zh) * 2022-08-11 2025-09-23 长沙矿冶研究院有限责任公司 一种含砷废酸的处理方法
CN116395779B (zh) * 2023-06-07 2023-09-26 赛恩斯环保股份有限公司 一种从污酸硫化后液中抑镉萃氟的方法
CN117228871B (zh) * 2023-09-08 2024-04-16 北京神舟茂华环保科技有限公司 一种含氟废水中氟离子选择性分离及全组分回收的方法
CN117185261B (zh) * 2023-09-12 2026-04-07 中国石油化工股份有限公司 一种废硫酸净化浓缩处理系统及其使用工艺
CN117358042A (zh) * 2023-11-10 2024-01-09 昆明理工大学 一种冶炼制酸烟气冷却酸洗过程中脱氟除氯的处理系统及其处理工艺
CN118026457A (zh) * 2024-03-19 2024-05-14 鲁信天地人环境科技(安徽)集团有限公司 一种酸洗废液资源化回用系统和方法
CN118108304A (zh) * 2024-03-19 2024-05-31 鲁信天地人环境科技(安徽)集团有限公司 一种废酸资源化回用系统和方法
CN118878129B (zh) * 2024-07-22 2026-02-27 河南中原黄金冶炼厂有限责任公司 一种贵金属冶炼高氯物料的处理工艺
CN119019042B (zh) * 2024-09-18 2026-03-20 云南宁氟环保科技有限公司 含氟废水中低成本高效回收氟元素的方法
CN119504075A (zh) * 2024-12-02 2025-02-25 昆明冶金研究院有限公司 一种回收利用高砷铜污酸的方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1789445A (zh) * 2005-12-23 2006-06-21 朱永文 铜冶炼高砷烟尘硫酸浸出液分离铜砷锌的方法
US20080056982A1 (en) * 2006-08-30 2008-03-06 Danny Mislenkov Process for recycling waste acid
CN101429594A (zh) * 2008-12-15 2009-05-13 中南大学 二氧化硫还原-扩散渗析法从高铜高砷废水中分离和回收铜和砷
JP4353731B2 (ja) * 2003-06-10 2009-10-28 前澤工業株式会社 溶液中のヒ素の除去方法
CN103553248A (zh) * 2013-10-23 2014-02-05 中南大学 重金属污酸废水资源化回收方法及装置
CN103599773A (zh) * 2013-11-26 2014-02-26 沈阳化工大学 利用膨润土吸附回收工业催化剂废渣中贵金属元素的方法
CN105439355A (zh) * 2015-12-28 2016-03-30 中南大学 污酸资源回收与深度处理方法及装置

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2006348359A (ja) * 2005-06-17 2006-12-28 Kazuhiro Niizawa 金属の回収方法
CN101618898A (zh) * 2008-07-02 2010-01-06 深圳市众恒隆实业有限公司 酸性废水中金、铂金和钯金的离子交换回收方法
CN102168176B (zh) * 2011-03-10 2012-11-14 田文学 焙烧——氰化含金尾渣中有价金属综合回收工艺
CN103014355B (zh) * 2012-12-13 2014-12-24 马永涛 铜冶炼烟灰多金属综合回收工艺
CN104445095B (zh) * 2014-12-18 2016-05-25 中南大学 一种冶炼污酸净化的方法
EP3709001B1 (en) * 2015-11-10 2024-03-06 LacriSciences LLC Systems and methods for determining sample osmolarity

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4353731B2 (ja) * 2003-06-10 2009-10-28 前澤工業株式会社 溶液中のヒ素の除去方法
CN1789445A (zh) * 2005-12-23 2006-06-21 朱永文 铜冶炼高砷烟尘硫酸浸出液分离铜砷锌的方法
US20080056982A1 (en) * 2006-08-30 2008-03-06 Danny Mislenkov Process for recycling waste acid
CN101429594A (zh) * 2008-12-15 2009-05-13 中南大学 二氧化硫还原-扩散渗析法从高铜高砷废水中分离和回收铜和砷
CN103553248A (zh) * 2013-10-23 2014-02-05 中南大学 重金属污酸废水资源化回收方法及装置
CN103599773A (zh) * 2013-11-26 2014-02-26 沈阳化工大学 利用膨润土吸附回收工业催化剂废渣中贵金属元素的方法
CN105439355A (zh) * 2015-12-28 2016-03-30 中南大学 污酸资源回收与深度处理方法及装置

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107162305A (zh) * 2017-07-07 2017-09-15 金川集团股份有限公司 一种酸性废水处理装置及其使用方法
CN107445379A (zh) * 2017-08-25 2017-12-08 金川集团股份有限公司 一种酸性废水蒸发减排的装置及方法
CN113354171A (zh) * 2021-05-13 2021-09-07 西北矿冶研究院 一种从铜冶炼废酸中深度脱砷的工艺方法
CN113354171B (zh) * 2021-05-13 2022-11-08 西北矿冶研究院 一种从铜冶炼废酸中深度脱砷的工艺方法
CN115057568A (zh) * 2022-06-08 2022-09-16 厦门钨业股份有限公司 仲钨酸铵结晶母液的处理方法
CN115057568B (zh) * 2022-06-08 2023-10-31 厦门钨业股份有限公司 仲钨酸铵结晶母液的处理方法
CN115156298A (zh) * 2022-07-25 2022-10-11 泰州海陵液压机械股份有限公司 一种平整机轧辊冷却用喷淋装置

Also Published As

Publication number Publication date
CN105439355B (zh) 2018-05-25
US20190023585A1 (en) 2019-01-24
US10662075B2 (en) 2020-05-26
CN105439355A (zh) 2016-03-30

Similar Documents

Publication Publication Date Title
WO2017113882A1 (zh) 污酸资源回收与深度处理方法及装置
CN105540973B (zh) 高砷污酸废水净化及循环利用的方法
CN108002580B (zh) 一种酸性烟气洗涤废水处理方法及其用途
CN109081409B (zh) 一种选冶联合清洁处理污酸的方法
CN108218038A (zh) 一种树脂吸脱附-扩散渗析处理含重金属废水的方法
CN102120658B (zh) 电解锰生产末端废水中氨氮的处理和回收方法
CN110734169A (zh) 一种酸性溶液除氯的方法
CN111003853A (zh) 一种电镀废液处理方法
CN102910760A (zh) 一种含重金属污酸的处理工艺
CN108666644B (zh) 一种从锂电池废电解液中回收氟和锂的方法
CN109824193A (zh) 铝氧化工业废酸回收工艺
CN108191132A (zh) 一种高氯盐高酸废水中重金属的回收方法
CN217264980U (zh) 一种酸洗废酸的脱酸装置
CN107311363A (zh) 一种含砷硫酸污酸的净化回用工艺
CN111499055B (zh) 一种锂系橡胶合成废水的综合处理方法
CN107381705B (zh) 一种相变调控分离回收水中多种阳离子重金属的方法
CN105543481B (zh) 铜阳极泥处理产生的高酸废液中铜、铋、砷分离的方法
CN205368001U (zh) 污酸资源回收与深度处理装置
Zhao et al. Application of AnMBR ion exchange technology in water treatment
CN112607925A (zh) 一种硅钢稀酸废水零排放处理方法和系统
CN107473319B (zh) 一种相变调控回收水中阳离子重金属的方法
CN111762927A (zh) 一种高酸度化工含汞废酸液联合脱汞的方法和装置
CN107335399B (zh) 一种相变调控分离回收水中重金属阴、阳离子的方法
CN100415654C (zh) H酸生产废水的净化和资源回收利用的方法
CN213680180U (zh) 一种石灰石-石膏法脱硫废水氯离子萃取系统

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16880675

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 16880675

Country of ref document: EP

Kind code of ref document: A1

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205 DATED 14-12-2018)

122 Ep: pct application non-entry in european phase

Ref document number: 16880675

Country of ref document: EP

Kind code of ref document: A1