A method and system for recovering iodine from wastewater containing organic iodide

Abstract

The application discloses a method and system for recovering iodine from wastewater containing organic iodide, and the method comprises three steps of biochemical treatment, oxidation adsorption and desorption to recover elemental iodine or coarse iodine from the wastewater containing organic iodide. The iodine recovery of industrialized wastewater with large flow is realized by using a continuous flow reactor.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of wastewater treatment, in particular to a method and system for recovering iodine from wastewater containing organic iodide. BACKGROUND

[0002] China is short of iodine resources, about 90% of iodine is relied on imports, and the recycling of iodine resources is particularly important. The treatment of wastewater containing organic iodide is a difficult production technical problem, because if the wastewater is not properly disposed of during biochemical treatment, elemental iodine will be produced, which will destroy the bacterial flora of the biochemical system and cause the biochemical system of the wastewater to collapse. Currently, the organic iodide is separated from the wastewater by concentration method, which will consume a large amount of energy; the separated organic iodide is generally converted into inorganic iodide by zinc powder reduction method, and then elemental iodine is obtained by acidification and oxidation, and a large amount of solid waste containing zinc salt will be inevitably produced in the reduction process, which will cause great pressure on the environment. SUMMARY

[0003] The present application solves the problems of large energy consumption or large pollution in the recovery of iodine from wastewater containing organic iodide.

[0004] The present application provides a method and system for recovering iodine from wastewater containing organic iodide.

[0005] The technical solution of the present application is:

[0006] A method for recovering iodine from wastewater containing organic iodide, comprising:

[0007] Biochemical treatment: the wastewater containing organic iodide is treated by anaerobic process, which is used to convert the organic iodide in the wastewater into inorganic iodide ions and to reduce the chemical oxygen demand (COD) of the wastewater to less than or equal to 2000 mg / L; after the anaerobic process, the wastewater is treated by aerobic process or facultative process, and the dissolved oxygen in the aerobic process or facultative process is less than 2 mg / L. After the anaerobic treatment, the chemical oxygen demand of the wastewater can be reduced to less than or equal to 2000 mg / L, and the chemical oxygen demand of the wastewater is further reduced after the aerobic process or facultative process.

[0008] Oxidation and adsorption: the pH value of the wastewater treated by biochemical treatment is adjusted to be acidic, and then oxidation is carried out to convert the inorganic iodide ions into iodine, and the iodine is adsorbed by an adsorption device.

[0009] Desorption and recovery: the adsorption device is desorbed, and the eluent obtained by desorption is adjusted to be acidic, and then oxidation is carried out to obtain crude iodine or elemental iodine.

[0010] Preferably, the wastewater after biochemical treatment is delivered to a continuous flow reactor, and the oxidation adsorption treatment is performed in the continuous flow reactor.

[0011] Preferably, the wastewater after biochemical treatment is delivered to a reaction kettle, and the oxidation adsorption treatment is performed in the reaction kettle.

[0012] Preferably, the dissolved oxygen is less than 1 mg / L.

[0013] Preferably, the pH value is adjusted to 0-5 in the oxidation adsorption treatment.

[0014] Preferably, the pH value is adjusted to 0-5 in the desorption recovery treatment.

[0015] Preferably, the adsorption device is provided with an adsorbent, and the adsorbent includes macroporous adsorption resin or activated carbon or diatomite.

[0016] Preferably, the adsorption is stopped when the wastewater passing through the adsorption device reaches a preset threshold or the adsorption device reaches a preset threshold.

[0017] Preferably, the pH value is adjusted by adding an acid solution in the oxidation adsorption treatment, and the acid solution includes hydrochloric acid or sulfuric acid or phosphoric acid.

[0018] Preferably, the pH value is adjusted by adding an acid solution in the desorption recovery treatment, and the acid solution includes hydrochloric acid or sulfuric acid or phosphoric acid.

[0019] Preferably, an oxidizing agent is added for oxidation reaction in the oxidation adsorption treatment, and the oxidizing agent includes hydrogen peroxide or chlorine or sodium hypochlorite or sodium nitrite.

[0020] Preferably, an oxidizing agent is added for oxidation reaction in the desorption recovery treatment, and the oxidizing agent includes hydrogen peroxide or chlorine or sodium hypochlorite or sodium nitrite.

[0021] Preferably, the continuous flow reactor is provided with a turbulence device for generating turbulent flow of liquid in the continuous flow reactor.

[0022] Preferably, the pH value is adjusted to 2-3.

[0023] Preferably, the adsorbent is macroporous adsorption resin, and the adsorption device is a resin column.

[0024] A system for recovering iodine from wastewater containing organic iodide, for implementing the method for recovering iodine from wastewater containing organic iodide, including an anaerobic device, an aerobic device or a facultative device, a separation device, a reaction device, an adsorption device and a recovery device.

[0025] Preferably, the reaction apparatus is a continuous flow reactor, and the continuous flow reactor is equipped with a flow turbulence device. The flow turbulence device is used to adjust the flow rate of wastewater in the continuous flow reactor to a Reynolds number of 60,000-140,000. Preferably, the Reynolds number is 70,000-90,000.

[0026] Preferably, the adsorption device is provided with a window for observing the wastewater or a detection device for detecting the state of the wastewater.

[0027] Compared with the prior art, the present invention has the following advantages and effects:

[0028] This invention directly treats wastewater containing organic iodides using biochemical methods, converting the organic iodides into inorganic iodides, which are then acidified and oxidized to elemental iodine. The elemental iodine is then enriched using an adsorption device. The process avoids energy-intensive concentration methods, and the conversion from organic to inorganic iodides does not employ chemical reduction methods such as zinc powder or incineration. Instead, it utilizes the physical properties of the adsorption device itself to adsorb and enrich elemental iodine. The overall solution is low in energy consumption, low in pollution, and low in cost, making it particularly suitable for the treatment and iodine recovery of large volumes of wastewater containing organic iodides. Attached Figure Description

[0029] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0030] Figure 1 This is a schematic diagram of the process of the present invention. Detailed Implementation

[0031] The present invention will be further described in detail below with reference to the embodiments. The following embodiments are explanations of the present invention, but the present invention is not limited to the following embodiments.

[0032] Example:

[0033] A method for recovering iodine from wastewater containing organic iodides includes:

[0034] Biochemical treatment: Wastewater containing organic iodides is treated using an anaerobic process to convert the organic iodides in the wastewater into inorganic iodides. The wastewater treated by the anaerobic process is then treated by an aerobic or facultative process. The dissolved oxygen in the aerobic or facultative process is less than 2 mg / L, further reducing the chemical oxygen demand in the wastewater to less than 500 mg / L.

[0035] Oxidative adsorption: The pH value of the biochemically treated wastewater is adjusted to acidic and then oxidized. The oxidized wastewater is then used to adsorb iodine using an adsorption device.

[0036] Desorption recovery: desorption of the adsorption device, pH adjustment of the eluent obtained by desorption, oxidation after adjusting to acidic, and filtration to obtain iodine.

[0037] In one or more embodiments, the organic iodide in the wastewater includes iodine contrast agent and its intermediates, iodobenzene, etc., and the generated wastewater mainly includes various, such as iodine contrast agent iodination process filter press wastewater, acylation, hydrolysis process decolorization before filter press wastewater and decolorization after filter press wastewater, condensation process vacuum distillation wastewater, resin regeneration cleaning wastewater and thin film evaporation wastewater, refining process resin regeneration cleaning after atmospheric distillation wastewater, thin film evaporation wastewater, resin desalination after regeneration cleaning wastewater, and finally ultrafiltration wastewater, etc. The COD concentration index of the wastewater is relatively high, for example, the COD is 20000 mg / L.

[0038] In one or more embodiments, the concentration of organic iodide in the wastewater is 50-3000 ppm.

[0039] In one or more embodiments, the anaerobic process, also known as anoxic process, refers to a process in which various complex organic matters in wastewater are decomposed and converted into substances such as methane and carbon dioxide by the action of anaerobic microorganisms under the condition of no molecular oxygen. Specifically, it refers to the metabolic characteristics of anaerobic microorganisms, which gradually convert long-chain hydrocarbons, aromatic compounds and other macromolecular organic matters into methane, carbon dioxide, water, hydrogen sulfide and ammonia, etc. through a series of complex biochemical reactions in anoxic environment. This process significantly reduces the biological toxicity of wastewater and greatly improves the biodegradability of wastewater, making it easier for the originally difficult-to-treat wastewater to be accepted and degraded by subsequent biological treatment processes. In addition, part of the organic matter is removed during hydrolysis and acidification, further reducing the burden on the subsequent treatment unit, providing more stable and high-quality water conditions for it, and improving the treatment efficiency of the entire wastewater treatment system.

[0040] In one or more embodiments, the anaerobic process can be divided into three stages: hydrolysis-acidification stage, acetogenesis stage, and methanogenesis stage. (1) Hydrolysis-acidification stage: Hydrolysis can be defined as the process in which complex, insoluble polymers are converted into simple, soluble monomers or dimers. High molecular weight organic compounds cannot be directly utilized by bacteria because they are too large to pass through the cell membrane. They are first broken down into small molecules by extracellular enzymes in the first stage. For example, cellulose is hydrolyzed by cellulase into cellobiose and glucose, starch is broken down by amylase into maltose and glucose, and proteins are hydrolyzed by proteases into short peptides and amino acids, etc. These small molecules can dissolve in water and pass through the cell membrane to be utilized by bacteria. The hydrolysis process is usually slow and is therefore considered to be the rate-limiting step in the anaerobic degradation of high molecular weight organic compounds or suspended solids. Various factors such as temperature, composition of the organic compounds, concentration of the hydrolysis products, etc. can affect the rate and extent of hydrolysis. The rate of hydrolysis can be described by the following kinetic equation: p = po / (l + Kh.T), where p represents the concentration of degradable, insoluble substrate, po represents the initial concentration of the insoluble substrate, Kh represents the hydrolysis constant, and T represents the residence time. Acidification can be defined as the biological degradation process in which soluble organic compounds are converted into end products, mainly volatile fatty acids, in which the compounds act both as electron acceptors and electron donors. In this stage, the above-mentioned small molecules are converted into simpler compounds by intracellular conversion of the fermentation bacteria (i.e., acidogenic bacteria) and are secreted outside the cells. Most of the fermentation bacteria are strict anaerobes, but about 1% of facultative anaerobes are usually present in anaerobic environments, and these facultative anaerobes can protect strict anaerobes such as methanogens from damage and inhibition by oxygen. The main products of this stage are volatile fatty acids, alcohols, lactic acid, carbon dioxide, hydrogen, ammonia, hydrogen sulfide, etc., and the composition of the products depends on the conditions of the anaerobic degradation, the types of substrates, and the microbial population involved in the acidification. (2) Acetogenesis stage: The products of the previous stage are further converted into acetic acid, hydrogen, carbonic acid, and new cell mass by the action of hydrogen-producing acetogenic bacteria. (3) Methanogenesis stage: In this stage, acetic acid, hydrogen, carbonic acid, formic acid, and methanol are converted into methane, carbon dioxide, and new cell mass. The process in which methanogenic bacteria convert acetic acid, acetate, carbon dioxide, and hydrogen into methane is accomplished by two physiologically different groups of methanogens, one group converting hydrogen and carbon dioxide into methane, and the other group decarboxylating acetic acid or acetate to produce methane, with the former accounting for about 1 / 3 of the total amount and the latter accounting for about 2 / 3.

[0041] In one or more embodiments, the microorganisms participating in the anaerobic biological treatment are mainly bacteria, which can be divided into two categories: non-methane-producing bacteria (acid-producing bacteria) and methane-producing bacteria. The non-methane-producing bacteria mainly consist of obligate anaerobes and facultative anaerobes, about 18 genera and more than 50 species. The former mainly includes Clostridium, Bacteroides, Bifidobacterium, Corynebacterium, and Actinomyces, etc. The latter mainly includes Proteus, Pseudomonas, Bacillus, Streptococcus, Flavobacterium, Pseudomonas, Aerobacter, etc. The common methane-producing bacteria mainly include four categories: Methanobacterium, Methanococcus, Methanosarcina, and Methanospirillum.

[0042] In one or more embodiments, the aerobic process treatment refers to a biochemical process in which organic matter is degraded and converted into humus-like substances under the participation of microorganisms, suitable carbon-nitrogen ratio, moisture content, and oxygen, etc.

[0043] In one or more embodiments, the aerobic process treatment is as follows: under aerobic conditions, aerobic microorganisms oxidize and decompose organic matter through respiration, ultimately producing carbon dioxide, water, and heat. Under aerobic conditions, autotrophic bacteria nitrify NH3-N (NH4 + ) to NO3 - , which requires the participation of oxygen.

[0044] In one or more embodiments, the microorganisms in the aerobic treatment are mainly bacteria (mainly aerobic heterotrophic bacteria) and protozoa, in addition to yeast, filamentous fungi, unicellular algae, rotifers, nematodes, etc. Bacteria account for 90% of the total number of microorganisms, with a quantity of 10 8 -10 9 million / mL, which are the main force for removing organic pollutants in water. The most common dominant population is Alcaligenes, Bacillus, Flavobacterium, Pseudomonas, Zooglea, followed by Achromobacter, Nocardia, Bdellovibrio, nitrifying bacteria, Escherichia coli, etc., which are all chemoautotrophic bacteria, most of which are gram-negative bacteria that can effectively decompose organic pollutants in wastewater.

[0045] In one or more embodiments, the facultative process refers to a process of simultaneously treating organic matters in wastewater by aerobic and anaerobic processes using facultative anaerobic bacteria (bacteria capable of both aerobic respiration and anaerobic respiration). In the prior art, the COD of industrial wastewater after anaerobic treatment is generally 4000-6000 mg / L, and thus must be treated by an aerobic process to reduce the COD to a desired value. Even after the facultative process, the wastewater must be treated by an aerobic process. By reducing the COD to 2000 mg / L or less in the anaerobic process stage, the facultative process or the aerobic process alone can reduce the COD to a desired value, and thus the wastewater does not need to be treated by an aerobic process after the facultative process. In one or more embodiments, increasing the residence time of the anaerobic process, increasing the volume of the anaerobic process device, and other means that can increase the capacity of the anaerobic process are technical means for implementing the present application, and thus the COD is reduced to 2000 mg / L or less in the anaerobic process stage.

[0046] In one or more embodiments, the dissolved oxygen in the aerobic process or the facultative process is less than 2 mg / L. In the prior art, the dissolved oxygen in the aerobic process is 2-4 mg / L. After the wastewater containing organic iodide is treated by the prior art aerobic process or the facultative process, the inorganic iodine ions in the wastewater are oxidized to elemental iodine. Elemental iodine has a physical property of killing bacteria, and thus destroys the microorganisms required for the anaerobic process, the aerobic process, or the facultative process, and thus the entire biochemical treatment cannot work properly. Therefore, in the present embodiment, the dissolved oxygen in the aerobic process or the facultative process is less than 2 mg / L, which can avoid the generation of elemental iodine in the biochemical treatment, and can reduce the COD of the wastewater to a desired value, for example, 400-600 mg / L, by biochemical treatment.

[0047] In one or more embodiments, the organic iodide-containing production wastewater is subjected to biochemical treatment of sewage, and then transferred to a reaction kettle or a continuous reactor, the pH value is adjusted to be acidic with an acid, an appropriate amount of oxidizing agent is added, and after a period of reaction, the wastewater is transferred to an adsorption device containing an adsorbent for iodine adsorption; the above steps are repeated, and when the adsorption is close to saturation, the adsorbed iodine on the adsorption device is desorbed with an alkaline aqueous solution, the alkaline eluent is adjusted to be acidic with an acid, and then an appropriate amount of oxidizing agent is added to oxidize elemental iodine, and the crude iodine is obtained by filtration. Preferably, due to the large amount of production wastewater, more reaction kettles are required for acidification reaction, and multiple repeated treatments are required, which consumes time and effort. The continuous flow reaction can be conveniently processed by using columnar reactors, tubular reactors, grid type reactors and the like. Preferably, the adsorbent can be selected from macroporous adsorption resin, activated carbon, diatomite and the like, and the adsorbent can be packed into a column for convenient adsorption. Preferably, the adsorbent is macroporous adsorption resin, and the adsorption device is a macroporous adsorption resin column. Preferably, the acid for adjusting the pH value can be selected from hydrochloric acid (including dilute hydrochloric acid or concentrated hydrochloric acid or concentrated hydrochloric acid diluted with water), sulfuric acid (including dilute sulfuric acid or concentrated sulfuric acid or concentrated sulfuric acid diluted with water), phosphoric acid (including dilute phosphoric acid or concentrated phosphoric acid or concentrated phosphoric acid diluted with water) or a mixed solution of two or more acids (for example, a mixed solution of hydrochloric acid and sulfuric acid), and the like, and hydrochloric acid is preferred. Preferably, the pH value is adjusted to be acidic, preferably 4 or lower, and more preferably 2-4. Preferably, the oxidizing agent can be hydrogen peroxide, chlorine, sodium hypochlorite, sodium nitrite or any combination that does not produce a chemical reaction (for example, a mixed solution of sodium hypochlorite and sodium nitrite), and the like, and hydrogen peroxide is preferred.

[0048] In one specific embodiment, the organic iodide-containing wastewater is subjected to biochemical treatment of factory sewage station, pumped into a reaction kettle 6.5 tons, the pH value is adjusted to be 2 or lower with about 30L of concentrated hydrochloric acid, 2.8L of hydrogen peroxide is added, and the oxidation reaction is carried out for 20-30 minutes. The oxidized wastewater is pumped into a resin column, and the elemental iodine is adsorbed by the resin column (containing resin 4.5m 3 ) in the resin column. The pH value of the adsorbed wastewater is adjusted to 6-9 with sodium hydroxide aqueous solution, and the wastewater is discharged into a sewage tank. The above operation is continuously repeated, and when the amount of wastewater passing through the resin column reaches a preset threshold (the preset threshold is the amount of wastewater passing through, for example, the amount of wastewater passing through is 1200-1500 tons), about 4000L of 5% sodium hydroxide aqueous solution is used for desorption, and about 4000L of drinking water is used for washing. The eluate is combined, the pH value is adjusted to be 2 or lower with concentrated hydrochloric acid, 150-300L of hydrogen peroxide is added for oxidation, and the crude iodine is obtained by filtration.

[0049] One embodiment, the wastewater containing organic iodide is treated by the biochemical process in the factory sewage station, and then pumped into the pipeline reactor at a flow rate of 15 cubic meters per hour. Concentrated hydrochloric acid is pumped into the reactor at a rate of 68.6 L / h, and the concentrated hydrochloric acid adjusts the wastewater to be acidic (pH 0-4). Hydrogen peroxide is pumped into the reactor at a flow rate of 4.6 L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into a resin column (containing resin 4.5 m 3 ). The adsorbed wastewater flows out of the resin column discharge pipe and liquid caustic is pumped into the resin column discharge pipe. The flow rate of the liquid caustic metering pump is adjusted so that the pH of the solution at the discharge port is between 6-9. When the resin column passes 1200 tons of wastewater, adsorption is stopped, about 4000 L of 5% sodium hydroxide solution is pumped into the resin column for desorption, and about 4000 L of drinking water is used for washing. The two eluents are combined, the pH is adjusted to below 2 with hydrochloric acid, 150-300 L of hydrogen peroxide is added for oxidation, and the crude iodine is obtained by suction filtration.

[0050] One embodiment, the wastewater containing organic iodide is treated by the biochemical process in the factory sewage station, and then pumped into the pipeline reactor at a flow rate of 15 cubic meters per hour. Concentrated sulfuric acid is pumped into the reactor at a rate of 23 L / h, and the concentrated sulfuric acid adjusts the wastewater to be acidic (pH 0-4). Commercial sodium hypochlorite solution is pumped into the reactor at a flow rate of 9 L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into a resin column (containing resin 4.5 m 3 ). The adsorbed wastewater flows out of the resin column discharge pipe and liquid caustic is pumped into the resin column discharge pipe. The flow rate of the liquid caustic metering pump is adjusted so that the pH of the solution at the discharge port is between 6-9. When the resin column passes 1300 tons of wastewater, adsorption is stopped, about 4000 L of 5% sodium hydroxide solution is pumped into the resin column for desorption, and about 4000 L of drinking water is used for washing. The two eluents are combined, the pH is adjusted to below 2 with sulfuric acid, 300-500 L of commercial sodium hypochlorite solution is added for oxidation, and the crude iodine is obtained by suction filtration.

[0051] One embodiment, the wastewater containing organic iodide is treated by the biochemical process in the factory sewage station, and then pumped into the pipeline reactor at a flow rate of 15 cubic meters per hour. Concentrated hydrochloric acid is pumped into the reactor at a rate of 68.6 L / h, and the concentrated hydrochloric acid adjusts the wastewater to be acidic (pH 0-4). Sodium hypochlorite is pumped into the reactor at a flow rate of 12 L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into a resin column (containing resin 4.5 m 3The adsorbed wastewater flows out through the discharge pipe of the resin column, and liquid alkali is pumped into the discharge pipe. The flow rate of the liquid alkali metering pump is adjusted to keep the pH of the aqueous solution at the discharge port between 6 and 9. When the wastewater volume passing through the resin column reaches 1500 tons, adsorption is stopped, and about 4000L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. Then, about 4000L of drinking water is used for washing. The two eluents are combined, and the pH is adjusted to below 2 with sulfuric acid. 600-1000L of commercially available sodium hypochlorite solution is added for oxidation, and crude iodine is obtained by filtration.

[0052] In one specific implementation, wastewater containing organic iodides, after biochemical treatment at the factory's wastewater treatment plant, is pumped into a pipeline reactor at a flow rate of 15 cubic meters per hour. Concentrated sulfuric acid is pumped into the reactor at a rate of 23 L / h to adjust the wastewater to acidity (pH 0-4). Hydrogen peroxide is then pumped into the reactor at a flow rate of 4.6 L / h for continuous reaction. The resulting solution is then continuously pumped from the pipeline reactor into a resin column (containing 4.5 m³ of resin). 3 The adsorbed wastewater flows out through the discharge pipe of the resin column, and liquid alkali is pumped into the discharge pipe of the resin column. The flow rate of the liquid alkali metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port between 6 and 9. When the wastewater flow through the resin column reaches the preset threshold (the preset threshold is the flow time, for example, the flow time is 50-100 hours), adsorption is stopped, and about 4000L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. Then, it is washed with about 4000L of drinking water. The two eluents are combined, and the pH value is adjusted to below 2 with sulfuric acid. Then, 600-1000L of commercially available sodium hypochlorite solution is added for oxidation, and the crude iodine is obtained by filtration.

[0053] A system for recovering iodine from wastewater containing organic iodides, and a method for recovering iodine from wastewater containing organic iodides, comprising an anaerobic device, an aerobic or facultative anaerobic device, a separation device, a reaction device, an adsorption device, and a recovery device, wherein the wastewater sequentially passes through the anaerobic device, the aerobic or facultative anaerobic device, the separation device, the reaction device, the adsorption device, and the recovery device.

[0054] In one or more embodiments, the anaerobic device, aerobic device, or facultative device adopts conventional anaerobic tanks, aerobic tanks, or facultative tanks, and the size and specifications of the anaerobic tanks, aerobic tanks, or facultative tanks can be adjusted according to the wastewater treatment requirements.

[0055] In one or more embodiments, the separation device employs methods including sedimentation, centrifugation, membrane separation, distillation, sublimation, crystallization, precipitation, solvent extraction, ion exchange, chromatographic separation, centrifugal separation, electrodialysis, electrochemical separation, salting out, etc.

[0056] In one or more embodiments, the adsorption device employs an adsorption column. The recovery device employs a reaction vessel.

[0057] In one or more embodiments, a turbulence device is arranged in the continuous flow reactor, and the turbulence device is used to generate turbulence in the liquid in the continuous flow reactor. The Reynolds number of the wastewater flow rate in the continuous flow reactor is 60000-140000, which can ensure sufficient mixing of the wastewater and the oxidizing agent and ensure complete oxidation reaction. Preferably, the Reynolds number is 70000-90000. The lower the Reynolds number, the less sufficient the mixing of the wastewater and the oxidizing agent, which leads to an increase in the length of the oxidation reaction, and thus an increase in the length of the reactor, resulting in an increase in cost and a decrease in economic benefit. If the Reynolds number is too high, a more complex turbulence device is required, resulting in an increase in cost and a decrease in economic benefit. The turbulence device can adopt a structure that can meet the above-mentioned Reynolds number requirements, such as a paddle, a metal mesh, etc.

[0058] In one or more embodiments, the size and specifications of the continuous reactor can be adjusted according to the treatment requirements of the wastewater. Preferably, a tubular reactor is used, which includes a horizontal tubular reactor, a vertical tubular reactor, a coil tubular reactor, a U-shaped tubular reactor, etc. In order to make the equipment compact and save space, a coil tubular reactor is preferred.

[0059] In one or more embodiments, an observation window is provided on the adsorption device for observing the state of the liquid in the adsorption device.

[0060] In one specific embodiment, the wastewater containing organic iodides is sequentially subjected to a wastewater conditioning tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, an A / O (A / O process connects the front-stage anoxic section and the rear-stage aerobic section in series, the DO (dissolved oxygen) in the A section is not greater than 0.2 mg / L, and the DO in the O section is 0-2 mg / L. The hydrolysis acidification tank and the anoxic section belong to anaerobic devices, and anaerobic bacteria are distributed in the hydrolysis acidification tank and the anoxic section. Compared with the existing non-methane-producing bacteria distributed in the hydrolysis acidification tank, the treatment capacity of the anaerobic process is increased, and the COD can be reduced to below 2000 mg / L. In the anoxic section, the heterotrophic bacteria hydrolyze starch, fiber, carbohydrates, and other suspended pollutants and soluble organic matter in the wastewater into organic acids, so that the macromolecular organic matter is decomposed into small molecular organic matter, and the insoluble organic matter is converted into soluble organic matter. When these hydrolyzed products in the anoxic section enter the aerobic tank for aerobic treatment, the biodegradability of the wastewater is improved, and the oxidation efficiency is improved; in the anoxic section, the heterotrophic bacteria ammonify the protein, fat, and other pollutants (N on the organic chain or amino group in the amino acid) to release ammonia (NH3, NH4 + ), and under sufficient oxygen supply conditions, the autotrophic bacteria oxidize NH3-N (NH4 + ) to NO3 - , which is returned to the A tank through reflux control, and under anoxic conditions, the heterotrophic bacteria denitrify NO3 -The reduction to molecular nitrogen (N2) completes the cycle of C, N, O in the ecology, to achieve the harmless treatment of sewage), MBR pool after biochemical treatment, with pump at a flow rate of 15 cubic meters / hour into the pipeline reactor. Pump concentrated hydrochloric acid into the reactor at 68.6L / h, concentrated hydrochloric acid will be adjusted to acidic wastewater (pH is 2-4), pump hydrogen peroxide into the reactor at a flow rate of 4.6L / h for continuous reaction. And the solution from the pipeline reactor after the reaction is continuously pumped into the resin column (loaded with resin 4.5m 3 ) in the discharge pipe of resin column pump liquid alkali, adjust the flow of liquid alkali metering pump, make the pH value of the effluent aqueous solution between 6-9. To be resin column through the wastewater for 50 hours, stop adsorption, pump 5% sodium hydroxide solution into the resin column about 4000L for desorption, and then washed with about 4000L drinking water, combined two eluate. Two eluate input into the reaction kettle, adjust the pH value to 2 or less with hydrochloric acid, add hydrogen peroxide 150-300L oxidation, suction filtration of crude iodine 368kg, purity 92.1%.

[0061] A specific embodiment, the wastewater containing organic iodide in turn through the wastewater conditioning tank, hydrolysis acidification tank (hydrolysis acidification tank belongs to anaerobic device, and the anaerobic bacteria are distributed in the hydrolysis acidification tank and the anoxic section, compared with the existing non-methane producing bacteria distributed in the hydrolysis acidification tank, the processing capacity of anaerobic process is increased, which can reduce the COD to below 2000mg / L), hydrolysis acidification sedimentation tank, primary A / O, intermediate sedimentation tank, secondary A / O (the structure of primary A / O and secondary A / O can be the same or different, for example, in this embodiment, the structure of primary A / O and secondary A / O is the same, and the treatment time is the same), final sedimentation tank, MBR pool (mbr membrane technology first removes biodegradable organic pollutants in water by activated sludge, and then uses membrane assembly to force intercept the activated sludge in the biological reactor and most of the suspended solids, to realize the solid-liquid separation of purified water and activated sludge, thereby strengthening the biochemical reaction and improving the sewage treatment effect and the quality of effluent) after biochemical treatment, with pump at a flow rate of 15 cubic meters / hour into the pipeline reactor. Pump concentrated hydrochloric acid into the reactor at 68.6L / h, concentrated hydrochloric acid will be adjusted to acidic wastewater (pH is 2), pump hydrogen peroxide into the reactor at a flow rate of 4.6L / h for continuous reaction. And the solution from the pipeline reactor after the reaction is continuously pumped into the resin column (loaded with resin 4.5m 3 ) in the discharge pipe of resin column pump liquid alkali, adjust the flow of liquid alkali metering pump, make the pH value of the effluent aqueous solution between 6-9. To be resin column through the wastewater for 100 hours, stop adsorption, pump 5% sodium hydroxide solution into the resin column about 4000L for desorption, and then washed with about 4000L drinking water, combined two eluate. Two eluate input into the reaction kettle, adjust the pH value to 2 or less with hydrochloric acid, add hydrogen peroxide 150-300L oxidation, suction filtration of crude iodine.

[0062] One embodiment, the wastewater containing organic iodide is sequentially through the wastewater conditioning tank, hydrolysis acidification tank, hydrolysis acidification sedimentation tank, primary A / O, intermediate sedimentation tank, secondary A / O (the structure of primary A / O and secondary A / O in this embodiment is different, and the processing time is different), final sedimentation tank, MBR tank (mbr membrane technology first removes biodegradable organic pollutants in water by activated sludge, and then uses membrane components to force intercept the activated sludge in the biological reactor and most of the suspended solids, to achieve solid-liquid separation of the purified water and activated sludge, thereby strengthening the biochemical reaction, improving the sewage treatment effect and the quality of effluent) to complete the biochemical treatment, and is pumped into the pipeline reactor at a flow rate of 15 cubic meters / hour. Concentrated sulfuric acid is pumped into the reactor at a rate of 23L / h, and the concentrated sulfuric acid adjusts the wastewater to be acidic (pH is 3), and sodium hypochlorite is pumped into the reactor at a flow rate of 10L / h for continuous reaction. The solution after reaction is continuously pumped from the pipeline reactor into the resin column (containing resin 4.5m 3 ) in the resin column. Pump liquid alkali into the discharge pipe of the resin column, adjust the flow rate of the liquid alkali metering pump, and make the pH value of the aqueous solution at the discharge port between 6-9. When the resin column reaches the preset threshold value (the preset threshold value is the use time of the resin column, for example, 100-200 hours), stop adsorption, pump about 4000L of 5% sodium hydroxide solution into the resin column for desorption, and then wash with about 4000L of drinking water. Combine the two eluents. Input the two eluents into the reaction kettle, adjust the pH value to below 2 with sulfuric acid, add 600-1000L of commercially available sodium hypochlorite solution for oxidation, and filter to obtain crude iodine.

[0063] One embodiment, the wastewater containing organic iodide is sequentially through the wastewater conditioning tank, hydrolysis acidification tank, hydrolysis acidification sedimentation tank, A / O (A / O process connects the front-stage anoxic stage and the rear-stage aerobic stage in series, DO (dissolved oxygen) in A section is not greater than 0.2mg / L, and DO in O section is 0.2mg / L. In the anoxic stage, heterotrophic bacteria hydrolyze starch, fiber, carbohydrates and other suspended pollutants and soluble organic matter in the wastewater into organic acids, so that large molecular organic matter is decomposed into small molecular organic matter, and insoluble organic matter is converted into soluble organic matter. When these hydrolyzed products in the anoxic stage enter the aerobic tank for aerobic treatment, the biodegradability of the wastewater is improved, and the oxygen efficiency is improved. In the anoxic stage, heterotrophic bacteria ammonify (N or amino group in amino acid) protein, fat and other pollutants to free ammonia (NH3, NH4 + ). Under sufficient oxygen supply conditions, autotrophic bacteria oxidize NH3-N (NH4 + ) to NO3 - , which returns to the A tank through reflux control. Under anoxic conditions, heterotrophic bacteria denitrify NO3 -The reduction of molecular nitrogen (N2) completes the cycle of C, N, O in the ecology, realizes the harmless treatment of sewage, and the biochemical treatment is completed after the MBR tank. The concentrated hydrochloric acid is pumped into the reactor at a flow rate of 68.6 L / h, the concentrated hydrochloric acid adjusts the wastewater to be acidic (pH is 2), and the hydrogen peroxide is pumped into the reactor at a flow rate of 4.6 L / h for continuous reaction. And the solution after reaction is continuously pumped from the pipeline reactor into the resin column (loaded with resin 4.5 m 3 ). The liquid alkali is pumped into the discharge pipe of the resin column, and the flow rate of the liquid alkali metering pump is adjusted to make the pH value of the aqueous solution at the discharge port about 6. When the resin column is used for 200 hours, stop adsorption, pump about 4000 L of 5% sodium hydroxide solution into the resin column for desorption, and then wash with about 4000 L of drinking water. Combine the two eluents. The two eluents are input into the reaction kettle, the pH value is adjusted to 1 with hydrochloric acid, 150-300 L of hydrogen peroxide is added for oxidation, and the crude iodine is obtained by suction filtration.

[0064] In one specific embodiment, the wastewater containing organic iodide is sequentially subjected to a wastewater conditioning tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the front-stage anoxic section and the rear-stage aerobic section in series, the DO (dissolved oxygen) in the A section is not greater than 0.2 mg / L, and the DO in the O section is 2 mg / L. In the anoxic section, the heterotrophic bacteria hydrolyze starch, fiber, carbohydrates and other suspended pollutants and soluble organic matter in the wastewater into organic acids, decompose large molecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these hydrolyzed products in the anoxic section enter the aerobic tank for aerobic treatment, the biodegradability of the wastewater is improved, and the oxygen efficiency is improved. In the anoxic section, the heterotrophic bacteria ammonify (N on the organic chain or amino group in the amino acid) to free ammonia (NH3, NH4 + ). Under sufficient oxygen supply conditions, the autotrophic bacteria nitrify NH3-N (NH4 + ) to NO3 - , which returns to the A tank through reflux control. Under anoxic conditions, the heterotrophic bacteria denitrify NO3 - to molecular nitrogen (N2) to complete the cycle of C, N, O in the ecology and realize the harmless treatment of wastewater. The biochemical treatment is completed after the MBR tank, and the wastewater is transported into the pipeline reactor at a flow rate of 15 cubic meters / hour by a pump. The concentrated hydrochloric acid is pumped into the reactor at a flow rate of 68.6 L / h, the concentrated hydrochloric acid adjusts the wastewater to be acidic (pH is 4), and the hydrogen peroxide is pumped into the reactor at a flow rate of 4.6 L / h for continuous reaction. And the solution after reaction is continuously pumped from the pipeline reactor into the resin column (loaded with resin 4.5 m 3Liquid alkali is pumped into the discharge pipe of the resin column, and the flow rate of the liquid alkali metering pump is adjusted to ensure that the pH of the aqueous solution at the discharge port is around 9. After the resin column has been used for 100 hours, adsorption is stopped, and approximately 4000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. Then, approximately 4000 L of drinking water is used for washing, and the two eluents are combined. The two eluents are then transferred to a reaction vessel, the pH is adjusted to 2 with hydrochloric acid, and 150-300 L of hydrogen peroxide is added for oxidation. The solution is then filtered to obtain elemental iodine.

[0065] In one specific implementation, wastewater containing organic iodides sequentially passes through a wastewater equalization tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O process (the A / O process connects the anoxic section and the aerobic section in series; the dissolved oxygen (DO) in section A is no more than 0.2 mg / L, and the DO in section O is 1 mg / L). In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, and carbohydrates, as well as soluble organic matter, into organic acids, breaking down large organic molecules into smaller ones and converting insoluble organic matter into soluble organic matter. When these products from anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the wastewater is improved, and the oxygen efficiency is increased. In the anoxic section, heterotrophic bacteria also ammonify pollutants such as proteins and fats (by releasing ammonia (NH3, NH4) through ammoniation of nitrogen (N) in organic chains or amino groups in amino acids). + Under sufficient oxygen supply, the nitrification process of autotrophic bacteria will convert NH3-N (NH4+) into nitrogen. + Oxidized to NO3 - The nitrogen is returned to tank A via reflux control. Under anoxic conditions, the denitrification by heterotrophic bacteria removes NO3. - The wastewater is reduced to molecular nitrogen (N2) to complete the C, N, and O cycle in the ecosystem, achieving harmless treatment. After biological treatment in the MBR tank, the wastewater is pumped into the pipeline reactor at a flow rate of 15 cubic meters per hour. Concentrated hydrochloric acid and hydrogen peroxide are pumped into the reactor at flow rates of 68.6 L / h and 4.6 L / h, respectively, for continuous reaction. After the concentrated hydrochloric acid adjusts the mixture to acidity, the hydrogen peroxide begins the oxidation reaction. The resulting solution is then continuously pumped from the pipeline reactor into a resin column (containing 4.5 m³ of resin). 3 Liquid alkali is pumped into the discharge pipe of the resin column, and the flow rate of the liquid alkali metering pump is adjusted to maintain the pH of the aqueous solution at the discharge port at approximately 8. When the wastewater volume passing through the resin column reaches 2000-3000 tons, adsorption is stopped. Approximately 4000L of a 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption, followed by washing with approximately 4000L of drinking water. The two eluents are combined. The two eluents are then transferred to a reaction vessel, the pH is adjusted to 0.5 with hydrochloric acid, and 150-300L of hydrogen peroxide is added for oxidation. The mixture is then filtered to obtain elemental iodine.

[0066] One specific embodiment, the wastewater containing organic iodide is sequentially through wastewater conditioning tank, hydrolysis acidification tank, hydrolysis acidification sedimentation tank, A / O (A / O process will the front stage anoxic and the latter stage aerobic together, A section DO (dissolved oxygen) is not more than 0.2 mg / L, O section DO = 1 mg / L. In the anoxic heterotrophic bacteria will wastewater starch, fiber, carbohydrates and other suspended pollutants and soluble organic matter hydrolysis into organic acid, so that the macromolecular organic matter is decomposed into small molecular organic matter, insoluble organic matter into soluble organic matter, when these anoxic hydrolysis products into the aerobic tank for aerobic treatment, improve the biodegradability of wastewater, improve the efficiency of oxygen; In the anoxic heterotrophic bacteria will protein, fat and other pollutants ammonification (N or amino acid in the organic chain of amino) free ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, autotrophic nitrification of NH3-N (NH4 + ) is oxidized to NO3 - , through the reflux control returns to the A pool, under anoxic conditions, denitrification of heterotrophic bacteria will NO3 - Reduced to molecular nitrogen (N2) to complete the C, N, O in the ecological cycle, to achieve harmless treatment of wastewater), MBR pool after biochemical treatment, with a pump to 15 cubic meters / hour flow rate into the pipeline reactor. Concentrated acid solution (mixed solution of concentrated sulfuric acid and concentrated hydrochloric acid in a ratio of 1:2), hydrogen peroxide are pumped into the reactor at a flow rate of 30 L / h and 4.6 L / h respectively for continuous reaction, the concentrated acid solution will be mixed to acidic, hydrogen peroxide begins to oxidize. And the solution after the reaction from the pipeline reactor is continuously pumped into the resin column (loaded with resin 4.5 m 3 ). The discharge pipe of the resin column is pumped into liquid alkali, adjust the flow of the liquid alkali metering pump, so that the pH value of the effluent is about 8. When the wastewater through the resin column reaches the preset threshold (preset threshold is color, for example, the wastewater appears color), stop adsorption, pump 5% sodium hydroxide solution into the resin column about 3000 L for desorption, and then wash with about 3000 L drinking water, combine the two eluates. The two eluates are input into the reaction kettle, adjust the pH value to 0.5 with hydrochloric acid, add hydrogen peroxide 150-300 L for oxidation, and filter to get iodine.

[0067] One specific embodiment, the wastewater containing organic iodide is sequentially through wastewater conditioning tank, hydrolysis acidification tank, hydrolysis acidification sedimentation tank, A / O (A / O process will the front stage anoxic and the latter stage aerobic together, A section DO (dissolved oxygen) is not more than 0.2 mg / L, O section DO = 1 mg / L. In the anoxic heterotrophic bacteria will wastewater starch, fiber, carbohydrates and other suspended pollutants and soluble organic matter hydrolysis into organic acid, so that the macromolecular organic matter is decomposed into small molecular organic matter, insoluble organic matter into soluble organic matter, when these anoxic hydrolysis products into the aerobic tank for aerobic treatment, improve the biodegradability of wastewater, improve the efficiency of oxygen; In the anoxic heterotrophic bacteria will protein, fat and other pollutants ammonification (N or amino group in the organic chain of amino acid) free ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, autotrophic nitrification of NH3-N (NH4 + ) is oxidized to NO3 - , through the return control returns to the A pool, under anoxic conditions, denitrification of heterotrophic bacteria will NO3 - reduced to molecular nitrogen (N2) to complete the C, N, O in the ecological cycle, to achieve the harmless treatment of wastewater), MBR pool after biochemical treatment, with a pump to 15 cubic meters / hour flow rate into the pipeline reactor. Concentrated acid solution (mixed solution of concentrated phosphoric acid and concentrated hydrochloric acid in a ratio of 1:3), hydrogen peroxide are pumped into the reactor at a flow rate of 50 L / h and 4.6 L / h respectively for continuous reaction, after the concentrated acid solution is adjusted to acidic, hydrogen peroxide starts the oxidation reaction. And the solution after the reaction from the pipeline reactor is continuously pumped into the resin column (loaded with resin 4.5 m 3 ). The discharge pipe of the resin column is pumped into liquid alkali, adjust the flow of the liquid alkali metering pump, so that the pH value of the discharge port aqueous solution is about 8. When the observation window of the resin column appears color (the color of iodine element), stop adsorption, pump 5% sodium hydroxide solution about 5000 L into the resin column for desorption, and then wash with about 5000 L drinking water, combine the two eluates. The two eluates are input into the reaction kettle, adjust the pH value to 0.5 with hydrochloric acid, add hydrogen peroxide 150-300 L for oxidation, and filter to obtain iodine element.

[0068] One specific embodiment, the wastewater containing organic iodide is sequentially through the wastewater conditioning tank, hydrolysis acidification tank, hydrolysis acidification sedimentation tank, A / O (A / O process will be the first stage of anoxic and the latter aerobic section in series, A section DO (dissolved oxygen) is not more than 0.2 mg / L, O section DO = 1 mg / L. In the anoxic heterotrophic bacteria will be in wastewater starch, fiber, carbohydrates and other suspended pollutants and soluble organic matter hydrolysis of organic acids, so that the macromolecular organic matter into small molecular organic matter, insoluble organic matter into soluble organic matter, when these anoxic hydrolysis of the products into the aerobic tank for aerobic treatment, improve the biodegradability of wastewater, improve the efficiency of oxygen; in the anoxic heterotrophic bacteria will be protein, fat and other pollutants ammonification (N or amino acid in the organic chain of amino) free ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, autotrophic nitrification of NH3-N (NH4 + ) oxidation of NO3 - , through the return control to the A pool, under anoxic conditions, denitrifying bacteria denitrification of NO3 - reduced to molecular nitrogen (N2) to complete the C, N, O in the ecological cycle, to achieve the harmless treatment of wastewater), MBR pool after biochemical treatment, with a pump at a flow rate of 15 cubic meters / hour into the pipeline reactor. Concentrated hydrochloric acid, oxidizing agent (a mixture of sodium hypochlorite and sodium nitrite mixed solution according to the ratio of 1:1 mixed solution) are pumped into the reactor at a flow rate of 68.6 L / h and 5.8 L / h for continuous reaction, concentrated hydrochloric acid to adjust the mixture to acidic, oxidizing agent starts the oxidation reaction. And the reaction solution from the pipeline reactor is continuously pumped into the resin column (resin 4.5 m 3 ) inside. Pump liquid alkali in the discharge pipe of the resin column, adjust the flow of the liquid alkali metering pump, so that the pH value of the water solution at the discharge port is about 8. When the iodine is detected in the liquid through the resin column, stop adsorption, pump about 3500 L of 5% sodium hydroxide solution into the resin column for desorption, and then wash with about 3500 L of drinking water. Combine the two eluents. Input the two eluents into the reaction kettle, adjust the pH value to 0.5 with hydrochloric acid, add 150-300 L of hydrogen peroxide for oxidation, and filter to obtain iodine.

[0069] The iodine monovalent currently sold on the market is 550-650 thousand yuan per ton, and the recovery method of the present application can achieve good economic benefits. For example, for 1000 tons of wastewater containing organic iodide with a concentration of about 800 ppm treated per day, the mass of iodine monovalent or coarse iodine recovered from the wastewater per month is 10-12 tons, that is, the economic benefits of 5-8 million yuan per month can be obtained by recovering iodine; and with the increase of the daily treatment capacity and the concentration of organic iodide, the amount of recovery will also be correspondingly increased. The recovery method of the present application can achieve commercial success, and has outstanding substantial features and significant progress compared with the existing wastewater treatment method.

[0070] In addition, it should be noted that the specific embodiments described in the specification, the shape of the components, the name taken, etc. can be different. Any equivalent or simple change made according to the structure, features and principles described in the patent concept of the present application is included in the protection scope of the present application. Those skilled in the art can make various modifications or supplements to the described specific embodiments or use similar ways to replace, as long as it does not deviate from the structure of the present application or exceed the scope defined by the present claims, which shall belong to the protection scope of the present application.

Claims

1. A method for recovering iodine from wastewater containing organic iodides, characterized in that, include: Biochemical treatment: Wastewater containing organic iodides is treated using an anaerobic process to convert the organic iodides in the wastewater into inorganic iodide ions and to reduce the chemical oxygen demand of the wastewater to less than or equal to 2000 mg / L; after anaerobic treatment, it is treated using an aerobic or facultative process, and the dissolved oxygen in the aerobic or facultative process is less than 2 mg / L. Oxidative adsorption: The pH value of the biochemically treated wastewater is adjusted to acidic and then oxidized to convert inorganic iodide ions into iodine, which is then adsorbed by an adsorption device. Desorption and recovery: Desorption is performed on the adsorption device, the pH of the eluent obtained from desorption is adjusted to acidity, and then oxidized and filtered to obtain crude iodine or elemental iodine.

2. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, The biochemically treated wastewater is transported to a continuous flow reactor for oxidation and adsorption treatment.

3. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, The biochemically treated wastewater is transported to a reaction vessel for oxidation and adsorption treatment.

4. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, The dissolved oxygen is less than 1 mg / L.

5. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, The pH value is adjusted to 0-5 during the oxidation adsorption treatment.

6. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, The pH value is adjusted to 0-5 during the desorption and recovery process.

7. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, The adsorption device is equipped with an adsorbent, which may include macroporous adsorption resin, activated carbon, or diatomaceous earth.

8. The method for recovering iodine from wastewater containing organic iodides according to claim 1, characterized in that, Adsorption stops when the wastewater passing through the adsorption device reaches a preset threshold or when the adsorption device reaches a preset threshold.

9. The method for recovering iodine from wastewater containing organic iodides according to claim 2, characterized in that, The continuous flow reactor is equipped with a flow turbulence device, which is used to adjust the flow rate of wastewater in the continuous flow reactor to a Reynolds number of 60,000-140,000.

10. The method for recovering iodine from wastewater containing organic iodides according to claim 5, characterized in that, Adjust the pH value to 2-3.

11. The method for recovering iodine from wastewater containing organic iodides according to claim 6, characterized in that, Adjust the pH value to 2-3.

12. The method for recovering iodine from wastewater containing organic iodides according to claim 7, characterized in that, The adsorbent is a macroporous adsorption resin, and the adsorption device is a resin column.

13. The method for recovering iodine from wastewater containing organic iodides according to any one of claims 1-12, characterized in that, It includes anaerobic devices, aerobic or facultative anaerobic devices, separation devices, reaction devices, adsorption devices, and recovery devices.

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