Method and system for recovering iodine from wastewater containing organic iodide

Abstract

The invention discloses a method and a system for recovering iodine from wastewater containing organic iodide, and iodine elementary substance or crude iodine is recovered from the wastewater containing the organic iodide through three steps of biochemical treatment, oxidative adsorption and desorption recovery. The iodine recovery of large-flow industrial wastewater is realized by utilizing the continuous flow reactor.

Description

Technical Field

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

[0002] my country is short of iodine resources, with approximately 90% of its iodine supply imported. Therefore, the recycling of iodine resources is particularly important. The treatment of wastewater containing organic iodides is a complex production technology challenge. Improper biochemical treatment of such wastewater can produce elemental iodine, which can disrupt the biochemical system and cause its collapse. Currently, organic iodides are typically separated from wastewater through concentration, which consumes significant amounts of energy. Iodine recovery typically involves zinc powder reduction to convert the organic iodides into inorganic iodides, which are then acidified and oxidized to yield elemental iodine. This reduction process inevitably produces a significant amount of solid waste, including zinc salts, which places significant pressure on the environment. Summary of the Invention

[0003] The present invention aims to solve the problem that the existing iodine recovery from wastewater containing organic iodides consumes a lot of energy or causes great pollution.

[0004] To solve the above technical problems, the present invention provides a method and system for recovering iodine from wastewater containing organic iodides.

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

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

[0007] 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 reduce the chemical oxygen demand (COD) in the wastewater to less than or equal to 2000 mg / L. After anaerobic treatment, the wastewater is treated using an aerobic or facultative aerobic process, where the dissolved oxygen level is less than 2 mg / L. Anaerobic treatment can reduce the COD in the wastewater to less than or equal to 2000 mg / L, and aerobic or facultative aerobic treatment further reduces the COD.

[0008] Oxidative adsorption: The pH value of the biochemically treated wastewater is adjusted to acidic and then oxidized to convert inorganic iodide ions into iodine, and the iodine is adsorbed using an adsorption device.

[0009] Desorption and recovery: desorb the adsorption device, adjust the pH value of the eluate obtained by desorption to acidic, then oxidize it and filter it to obtain crude iodine or elemental iodine.

[0010] Preferably, the wastewater that has undergone biochemical treatment is transported to a continuous flow reactor, where it undergoes oxidative adsorption treatment.

[0011] Preferably, the biochemically treated wastewater is transported to a reactor and subjected to oxidative adsorption treatment in the reactor.

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

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

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

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

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

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

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

[0019] Preferably, in the oxidative adsorption treatment, an oxidizing reaction is carried out by adding an oxidizing agent, and the oxidizing agent includes hydrogen peroxide, chlorine, sodium hypochlorite, or sodium nitrite.

[0020] Preferably, in the desorption recovery process, an oxidation reaction is carried out by adding an oxidant, and the oxidant includes hydrogen peroxide, chlorine, sodium hypochlorite, or sodium nitrite.

[0021] Preferably, the continuous flow reactor is provided with a flow disturbing device, which is used to generate turbulence in the liquid in the continuous flow reactor.

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

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

[0024] A system for recovering iodine from wastewater containing organic iodides is used to implement the method for recovering iodine from wastewater containing organic iodides, comprising an anaerobic device, an aerobic device or an anaerobic 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 a flow disturbance device is provided in the continuous flow reactor. The flow disturbance device is used to adjust the flow rate of the 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 method directly biochemically treats wastewater containing organic iodides, converting them into inorganic iodides. The organic iodides are then acidified and oxidized to elemental iodine, which is then enriched using an adsorption device. This process avoids energy-intensive concentration, and the conversion of organic iodides to inorganic iodides does not involve chemical reduction methods such as zinc powder or incineration. Instead, the physical properties of the adsorption device are used to adsorb and enrich the iodine. The overall solution offers low energy consumption, minimal pollution, and low cost, making it particularly suitable for treating large volumes of wastewater containing organic iodides and recovering iodine. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0030] Figure 1 It is a schematic diagram of the process of the present invention. DETAILED DESCRIPTION

[0031] The present invention will be further described in detail below with reference to the examples. The following examples are intended to explain the present invention but the present invention is not limited to the following examples.

[0032] Example:

[0033] A method for recovering iodine from wastewater containing organic iodide, comprising:

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

[0035] Oxidation adsorption: The pH value of the biochemically treated wastewater is adjusted to acidic and then oxidized. The oxidized wastewater is adsorbed by an adsorption device to absorb iodine;

[0036] Desorption and recovery: desorb the adsorption device, adjust the pH value of the eluate obtained by desorption to acidic, then oxidize it and filter it to obtain elemental iodine.

[0037] In one or more embodiments, the organic iodides in the wastewater include iodine contrast agents and their intermediates, iodobenzene, and the like. The wastewater generated primarily includes filter press wastewater from the iodine contrast agent iodination process; filter press wastewater before and after decolorization from the acylation and hydrolysis processes; vacuum distillation wastewater, resin regeneration and cleaning wastewater, and thin-film evaporation wastewater from the condensation process; atmospheric distillation wastewater after resin regeneration and cleaning, thin-film evaporation wastewater, resin regeneration and cleaning wastewater after desalination, and the final ultrafiltration wastewater from the refining process. The wastewater has a high COD concentration, for example, 20,000 mg / L.

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

[0039] In one or more embodiments, the anaerobic process, also known as the anoxic process, refers to the process of decomposing various complex organic substances in wastewater into substances such as methane and carbon dioxide through the action of anaerobic microorganisms under conditions without molecular oxygen. Specifically, it refers to the use of the metabolic characteristics of anaerobic microorganisms. These microorganisms, in an oxygen-deficient environment, gradually convert long-chain hydrocarbons, aromatic compounds and other macromolecular organic substances into methane, carbon dioxide, water, hydrogen sulfide and ammonia through a series of complex biochemical reactions. This process significantly reduces the biological toxicity of wastewater and greatly improves the biodegradability of wastewater, making the wastewater that was originally difficult to treat easier to be accepted and degraded by subsequent biological treatment processes. In addition, the hydrolysis and acidification process is also accompanied by the removal of some organic matter, which further reduces the burden on subsequent treatment units, provides them with more stable and high-quality water inlet conditions, and improves the treatment efficiency of the entire wastewater treatment system.

[0040] In one or more embodiments, the anaerobic process can be divided into three stages: a hydrolysis and acidification stage, an acetogenesis stage, and a methanogenesis stage. (1) Hydrolysis and acidification stage: Hydrolysis can be defined as the process by which complex insoluble polymers are converted into simple soluble monomers or dimers. Due to their large relative molecular weight, high molecular weight organic matter cannot pass through the cell membrane and therefore cannot be directly utilized by bacteria. In the first stage, they are decomposed into small molecules by bacterial extracellular enzymes. For example, cellulose is hydrolyzed into cellobiose and glucose by cellulase, starch is decomposed into maltose and glucose by amylase, and protein is hydrolyzed into short peptides and amino acids by protease. These small molecular hydrolysis products can dissolve in water and pass through the cell membrane for use by bacteria. The hydrolysis process is usually slow and is therefore considered to be the rate-limiting stage for the anaerobic degradation of wastewater containing high molecular weight organic matter or suspended matter. Various factors such as temperature, composition of organic matter, concentration of hydrolysis products, etc. may affect the rate and degree of hydrolysis. The hydrolysis rate can be described by the following kinetic equation: p = po / (1 + Kh.T), where p represents the concentration of the 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 biodegradation process in which organic compounds act as both electron acceptors and electron donors, converting soluble organic matter into end products primarily composed of volatile fatty acids. During this stage, fermentative bacteria (i.e., acidifying bacteria) convert these small molecules into simpler compounds within their cells and secrete them extracellularly. While the vast majority of fermentative bacteria are strict anaerobes, approximately 1% of facultative anaerobes are present in anaerobic environments. These facultative anaerobes protect strict anaerobes, such as methanogens, from oxygen damage and inhibition. The main products of this stage include volatile fatty acids, alcohols, lactic acid, carbon dioxide, hydrogen, ammonia, and hydrogen sulfide. The product composition depends on the anaerobic degradation conditions, substrate type, and the microbial population involved in the acidification. (2) Acetogenesis: Under the action of hydrogen-producing acetogenic bacteria, the products of the previous stage are further converted into acetic acid, hydrogen, carbonic acid, and new cellular substances. (3) Methane stage: In this stage, acetic acid, hydrogen, carbonic acid, formic acid, and methanol are converted into methane, carbon dioxide, and new cellular substances. The process of methane bacteria converting acetic acid, acetate, carbon dioxide, and hydrogen into methane is completed by two physiologically different methanogens. One group converts hydrogen and carbon dioxide into methane, and the other group produces methane from acetic acid or acetate decarboxylation. The former accounts for about 1 / 3 of the total, and the latter accounts for about 2 / 3.

[0041] In one or more embodiments, the microorganisms involved in anaerobic biological treatment are mainly bacteria, which can be divided into two major categories: non-methanogenic bacteria (acid-producing bacteria) and methanogenic bacteria. Non-methanogenic bacteria are mainly composed of obligate anaerobes and facultative anaerobes, and there are about 18 genera and more than 50 species. Among them, the former mainly include Clostridium, Bacteroides, Bifidobacterium, Corynebacterium and Actinomyces. The latter mainly include Proteus, Pseudomonas, Bacillus, Streptococcus, Flavobacterium, Pseudomonas, Aerobacterium and the like. Common methanogenic bacteria are mainly divided into four categories: Methanobacterium, Methanococcus, Methanosarcina, and Methanospirillum.

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

[0043] In one or more embodiments, the aerobic process 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, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , this process requires the participation of oxygen.

[0044] In one or more embodiments, the microorganisms in aerobic treatment are mainly bacteria (mainly aerobic heterotrophic bacteria) and protozoa, in addition to yeast, filamentous mold, unicellular algae, rotifers, nematodes, etc. Bacteria account for 90% of the total number of microorganisms, with a number of 10 8 -10 9 The most common dominant species are Alcaligenes, Bacillus, Flavobacterium, Pseudomonas, and Zoogloea. Others include Achromobacter, Nocardia, Bdellovibrio, Nitrifying Bacterium, and Escherichia coli. These are all chemoheterotrophic bacteria, most of which are Gram-negative and can effectively decompose organic pollutants in wastewater.

[0045] In one or more embodiments, facultative aerobic process refers to the process of simultaneously carrying out aerobic and anaerobic treatment of organic matter in wastewater using facultative anaerobic bacteria (bacteria that can carry out aerobic respiration and can also carry out anaerobic respiration). In the prior art, the COD of industrial wastewater after anaerobic treatment is generally 4000-6000mg / L, so it must be treated with aerobic process to reduce COD to the required numerical value, that is, aerobic process must also be used after using facultative aerobic process treatment. The present invention can reduce COD to 2000mg / L and below by using facultative aerobic process or aerobic process alone, that is, it is not necessary to use aerobic process treatment after using facultative aerobic process treatment. In one or more embodiments, the technical means implemented by increasing the residence time of anaerobic process treatment or increasing the volume of anaerobic process treatment device and other means that can increase anaerobic process treatment capacity are all, and then COD is reduced to 2000mg / L and below in the anaerobic process stage.

[0046] In one or more embodiments, the dissolved oxygen in the aerobic process or the anaerobic process is less than 2 mg / L. The dissolved oxygen in the aerobic process in the prior art is 2-4 mg / L. The wastewater containing organic iodide after being treated by the existing aerobic process or the anaerobic process will oxidize the inorganic iodide ions in the wastewater into elemental iodine. The elemental iodine has the physical property of sterilization and will destroy the microorganisms required for the anaerobic process, the aerobic process or the anaerobic process, thereby making the entire biochemical treatment unable to work normally. Therefore, in this embodiment, the dissolved oxygen in the aerobic process or the anaerobic process is less than 2 mg / L, which can not only avoid the generation of elemental iodine in the biochemical treatment, but also reduce the COD of the wastewater to the required value, such as 400-600 mg / L, through the biochemical treatment.

[0047] In one or more embodiments, the production wastewater containing organic iodide is biochemically treated, transferred to a reactor or a continuous reactor, the pH value is adjusted to acidic with acid, an appropriate amount of oxidant is added, and after a period of reaction, it is transferred to an adsorption device equipped with an adsorbent for iodine adsorption; repeat the above steps, and after the adsorption is close to saturation, the iodine on the adsorption device is desorbed with an alkaline aqueous solution, the alkaline eluent is adjusted to acidic with acid, and an appropriate amount of oxidant is added to oxidize to obtain elemental iodine, which is filtered to obtain crude iodine. Preferably, due to the large discharge volume of production wastewater, more reactors are required for acidification reaction, and it needs to be repeated many times, which is time-consuming and labor-intensive. A continuous reactor such as a column reactor, a tubular reactor, or a grid reactor is used for continuous flow reaction, which can be conveniently processed. Preferably, the adsorbent can be selected from macroporous adsorption resin, activated carbon, diatomaceous earth, etc., and the adsorbent can be loaded into a column to facilitate adsorption. Preferably, the adsorbent is a macroporous adsorption resin, and the adsorption device is a macroporous adsorption resin column. Preferably, the acid for adjusting the pH value can be hydrochloric acid (including dilute hydrochloric acid, concentrated hydrochloric acid, or concentrated hydrochloric acid diluted with water), sulfuric acid (including dilute sulfuric acid, concentrated sulfuric acid, or concentrated sulfuric acid diluted with water), phosphoric acid (including dilute phosphoric acid, concentrated phosphoric acid, or concentrated phosphoric acid diluted with water), or a mixed solution of two or more acids (such as a mixed solution of hydrochloric acid and sulfuric acid), preferably hydrochloric acid. Preferably, the pH value is adjusted to an acidic state, preferably below 4, more preferably between 2 and 4. Preferably, the oxidant can be hydrogen peroxide, chlorine, sodium hypochlorite, sodium nitrite, or any combination that does not produce a chemical reaction (such as a mixed solution of sodium hypochlorite and sodium nitrite), preferably hydrogen peroxide.

[0048] In one embodiment, the wastewater containing organic iodide is biochemically treated at the factory sewage station, and then pumped into a reactor (6.5 tons), adjusted to a pH value below 2 with about 30L of concentrated hydrochloric acid, and 2.8L of hydrogen peroxide is added. The oxidation reaction is carried out for 20-30 minutes, and the oxidized wastewater is pumped into a resin column. 3 ) adsorbs elemental iodine, and the adsorbed wastewater is adjusted to a pH of 6-9 with an aqueous sodium hydroxide solution and discharged into a sewage pool. The above steps are repeated until the amount of wastewater passing through the adsorption resin column reaches a preset threshold (the preset threshold is the amount of wastewater passing through, for example, 1200-1500 tons of wastewater). Desorption is then performed with approximately 4000 L of a 5% aqueous sodium hydroxide solution, followed by washing with approximately 4000 L of drinking water. The eluates are combined, the pH is adjusted to below 2 with concentrated hydrochloric acid, and 150-300 L of hydrogen peroxide is added for oxidation, followed by filtration to obtain crude iodine.

[0049] In one embodiment, wastewater containing organic iodides is biochemically treated at a factory sewage station and then pumped into a 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 to adjust the wastewater to acidity (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 4.5 m3 of resin). 3 The adsorbed wastewater flows out through the resin column's discharge pipe, and liquid caustic soda is pumped into the resin column's discharge pipe. The flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port between 6 and 9. When the resin column has passed 1,200 tons of wastewater, adsorption is stopped, and approximately 4,000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 4,000 L of drinking water. The two eluates are combined, the pH value is adjusted to below 2 with hydrochloric acid, and 150-300 L of hydrogen peroxide is added for oxidation. Crude iodine is then filtered to obtain.

[0050] In one embodiment, wastewater containing organic iodides is biochemically treated at a factory sewage station and then 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). Commercially available 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 4.5 m3 of resin) 3 The adsorbed wastewater flows out through the resin column's discharge pipe, and liquid caustic soda is pumped into the resin column's discharge pipe. The flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port between 6 and 9. When the resin column has passed 1,300 tons of wastewater, adsorption is stopped, and approximately 4,000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 4,000 L of drinking water. The two eluates are combined, the pH value is adjusted to below 2 with sulfuric acid, and 300-500 L of commercially available sodium hypochlorite solution is added for oxidation. Crude iodine is then filtered to obtain.

[0051] In one embodiment, wastewater containing organic iodides is biochemically treated at a factory sewage station and then pumped into a 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 to adjust the wastewater to acidity (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 4.5 m3 of resin). 3The adsorbed wastewater flows out through the resin column's discharge pipe, and liquid caustic soda is pumped into the resin column's discharge pipe. The flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port between 6 and 9. When the resin column has passed 1,500 tons of wastewater, adsorption is stopped, and approximately 4,000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 4,000 L of drinking water. The two eluates are combined, the pH value is adjusted to below 2 with sulfuric acid, and 600-1,000 L of commercially available sodium hypochlorite solution is added for oxidation. Crude iodine is then filtered to obtain.

[0052] In one embodiment, wastewater containing organic iodides is biochemically treated at a factory sewage station and then 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 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 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 so that the pH value of the aqueous solution at the discharge port is between 6 and 9. When the amount of wastewater passing through the resin column reaches a preset threshold (the preset threshold is the passing time, for example, the passing time is 50-100 hours), the adsorption is stopped, and about 4000L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption, and then washed with about 4000L of drinking water. The two eluates are combined, the pH value 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.

[0053] A system for recovering iodine from wastewater containing organic iodides is used to implement the method for recovering iodine from wastewater containing organic iodides. The system comprises an anaerobic device, an aerobic device or an anaerobic device, a separation device, a reaction device, an adsorption device and a recovery device. The wastewater passes through the anaerobic device, the aerobic device or the anaerobic device, the separation device, the reaction device, the adsorption device and the recovery device in sequence.

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

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

[0056] In one or more embodiments, the adsorption device is an adsorption column, and the recovery device is a reactor.

[0057] In one or more embodiments, a flow disruptor is provided in the continuous flow reactor, and the flow disruptor is used to cause the liquid in the continuous flow reactor to produce turbulence, and the Reynolds number of the wastewater flow rate in the continuous flow reactor is 60000-140000, which can ensure the sufficient mixing of wastewater and oxidant and ensure that the oxidation reaction is complete. Preferably, the Reynolds number is 70000-90000. The lower the Reynolds number, the insufficient mixing of wastewater and oxidant, resulting in an increase in the duration of the oxidation reaction, and then the length of the reactor needs to be increased, resulting in an increase in cost and a decrease in economic benefit. If the Reynolds number is too high, a more complicated flow disruptor is needed, resulting in an increase in cost and a decrease in economic benefit. The flow disruptor can adopt a structure that can meet the above-mentioned Reynolds number requirement, such as a blade, a wire mesh, etc.

[0058] In one or more embodiments, the size and specifications of the continuous reactor can be adjusted according to the wastewater treatment requirements. Preferably, a tubular reactor is used, including a horizontal tubular reactor, a vertical tubular reactor, a coil reactor, a U-shaped tubular reactor, etc. In order to make the equipment compact and save space, a coil 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 a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (the A / O process connects the front anoxic section and the rear aerobic section in series, the DO (dissolved oxygen) of the A section is not greater than 0.2 mg / L, and the DO of 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-methanogenic bacteria distributed in the hydrolysis acidification tank, the treatment capacity of the anaerobic process is increased, and COD can be reduced. To below 2000mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in sewage into organic acids, decompose macromolecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of sewage and the oxidation efficiency are improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 -Reduced to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and transported into the pipeline reactor with a pump at a flow rate of 15 cubic meters / hour. Concentrated hydrochloric acid is pumped into the reactor at a rate of 68.6L / h. Concentrated hydrochloric acid adjusts the wastewater to acidity (pH 2-4), and hydrogen peroxide is pumped into the reactor at a flow rate of 4.6L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 Liquid caustic soda is pumped into the discharge pipe of the resin column, and the flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port between 6 and 9. After the resin column has passed wastewater for 50 hours, adsorption is stopped, and approximately 4000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 4000 L of drinking water, and the two eluates are combined. The two eluates are input into a reactor, the pH value is adjusted to below 2 with hydrochloric acid, and 150-300 L of hydrogen peroxide is added for oxidation. 368 kg of crude iodine with a purity of 92.1% is obtained by filtration.

[0061] In one embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank (the hydrolysis acidification tank belongs to an anaerobic device, and anaerobic bacteria are distributed in the hydrolysis acidification tank and the anoxic section. Compared with the existing non-methanogenic bacteria distributed in the hydrolysis acidification tank, the processing capacity of the anaerobic process is increased, and COD can be reduced to below 2000 mg / L), a hydrolysis acidification sedimentation tank, a primary A / O, an intermediate sedimentation tank, and a secondary A / O (the structures of the primary A / O and the secondary A / O can be the same or different, for example, In the implementation method, the first-stage A / O and the second-stage A / O have the same structure and the same treatment time), final sedimentation tank, MBR tank (MBR membrane technology first uses activated sludge to remove biodegradable organic pollutants in the water, and then uses membrane components to forcibly intercept the activated sludge and most of the suspended solids in the bioreactor to achieve solid-liquid separation of purified water and activated sludge, thereby strengthening the biochemical reaction, improving the sewage treatment effect and effluent water quality), and then the biochemical treatment is completed and pumped into the pipeline reactor at a flow rate of 15 cubic meters / hour. Concentrated hydrochloric acid is pumped into the reactor at a rate of 68.6L / h. Concentrated hydrochloric acid adjusts the wastewater to acidic (pH 2), and hydrogen peroxide is pumped into the reactor at a flow rate of 4.6L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 Liquid caustic soda is pumped into the discharge pipe of the resin column, and the flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port between 6 and 9. After the resin column has passed wastewater for 100 hours, adsorption is stopped, and approximately 4000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 4000 L of drinking water, and the two eluates are combined. The two eluates are input into a reactor, the pH value is adjusted to below 2 with hydrochloric acid, and 150-300 L of hydrogen peroxide is added for oxidation. Crude iodine is then filtered to obtain.

[0062] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, a primary A / O, an intermediate sedimentation tank, a secondary A / O (the structures of the primary A / O and the secondary A / O are different in this embodiment, and the treatment time is different), a final sedimentation tank, an MBR tank (MBR membrane technology first uses activated sludge to remove biodegradable organic pollutants in the water, and then uses a membrane component to forcibly intercept the activated sludge and most of the suspended solids in the bioreactor to achieve solid-liquid separation of purified water and activated sludge, thereby strengthening the biochemical reaction and improving the sewage treatment effect and effluent water quality) to complete the biochemical treatment and be pumped into a 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 acidity (pH 3). Sodium hypochlorite is pumped into the reactor at a flow rate of 10L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into a resin column (containing 4.5m resin) 3 ). Liquid caustic soda is pumped into the discharge pipe of the resin column, and the flow rate of the liquid caustic soda metering pump is adjusted so that the pH value of the aqueous solution at the discharge port is between 6 and 9. When the resin column reaches a preset threshold value (the preset threshold value is the service life of the resin column, for example, 100-200 hours), adsorption is stopped, and about 4000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption, and then washed with about 4000 L of drinking water, and the two eluates are combined. The two eluates are input into the reactor, the pH value is adjusted to below 2 with sulfuric acid, 600-1000 L of commercially available sodium hypochlorite solution is added for oxidation, and crude iodine is obtained by suction filtration.

[0063] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the anoxic section in front and the aerobic section in back in series, with the DO (dissolved oxygen) of the A section not exceeding 0.2 mg / L and the DO of the O section being 0.2 mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in the sewage into organic acids, decompose macromolecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage is improved and the efficiency of oxygen is improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 -Reduced to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and transported into the pipeline reactor with a pump at a flow rate of 15 cubic meters / hour. Concentrated hydrochloric acid is pumped into the reactor at a rate of 68.6L / h. Concentrated hydrochloric acid adjusts the wastewater to acidity (pH 2), and hydrogen peroxide is pumped into the reactor at a flow rate of 4.6L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 Pump liquid caustic soda into the discharge pipe of the resin column, adjusting the flow rate of the liquid caustic soda metering pump to maintain a pH of approximately 6 at the discharge port. After the resin column has been in use for 200 hours, stop adsorption and pump approximately 4000 L of 5% sodium hydroxide aqueous solution into the resin column for desorption. Rinse with approximately 4000 L of drinking water, and combine the two eluates. Transfer the two eluates to a reactor, adjust the pH to 1 with hydrochloric acid, and oxidize with 150-300 L of hydrogen peroxide. Filter to obtain crude iodine.

[0064] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the anoxic section in front and the aerobic section in back in series, with the DO (dissolved oxygen) of the A section not exceeding 0.2 mg / L and the DO of the O section being 2 mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in the sewage into organic acids, decompose macromolecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage is improved and the efficiency of oxygen is improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 - Reduced to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and transported into the pipeline reactor with a pump at a flow rate of 15 cubic meters / hour. Concentrated hydrochloric acid is pumped into the reactor at a rate of 68.6L / h. Concentrated hydrochloric acid adjusts the wastewater to acidity (pH 4), and hydrogen peroxide is pumped into the reactor at a flow rate of 4.6L / h for continuous reaction. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3Pump liquid caustic soda into the discharge pipe of the resin column, adjusting the flow rate of the liquid caustic soda metering pump so that the pH value of the aqueous solution at the discharge port is around 9. After the resin column has been in use for 100 hours, stop adsorption and pump approximately 4000L of 5% sodium hydroxide aqueous solution into the resin column for desorption. Then, wash with approximately 4000L of drinking water, and combine the two eluates. Transfer the two eluates to a reactor, adjust the pH to 2 with hydrochloric acid, and add 150-300L of hydrogen peroxide for oxidation. Filter to obtain elemental iodine.

[0065] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the anoxic section in front and the aerobic section in back in series, the DO (dissolved oxygen) of the A section is not greater than 0.2 mg / L, and the DO of the O section is 1 mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in the sewage into organic acids, decompose large molecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage is improved and the efficiency of oxygen is improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 - Reduced to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and transported into the pipeline reactor with a pump at a flow rate of 15 cubic meters / hour. Concentrated hydrochloric acid and hydrogen peroxide are pumped into the reactor at a flow rate of 68.6L / h and 4.6L / h respectively for continuous reaction. After the concentrated hydrochloric acid adjusts the mixed solution to acidity, the hydrogen peroxide begins the oxidation reaction. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 Liquid caustic soda is pumped into the discharge pipe of the resin column, and the flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port at around 8. When the resin column has passed 2,000-3,000 tons of wastewater, adsorption is stopped, and approximately 4,000 L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 4,000 L of drinking water, and the two eluates are combined. The two eluates are input into a reactor, the pH value is adjusted to 0.5 with hydrochloric acid, and 150-300 L of hydrogen peroxide is added for oxidation. Iodine is then filtered to obtain elemental iodine.

[0066] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the anoxic section in front and the aerobic section in back in series, the DO (dissolved oxygen) of the A section is not greater than 0.2 mg / L, and the DO of the O section is 1 mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in the sewage into organic acids, decompose large molecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage is improved and the efficiency of oxygen is improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 - Reduction to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and use a pump to transport it into the pipeline reactor at a flow rate of 15 cubic meters / hour. The concentrated acid solution (a mixed solution of concentrated sulfuric acid and concentrated hydrochloric acid in a ratio of 1:2) and hydrogen peroxide are pumped into the reactor at a flow rate of 30L / h and 4.6L / h respectively for continuous reaction. After the concentrated acid solution adjusts the mixed solution to acidity, the hydrogen peroxide begins to oxidize. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 ). Liquid caustic soda is pumped into the discharge pipe of the resin column, and the flow rate of the liquid caustic soda metering pump is adjusted so that the pH value of the aqueous solution at the discharge port is about 8. When the wastewater passing through the resin column reaches a preset threshold value (the preset threshold value is color, for example, the wastewater appears color), the adsorption is stopped, and about 3000L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption, and then washed with about 3000L of drinking water, and the two eluates are combined. The two eluates are input into the reactor, the pH value is adjusted to 0.5 with hydrochloric acid, 150-300L of hydrogen peroxide is added for oxidation, and iodine is obtained by filtration.

[0067] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the anoxic section in front and the aerobic section in back in series, the DO (dissolved oxygen) of the A section is not greater than 0.2 mg / L, and the DO of the O section is 1 mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in the sewage into organic acids, decompose large molecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage is improved and the efficiency of oxygen is improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 - Reduction to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and use a pump to transport it into the pipeline reactor at a flow rate of 15 cubic meters / hour. The concentrated acid solution (a mixed solution of concentrated phosphoric acid and concentrated hydrochloric acid in a ratio of 1:3) and hydrogen peroxide are pumped into the reactor at a flow rate of 50L / h and 4.6L / h respectively for continuous reaction. After the concentrated acid solution adjusts the mixed solution to acidity, the hydrogen peroxide begins to oxidize. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 ). Pump liquid caustic soda into the discharge pipe of the resin column, and adjust the flow rate of the liquid caustic soda metering pump so that the pH value of the aqueous solution at the discharge port is around 8. When color (the color of elemental iodine) appears on the observation window of the resin column, stop adsorption, pump about 5000L of 5% sodium hydroxide aqueous solution into the resin column for desorption, and then wash with about 5000L of drinking water, and combine the two eluates. Input the two eluates into the reactor, adjust the pH value to 0.5 with hydrochloric acid, add 150-300L of hydrogen peroxide for oxidation, and filter to obtain elemental iodine.

[0068] In a specific embodiment, wastewater containing organic iodide passes through a wastewater regulating tank, a hydrolysis acidification tank, a hydrolysis acidification sedimentation tank, and an A / O (A / O process connects the anoxic section in front and the aerobic section in back in series, the DO (dissolved oxygen) of the A section is not greater than 0.2 mg / L, and the DO of the O section is 1 mg / L. In the anoxic section, heterotrophic bacteria hydrolyze suspended pollutants such as starch, fiber, carbohydrates and soluble organic matter in the sewage into organic acids, decompose large molecular organic matter into small molecular organic matter, and convert insoluble organic matter into soluble organic matter. When these products of anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage is improved and the efficiency of oxygen is improved; in the anoxic section, heterotrophic bacteria ammine (N on the organic chain or amino group in amino acid) pollutants such as protein and fat to release ammonia (NH3, NH4 + ), under sufficient oxygen supply conditions, the nitrification of autotrophic bacteria converts NH3-N (NH4 + ) is oxidized to NO3 - , returned to pool A through reflux control, under anoxic conditions, the denitrification of heterotrophic bacteria converts NO3 - Reduced to molecular nitrogen (N2) to complete the cycle of C, N, and O in the ecology and achieve harmless sewage treatment), complete biochemical treatment after the MBR pool, and transported into the pipeline reactor with a pump at a flow rate of 15 cubic meters per hour. Concentrated hydrochloric acid and oxidant (a mixed solution of sodium hypochlorite and sodium nitrite in a ratio of 1:1) are pumped into the reactor at a flow rate of 68.6L / h and 5.8L / h respectively for continuous reaction. After the concentrated hydrochloric acid adjusts the mixed solution to acidity, the oxidant begins the oxidation reaction. The reacted solution is continuously pumped from the pipeline reactor into the resin column (containing 4.5m 3 Liquid caustic soda is pumped into the discharge pipe of the resin column, and the flow rate of the liquid caustic soda metering pump is adjusted to keep the pH value of the aqueous solution at the discharge port at approximately 8. When elemental iodine is detected in the liquid passing through the resin column, adsorption is stopped, and approximately 3500L of 5% sodium hydroxide aqueous solution is pumped into the resin column for desorption. The resin column is then washed with approximately 3500L of drinking water, and the two eluates are combined. The two eluates are input into a reactor, the pH value is adjusted to 0.5 with hydrochloric acid, and 150-300L of hydrogen peroxide is added for oxidation. The iodine is then filtered to obtain elemental iodine.

[0069] The current commercial unit price of iodine is 550,000 yuan / ton to 650,000 yuan / ton. Using the recovery method of the present invention, good economic benefits can be achieved. For example, for a wastewater treatment capacity of about 1,000 tons per day and a concentration of about 800 ppm of organic iodide, the mass of elemental iodine or crude iodine that can be recovered from the wastewater each month is 10 to 12 tons, that is, the economic benefits of 5 million to 8 million yuan can be generated by recovering iodine each month; and as the daily processing capacity and the concentration of organic iodide increase, the amount recovered will also increase accordingly. The recovery method of the present invention can achieve commercial success and has outstanding substantive characteristics and significant progress relative to existing wastewater treatment methods.

[0070] Furthermore, it should be noted that the specific embodiments described in this specification may vary in the shapes and names of their components. Any equivalent or simple variations based on the structure, features, and principles described in the patented concept of this invention are included within the scope of protection of this patent. Persons skilled in the art may make various modifications, additions, or substitutions to the described specific embodiments, and these modifications, as long as they do not deviate from the structure of the invention or exceed the scope defined by the claims, shall fall within the scope of protection of this invention.

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 the anaerobic process treatment, it is treated using an aerobic process or a facultative aerobic process, and the dissolved oxygen in the aerobic process or facultative aerobic process is less than 2 mg / L; Oxidation adsorption: Adjust the pH value of the biochemically treated wastewater to acidic and then oxidize it to convert inorganic iodine ions into iodine, and use an adsorption device to adsorb the iodine; Desorption and recovery: desorb the adsorption device, adjust the pH value of the eluate obtained by desorption to acidic, then oxidize it and filter it to obtain crude iodine or elemental iodine.

2. The method for recovering iodine from wastewater containing organic iodides according to claim 1, wherein The wastewater after biochemical treatment is transported to a continuous flow reactor, where it undergoes oxidation adsorption treatment.

3. The method for recovering iodine from wastewater containing organic iodides according to claim 1, wherein The biochemically treated wastewater is transported to the reactor, where it undergoes oxidation and adsorption treatment.

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

5. The method for recovering iodine from wastewater containing organic iodides according to claim 1, wherein: The pH value is adjusted to 0-5 during the oxidative adsorption treatment.

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

7. The method for recovering iodine from wastewater containing organic iodides according to claim 1, wherein: The adsorption device is provided with an adsorbent, which includes macroporous adsorption resin, activated carbon or diatomaceous earth.

8. The method for recovering iodine from wastewater containing organic iodides according to claim 1, wherein: When the wastewater passing through the adsorption device reaches a preset threshold or the adsorption device reaches a preset threshold, adsorption is stopped.

9. The method for recovering iodine from wastewater containing organic iodides according to claim 2, wherein: The continuous flow reactor is provided with a flow disturbance device, which is used to adjust the flow rate of the 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 or 6, characterized in that: Adjust the pH to 2-3.

11. The method for recovering iodine from wastewater containing organic iodides according to claim 7, wherein: The adsorbent is a macroporous adsorption resin, and the adsorption device is a resin column.

12. A system for recovering iodine from wastewater containing organic iodides, characterized in that: The method for recovering iodine from wastewater containing organic iodides according to any one of claims 1 to 11 comprises an anaerobic device, an aerobic device or an anaerobic device, a separation device, a reaction device, an adsorption device and a recovery device.

13. The system for recovering iodine from wastewater containing organic iodides according to claim 12, wherein: The reaction device is a continuous flow reactor, and a flow disturbance device is provided in the continuous flow reactor.

14. The system for recovering iodine from wastewater containing organic iodides according to claim 12, wherein: The adsorption device is provided with a window for observing the wastewater or a detection device for detecting the state of the wastewater.

15. The system for recovering iodine from wastewater containing organic iodides according to claim 13, wherein: The flow disturbance device is used to adjust the flow rate of the wastewater in the continuous flow reactor to a Reynolds number of 60,000-140,000.

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