CN219043164U

CN219043164U - Purification and recycling system

Info

Publication number: CN219043164U
Application number: CN202221698063.5U
Authority: CN
Inventors: 赵丹
Original assignee: Dalian Yili New Material Technology Co ltd
Current assignee: Dalian Yili New Material Technology Co ltd
Priority date: 2022-07-01
Filing date: 2022-07-01
Publication date: 2023-05-19
Anticipated expiration: 2032-07-01

Abstract

The utility model discloses a purification and recycling system, when the purification and recycling system is a solid mixture purification and recycling system: mainly comprises a crystallizer I, a mixing tank I, a cooling device I, a filter I, a bipolar membrane device I, a crystallizer II, a COD reduction unit I, a halogen generation reactor, an electrolysis device, a resin tank or a volatile acid generator; or when the purification reuse system is a purification reuse system for an aqueous solution: the system mainly comprises a nanofiltration unit III or electrodialysis equipment III for purifying monovalent ions, a crystallizer V, a mixing tank V, an electrolysis device, a resin tank, a crystallizer II, a bipolar membrane equipment II or a volatile acid generator, wherein the purification and recycling system is utilized to obtain a purified single substance from multicomponent substances in materials, and the single substance is used as a product to obtain the economic value of the single substance or the single substance is reused to obtain the use value of the single substance.

Description

Purification and recycling system

Technical Field

The utility model belongs to the technical field of purification and reuse, and particularly relates to a purification and reuse system.

Background

For some materials (solid materials or aqueous solutions), the component content is complex, and the materials cannot be directly used as pure materials or can not be industrially utilized; if a set of system can be provided, the material can be purified to obtain a single substance, and the single substance can be directly used as a product to obtain the economic value; the single substance can be reused in the working condition of required use to recycle the economic value, so the method is very significant for the energy recycling of the single substance.

Disclosure of Invention

The object of the present utility model is to provide a purification and reuse system for recovering valuable substances in a solid mixture or an aqueous solution.

A purification and reuse system, wherein the system is used for purifying and reusing a solid mixture or an aqueous solution;

when the system is a system for purifying and recycling the solid mixture, the solid mixture to be treated is the solid discharged from the solid discharge port of the crystallizer I, and the solid mixture is treated by the system:

the solid discharge port of the crystallizer I is connected to the inlet of a mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of a cooling device I, the outlet of the cooling device I is connected to the inlet of a filter I, and the liquid outlet of the filter I is connected to the water inlet of a bipolar membrane device I; or the liquid outlet of the filter I is connected to the water inlet of the crystallizer II; or the liquid outlet of the filter I is connected with the water inlet of the COD reduction unit I, and the water outlet of the COD reduction unit I is connected with an oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of a halogen generation reactor (for converting bromide ions into bromine);

The bipolar membrane equipment mainly comprises an anode electrode plate, a cathode electrode plate, a bipolar membrane, a cation selective permeation membrane, an anion selective permeation membrane, a matched power supply, a pump, a tank, a control electric instrument and the like, wherein under the action of an electric field, the bipolar membrane hydrolyzes water into hydrogen ions and hydroxyl ions, and under certain combined arrangement of the bipolar membrane, the cation selective permeation membrane and the anion selective permeation membrane, cations in feed liquid are combined with hydroxyl ions generated by water electrolysis to generate corresponding alkali (an alkali chamber formed between the membranes); anions in the feed liquid are combined with hydrogen ions generated by water electrolysis to generate corresponding acids (acid chambers formed between the membranes), namely bipolar membrane equipment can convert salts in the feed liquid into two products of corresponding acids (in an acid production tank) and bases (in an alkali production tank);

the crystallizer II is used for evaporating and crystallizing the aqueous solution to obtain a solid;

the purpose of the COD reducing unit I is to reduce COD in the inflow water;

or the solid discharge port of the crystallizer I is connected to the inlet of a mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of a filter I, the liquid outlet of the filter I is connected to the water inlet of a first evaporation tank, and the water outlet of the first evaporation tank is connected to the water inlet of the first evaporation tank (the first evaporation tank is used for crystallizing, separating and filtering and removing low-solubility salt in the aqueous solution, and the concentration by evaporation is controlled by the composition and the solubility of the concentrated solution, for example, the solubility of sodium chloride is relatively low and the solubility of sodium bromide is relatively high, so the solid of the first filter is mainly sodium chloride solid, and the liquid filtrate of the first filter is mainly sodium bromide aqueous solution); or the liquid outlet of the filter I is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the water inlet of the cooling device I, and the water outlet of the cooling device I is connected to the water inlet of the filter I (the evaporation tank I, the cooling device I and the filter I are used for removing the crystallization precipitation and filtration after the temperature of the salt with lower solubility in the aqueous solution is reduced, and the concentration by evaporation is controlled by the composition and the solubility of the concentrated solution; or the liquid outlet of the filter I is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the first filter (the first cooling device is utilized, the first filter is used for cooling down the salt with lower solubility in the aqueous solution, and then crystallizing, precipitating and filtering are removed;

The liquid outlet of the first filter is connected to the water inlet of the bipolar membrane device I; or the liquid outlet of the filter I is connected to the water inlet of the crystallizer II; or the liquid outlet of the filter I is connected to the water inlet of the COD reduction unit I, and the water outlet of the COD reduction unit I is connected to the oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of the halogen generating reactor;

or the solid discharge port of the crystallizer I is connected to the inlet of a mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of a filter I, the liquid outlet of the filter I is connected to the water inlet of a COD reduction unit I, the water outlet of the COD reduction unit I is connected to the water inlet of a nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to an oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of the COD reduction unit I, the water outlet of the COD reduction unit I is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to the oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of an electrolysis device (bromine ions are electrolyzed to generate bromine); or the liquid outlet of the filter I is connected to the water inlet of the resin tank VIII; or the liquid outlet of the filter I is connected to the water inlet of the resin tank VI; or the liquid outlet of the filter I is connected to the water inlet of the volatile acid generator (converting bromide ions into hydrobromic acid);

The electrodialysis device for purifying monovalent ions refers to a novel electrodialysis device with special effect, which is derived from conventional electrodialysis devices, and can obtain salt solution mainly comprising monovalent cations and monovalent anions from an outlet I from aqueous solution containing monovalent ions, divalent or more than divalent ions, and can also have concentration effect; the main action principle is that monovalent cation selective permeable membranes, monovalent anion selective permeable membranes or nanofiltration membranes are introduced into anion selective permeable membranes and cation selective permeable membranes of conventional electrodialysis according to the requirements and the ion characteristics of the inlet water, the monovalent cation selective permeable membranes only allow monovalent cations to pass through in theory, the monovalent anion selective permeable membranes only allow monovalent anions to pass through in theory, and the nanofiltration membranes only allow monovalent cations and monovalent anions to pass through in theory; for example, if sodium carbonate and sodium bromide are present in the water, an electrodialysis device for purifying monovalent ions corresponding to a membrane stack consisting of a cation selective permeable membrane and a monovalent anion selective permeable membrane or a cation selective permeable membrane and a nanofiltration membrane is used (remark, the principle of ion permeation through each membrane is the same as that of conventional electrodialysis, except that among anions, carbonate is a divalent anion, the monovalent anion selective permeable membrane and the nanofiltration membrane are theoretically impossible to permeate, only bromide is permeable, so that anions permeating through the monovalent anion selective permeable membrane and the nanofiltration membrane are only bromide and combine with sodium ions permeating through the cation selective permeable membrane, and a sodium bromide aqueous solution is mainly obtained at the outlet I), the outlet I is a sodium bromide aqueous solution, and the other outlet (i.e., the outlet II) is a sodium carbonate aqueous solution and contains a small amount of sodium bromide; and (3) injection: in the electrodialysis device for purifying monovalent ions, the outlet I refers to an outlet containing monovalent cations and monovalent anions (such as sodium bromide aqueous solution) and consists of an aqueous solution of ions penetrating through a membrane; outlet II refers to the outlet of a salt (such as an aqueous solution containing cobalt ions, manganese ions) consisting essentially of ≡divalent cations or ≡divalent anions, which is an aqueous solution consisting of ions that do not permeate the membrane; an aqueous solution of predominantly sodium ions (e.g. sodium bromide) exiting from the fresh water outlet of the nanofiltration unit V or the outlet I of the electrodialysis device V for purifying monovalent ions, to reduce the sodium ion content entering the oxidation reaction system;

Or the solid discharge port of the crystallizer I is connected to the feed port I of an esterification reactor, the esterification reactor is also provided with a washing liquid inlet, the washing liquid outlet of the esterification reactor (used for washing liquid and used for washing) is connected to the inlet of a cooling device I, and the outlet of the cooling device I is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the oxidation reaction system or the water inlet of the halogen generation reactor; at the moment, the esterification reactor is intermittently operated, and a washing program is started after the reaction is finished, namely, the esterification reaction and the washing are alternately carried out, and after the esterification reaction is finished, washing is carried out on the product ester by using a washing liquid;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the discharge port of the esterification reactor is connected to the inlet of a washing tank I, the washing tank I is also provided with a washing liquid inlet, the washing liquid outlet of the washing tank I (used washing liquid and used washing liquid) is connected to the inlet of a cooling device I, and the outlet of the cooling device I is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of an oxidation reaction system or a halogen generation reactor; the esterification reactor can be continuously operated, and products of the esterification reactor are fed into the washing tank I for washing;

Or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the esterification reactor is also provided with a washing liquid inlet, the washing liquid outlet of the esterification reactor is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the washing liquid outlet of the esterification reactor is connected to the water inlet of electrodialysis equipment V for purifying monovalent ions, and the water outlet II of the electrodialysis equipment V for purifying monovalent ions is connected to an oxidation reaction system; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the electrolysis device; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the resin tank VIII; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the resin tank VI; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the volatile acid generator; at the moment, the esterification reactor is intermittently operated, and a washing program is started after the reaction is finished, namely, the esterification reaction and the washing are alternately carried out, and after the esterification reaction is finished, washing is carried out on the product ester by using a washing liquid;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the discharge port of the esterification reactor is connected to the inlet of a washing tank I, the washing tank I is also provided with a washing liquid inlet, the washing liquid outlet of the washing tank I is connected to the water inlet of a nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to an oxidation reaction system; or the washing liquid outlet of the washing tank I is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to the oxidation reaction system; or the washing liquid outlet of the washing tank I is connected to the water inlet of the electrolysis device; or the washing liquid outlet of the washing tank I is connected to the water inlet of the resin tank VIII; or the washing liquid outlet of the washing tank I is connected to the water inlet of the resin tank VI; or the washing liquid outlet of the washing tank I is connected to the water inlet of the volatile acid generator; the esterification reactor can be continuously operated, and products of the esterification reactor are fed into the washing tank I for washing;

Or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the esterification reactor is also provided with a washing liquid inlet, the washing liquid outlet of the esterification reactor is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the water inlet of the filter I (the evaporation tank I is used for separating out, filtering and removing salt with lower solubility in the aqueous solution by crystallization, and the concentration by evaporation is controlled by the composition and the solubility of the concentrated solution, for example, the sodium chloride is relatively low in solubility and the sodium bromide is relatively high in solubility, so the solid of the filter I is mainly sodium chloride solid, and the liquid filtrate of the filter I is mainly sodium bromide aqueous solution); or the washing liquid outlet of the esterification reactor is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the water inlet of the cooling device I, and the water outlet of the cooling device I is connected to the water inlet of the filter I (the evaporation tank I, the cooling device I and the filter I are used for removing the crystallization precipitation and filtration after the temperature of the salt with lower solubility in the aqueous solution is reduced, and the concentration by evaporation is controlled by the composition and the solubility of the concentrated solution, for example, the solubility of sodium chloride is relatively low and the solubility of sodium bromide is relatively high, so the solid of the filter I is mainly sodium chloride solid, and the liquid filtrate of the filter I is mainly sodium bromide aqueous solution); or the washing liquid outlet of the esterification reactor is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the first filter (the first cooling device is used for cooling down the salt with lower solubility in the aqueous solution, and then crystallizing, precipitating, filtering and removing the salt;

The liquid outlet of the first filter is connected with the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system or the halogen generation reactor;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the discharge port of the esterification reactor is connected to the inlet of a washing tank I, the washing tank I is also provided with a washing liquid inlet, the washing liquid outlet of the washing tank I is connected to the water inlet of a first evaporation tank, the water outlet of the first evaporation tank is connected to the water inlet of a first filter (the first evaporation tank is utilized for filtering and removing low-solubility salt crystallization precipitation in the aqueous solution, and the concentration by evaporation is controlled by the composition and the solubility of the concentrated solution, for example, the solubility of sodium chloride is relatively low and the solubility of sodium bromide is relatively high, so the solid of the first filter is mainly sodium chloride solid, and the liquid filtrate of the first filter is mainly sodium bromide aqueous solution); or the washing liquid outlet of the washing tank I is connected to the water inlet of the evaporating tank I, the water outlet of the evaporating tank I is connected to the water inlet of the cooling device I, and the water outlet of the cooling device I is connected to the water inlet of the filter I (the evaporating tank I, the cooling device I and the filter I are used for removing crystallization precipitation and filtration after cooling down the salt with lower solubility in the aqueous solution, and the evaporation concentration is controlled to be concentrated to form a solution and the solubility; or the washing liquid outlet of the washing tank I is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the first filter (the first cooling device is used for cooling down the salt with lower solubility in the aqueous solution, and then crystallizing, precipitating, filtering and removing the salt;

or the solid discharge port of the crystallizer I is connected to the inlet of a mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of a filter I, and the solid outlet of the filter I is connected to an oxidation reaction system; acetic acid is fed into a liquid inlet of the mixing tank I;

or the solid discharge port of the crystallizer I is connected to the inlet of the combustion equipment I, the outlet of the combustion equipment I is connected to the water inlet of the mixing tank V, the mixing tank V is also provided with a liquid inlet, and the outlet of the mixing tank V is connected to the oxidation reaction system; or the outlet of the combustion device I is connected to the water inlet of a mixing tank V, the mixing tank V is also provided with a liquid inlet, the outlet of the mixing tank V is connected to the water inlet of a filter V, and the water outlet of the filter V is connected to the water inlet of the bipolar membrane device I, the water inlet of a crystallizer II, the water inlet of a halogen generation reactor, the water inlet of an electrolysis device, the water inlet of a resin tank VIII, the water inlet of a resin tank VI or the water inlet of a volatile acid generator; or the water outlet of the filter V is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the water outlet of the filter V is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to an oxidation reaction system; or the outlet of the mixing tank V is connected to the water inlet of the resin tank V, and the water outlet of the resin tank V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; or the water outlet of the resin tank V is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the water outlet of the resin tank V is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to an oxidation reaction system; or the outlet of the mixing tank V is connected to the water inlet of the resin tank VIII; or the outlet of the mixing tank V is connected to the water inlet of the resin tank VI; or the outlet of the mixing tank V is connected to an oxidation reaction system; or the outlet of the mixing tank V is connected to the water inlet of the halogen generating reactor; or the outlet of the mixing tank V is connected to the water inlet of the electrolysis device; or the outlet of the mixing tank V is connected to the water inlet of the volatile acid generator;

Or the solid discharge port of the crystallizer I is connected to the inlet of the mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of the filter I, the liquid outlet of the filter I is connected to the inlet of the combustion equipment II, the outlet of the combustion equipment II is connected to the inlet of the mixing tank XII, the mixing tank XII is also provided with a liquid inlet, and the outlet of the mixing tank XII is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or the solid discharge port of the crystallizer I is connected to the water inlet of the halogen generation reactor, and the water outlet of the halogen generation reactor is discharged;

or the solid discharge port of the crystallizer I is connected to the water inlet of the electrolysis device, and the water outlet of the electrolysis device is discharged;

or the solid discharge port of the crystallizer I is connected with the water inlet of the volatile acid generator, and the water outlet of the volatile acid generator is discharged;

or when the system is an aqueous solution purification and reuse system:

the water solution discharge pipeline is connected to the water inlet of the nanofiltration unit III, and the concentrated water outlet of the nanofiltration unit III is connected to the dosing port of the crystallizer V or the mixing tank V; the most important of the nanofiltration units is a nanofiltration membrane, wherein the nanofiltration membrane is a membrane capable of intercepting divalent ions and more than divalent ions and allowing monovalent ions to permeate, and in the utility model, the nanofiltration membrane is used for intercepting divalent ions (such as carbonate, characterized by sodium carbonate) on the nanofiltration concentrate side and transmitting monovalent ions (such as bromide, characterized by sodium bromide) on the nanofiltration concentrate side;

Or the aqueous solution discharge line is connected to the water inlet of the electrodialysis device III for purifying monovalent ions; the water outlet II of the electrodialysis device III for purifying monovalent ions is connected to a drug adding port of a crystallizer V or a mixing tank V;

the electrodialysis device for purifying monovalent ions refers to a novel electrodialysis device with special effect, which is derived from conventional electrodialysis devices, and can obtain salt solution mainly comprising monovalent cations and monovalent anions from an outlet I from aqueous solution containing monovalent ions, divalent or more than divalent ions, and can also have concentration effect; the main action principle is that monovalent cation selective permeable membranes, monovalent anion selective permeable membranes or nanofiltration membranes are introduced into anion selective permeable membranes and cation selective permeable membranes of conventional electrodialysis according to the requirements and the ion characteristics of the inlet water, the monovalent cation selective permeable membranes only allow monovalent cations to pass through in theory, the monovalent anion selective permeable membranes only allow monovalent anions to pass through in theory, and the nanofiltration membranes only allow monovalent cations and monovalent anions to pass through in theory; for example, if sodium carbonate and sodium bromide are present in the water, an electrodialysis device for purifying monovalent ions corresponding to a membrane stack consisting of a cation selective permeable membrane and a monovalent anion selective permeable membrane or a cation selective permeable membrane and a nanofiltration membrane is used (remark, the principle of ion permeation through each membrane is the same as that of conventional electrodialysis, except that among anions, carbonate is a divalent anion, the monovalent anion selective permeable membrane and the nanofiltration membrane are theoretically impossible to permeate, only bromide is permeable, so that anions permeating through the monovalent anion selective permeable membrane and the nanofiltration membrane are only bromide and combine with sodium ions permeating through the cation selective permeable membrane, and a sodium bromide aqueous solution is mainly obtained at the outlet I), the outlet I is a sodium bromide aqueous solution, and the other outlet (i.e., the outlet II) is a sodium carbonate aqueous solution and contains a small amount of sodium bromide; and (3) injection: in the electrodialysis device for purifying monovalent ions, the outlet I refers to an outlet containing monovalent cations and monovalent anions (such as sodium bromide aqueous solution) and consists of an aqueous solution of ions penetrating through a membrane; outlet II refers to an outlet that contains predominantly salts (like aqueous sodium carbonate) of divalent cations or divalent anions, which consists of an aqueous solution of ions that do not penetrate the membrane;

Or the water solution discharge pipeline is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the inlet of the filter II, and the solid outlet of the filter II is connected to the dosing port of the drying equipment or the mixing tank V; the outlet of the drying device is directly used as a product (sodium carbonate solid); for example, aqueous solutions containing sodium bromide and sodium carbonate are concentrated after evaporation, wherein sodium carbonate with low solubility forms solid precipitation, and sodium bromide with higher solubility is in the aqueous solution (sodium bicarbonate is also converted into sodium carbonate after heating);

or the water solution discharge pipeline is connected to the water inlet of the nanofiltration unit III, and the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the crystallizer II, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator; the most important of the nanofiltration units is a nanofiltration membrane, wherein the nanofiltration membrane is a membrane capable of intercepting divalent ions and more than divalent ions and allowing monovalent ions to permeate, and in the utility model, the nanofiltration membrane is used for intercepting divalent ions (such as carbonate, characterized by sodium carbonate) on the nanofiltration concentrate side and transmitting monovalent ions (such as bromide, characterized by sodium bromide) on the nanofiltration concentrate side;

Or the water solution discharge pipeline is connected to the water inlet of electrodialysis equipment III for purifying monovalent ions, and the water outlet I (refers to the outlet of salt (such as sodium bromide water solution) composed of monovalent cations and monovalent anions) of the electrodialysis equipment III for purifying monovalent ions is connected to the water inlet of an electrolysis device, the water inlet of a resin tank VI, the water inlet of a resin tank VIII, the water inlet of a crystallizer II, the water inlet of a bipolar membrane equipment II or the water inlet of a volatile acid generator;

or the water solution discharge pipeline is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the inlet of the filter II, and the liquid outlet of the filter II is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the crystallizer II, the water inlet of the resin tank VI, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator; the purpose of the evaporating pot I is to evaporate the solvent in a heating way, concentrate the solute, concentrate and precipitate the salt with low solubility therein, and then separate the salt by filtration; for example, aqueous solutions containing sodium bromide and sodium carbonate are concentrated after evaporation, wherein sodium carbonate with low solubility forms solid precipitation, and sodium bromide with higher solubility is in the aqueous solution;

Or the water solution discharge pipeline is connected to the water inlet of a mixing tank III, the mixing tank III is also provided with a dosing port, the outlet of the mixing tank III is connected to the inlet of a filter III, and the liquid outlet of the filter III is connected to the water inlet of an electrolysis device, the water inlet of a resin tank VIII, the water inlet of a resin tank VI, the water inlet of bipolar membrane equipment II, the water inlet of a crystallizer II or the water inlet of a volatile acid generator; for example, sodium carbonate and sodium bromide, adding calcium salt (such as calcium bromide) to convert carbonate into insoluble calcium carbonate, and filtering to remove the insoluble calcium carbonate; for example, a mixed solution of sodium carbonate, sodium bicarbonate and sodium bromide, and alkaline substances such as calcium salt (for example, calcium bromide) and sodium hydroxide are added to convert carbonate into calcium carbonate insoluble substances (the alkaline substances such as sodium hydroxide can raise the pH value and are beneficial to converting bicarbonate into carbonate radical), and the carbonate is removed by filtration;

or the water solution discharge pipeline is connected to the water inlet of the halogen generation reactor, and the water outlet of the halogen generation reactor is connected to the drug adding port or discharge of the mixing tank V; converting bromide ions in the aqueous solution into bromine simple substances through the halogen generation reactor and removing the bromine simple substances from the aqueous solution, wherein the rest is mainly sodium carbonate aqueous solution;

Or the water solution discharge pipeline is connected to the water inlet of the electrolysis device, and the water outlet of the electrolysis device is connected to the water inlet of the crystallizer III, the dosing port of the mixing tank V or the discharge; converting bromine ions in the aqueous solution into bromine simple substances through the electrolysis device and removing the bromine simple substances from the aqueous solution, wherein the rest is mainly sodium carbonate aqueous solution;

or the water solution discharge pipeline is connected to the water inlet of the resin tank VIII, and the water outlet of the resin tank VIII is connected to the water inlet of the crystallizer III, the dosing port of the mixing tank V or the discharge; converting bromide ions in the aqueous solution into bromine simple substances through the resin tank VIII and removing the bromine simple substances from the aqueous solution, wherein the rest is mainly sodium carbonate aqueous solution;

or the water solution discharge pipeline is connected with the water inlet of the volatile acid generator, and the water outlet of the volatile acid generator is connected with the water inlet of the crystallizer III, the dosing port of the mixing tank V or the discharge; the bromide ions in the aqueous solution are converted to hydrobromic acid and removed from the aqueous solution by the volatile acid generator, with the remainder being predominantly aqueous sodium carbonate.

Based on the above technical scheme, preferably, water, sodium carbonate aqueous solution, sodium hydroxide aqueous solution, organic solvent and the like are added into the liquid inlet of the mixing tank I.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the outlet of the mixing tank I is connected to the water inlet of the filter I, and the filtration may be performed twice or more, i.e. the mixing tank I comprises a mixing tank I-1, a mixing tank I-2, the filter I comprises a filter I-1, a filter I-2, i.e. the outlet of the mixing tank I-1 (i.e. the inlet of the mixing tank I) is connected to the inlet of the filter I-1, the liquid outlet of the filter I-1 is connected to the inlet of the mixing tank I-2, the outlet of the mixing tank I-2 is connected to the inlet of the filter I-2, the liquid outlet of the filter I-1 is the liquid outlet of the filter I (this is the case of two filtration), and so on.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the esterification reactor is a conventional esterification reactor and comprises all components of a conventional esterification reaction device.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for the solid mixture, the esterification reactor is further provided with a product ester outlet; or the washing tank I is provided with a product ester outlet.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the esterification reactor is further provided with a feed inlet II for adding alcohols into the esterification reactor.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the esterification reactor also needs to add catalyst.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the catalyst of the esterification reactor is preferably sulfuric acid or hydrobromic acid.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the esterification reactor is also provided with a water removal outlet.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the water removal outlet of the esterification reactor is preferably a gas phase water vapor outlet.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the washing liquid outlet of the esterification reactor is: layering in the esterification reactor, namely layering the washing liquid and the product ester, wherein a discharge port of the washing liquid is a discharge port of the layering of the used washing liquid, and the product ester is at the other outlet.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the washing liquid outlet (used washing liquid ) of the washing tank I is: layering in the washing tank I, namely layering the washing liquid and the product ester, wherein a discharge port of the washing liquid is a discharge port of the layering of the used washing liquid, and the product ester is at the other outlet.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the washing liquid used by the esterification reactor or the washing tank I is preferably water or dilute acid, sodium carbonate or the like.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for the solid mixture,

a gasification device (also called sublimation device, such as gasification tank) is also provided, the solid discharge outlet of the crystallizer I is connected to the inlet of the gasification device, and the solid discharge outlet of the gasification device is connected to the inlet of the mixing tank I, the inlet of the combustion device I, the feed inlet I of the esterification reactor, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device or the water inlet of the volatile acid generator; the gasification equipment is operated, the operation temperature of the gasification equipment exceeds the sublimation temperature of part of the solid components, and part of the organic components are sublimated into gas phase;

Or the filter I is also provided with a washing device I for washing the solid in the filter I, and the washing liquid is discharged from a liquid outlet of the filter I:

when water or aqueous solution of alkaline substances is used as the material of the liquid inlet of the mixing tank I, the washing liquid is discharged from the liquid outlet of the filter I; filtrate is also discharged from the liquid outlet of the filter I;

when the solvent is used as the material of the liquid inlet of the mixing tank I, the filtrate of the filter I is discharged from the solvent discharge port of the filter I; the washing liquid is discharged from a liquid outlet of the filter I (used washing liquid, used washed);

or further provided with a washing device II, the outlet of which is connected to the inlet of a solid-liquid separator XI (in the form of, for example, a filter or a layering tank, etc.), the solid outlet of which is connected to the inlet of a washing tank II, the outlet of which is also connected to the washing tank II, the outlet of which (used washing liquid ) is connected to the filter I, i.e. the solid of which is washed with washing liquid (for example, when solvent is used as the material of the liquid inlet of the mixing tank I);

Or further provided with a washing device III, the outlet of which is connected to the inlet of a solid-liquid separator XI, the liquid outlet of which is connected to the inlet of a crystallizer IV (heated evaporation to remove solvent), the solid outlet of which is connected to a washing tank III, which is also connected to the washing tank III, the outlet of which (meaning spent washing liquid, spent washing) is connected to a filter I; or the outlet of the washing tank III (used washing liquid ) is connected to a solid-liquid separator XII (a form such as a filter or a layering tank, etc.), and the liquid outlet of the solid-liquid separator XII is connected to the water inlet of the COD-reducing unit I, the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the evaporation tank I, the water inlet of the cooling device I or the water inlet of the volatile acid generator, namely, the solid of the crystallizer IV is washed by the washing liquid (such as when the solvent is used as the material of the liquid inlet of the mixing tank I).

the top of gasification equipment still is equipped with the condenser for retrieve the material of sublimating.

the liquid inlet of the mixing tank I is filled with water, alkaline substances, acidic substances or solvents.

the alkaline substance fed into the liquid inlet of the mixing tank I is preferably an aqueous solution of the alkaline substance (such as sodium carbonate aqueous solution); the acidic substance fed into the liquid inlet of the mixing tank I is preferably an aqueous solution of the acidic substance.

the solvent fed into the liquid inlet of the mixing tank I is a solvent capable of dissolving part or all of the solid components discharged from the solid discharge outlet of the crystallizer I.

The solvent fed into the liquid inlet of the mixing tank I is a solvent which can dissolve part or all of the solid components discharged from the solid discharge outlet of the crystallizer I, and alcohols, ethers, aromatics, acetic acid and the like are preferable.

the washing device I, the washing device II or the washing device III is characterized in that the provided washing liquid is water or dilute acid.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the fresh water outlet of the nanofiltration unit V or the water outlet I of the electrodialysis device V for purifying monovalent ions is connected to the water inlet of the bipolar membrane device one, the water inlet of the crystallizer one, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

the fresh water outlet of the nanofiltration unit V or the water outlet I of the electrodialysis device V for purifying monovalent ions is mainly salt composed of monovalent anions and monovalent cations, and the nanofiltration unit V or the electrodialysis device V for purifying monovalent ions is designed to separate the salt composed of monovalent anions and monovalent cations from the aqueous solution by using the nanofiltration unit V or the electrodialysis device V for purifying monovalent ions, so as to reduce the concentration of the salt composed of monovalent anions and monovalent cations in the aqueous solution entering the oxidation reaction system, because the salt (such as sodium ions) corresponding to monovalent cations is impurity for the oxidation reaction system;

The salt composed of monovalent anions and monovalent cations obtained by separation can be recovered by, for example, producing acid by bipolar membrane equipment I, crystallizing salt by crystallizer I, and other methods.

Based on the above technical scheme, preferably, when the purification and reuse system is the solid mixture purification and reuse system, the solid mixture purification and reuse system processes the solid mixture generated by the crystallizer I, and the solution mainly containing HAC, BA, cobalt ion, manganese ion, sodium ion, bromide ion and other components enters the crystallizer I to process (evaporating HAC to remove HAC) to obtain the solid mixture (i.e., the solid mixture generated by the crystallizer I), and the utility model processes the solid mixture, i.e., the solution mainly containing HAC, BA, cobalt ion, manganese ion, sodium ion, bromide ion and other components enters the feed inlet of the crystallizer I.

Based on the above technical solution, preferably, the solution mainly containing HAC, BA, cobalt ion, manganese ion, sodium ion, bromide ion, etc. is preferably the solution discharged from the acetic acid recovery system of the PTA plant (mainly containing HAC).

Based on the above technical solution, preferably, when the purification and reuse system is the pair of aqueous solution purification and reuse system, the aqueous solution (referred to as the treated aqueous solution) treated by the aqueous solution treatment system is preferably an aqueous solution containing bromide ions and carbonate and/or bicarbonate, that is, the aqueous solution discharge pipeline discharges an aqueous solution containing bromide ions and carbonate and/or bicarbonate (cations of the aqueous solution, such as sodium ions).

Based on the above technical scheme, preferably, the aqueous solution containing bromide ions contains carbonate and/or bicarbonate, and is preferably sewage discharged from a PTA factory.

Based on the above technical scheme, preferably, the sewage source discharged by the PTA factory is sewage obtained by concentrating the water discharged by a tail gas spray tower of the PTA factory, the water discharged after biochemical treatment or the water discharged after biochemical treatment.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the solid mixture at the solid outlet of the crystallizer I contains a certain humidity.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the COD reduction unit I includes at least one of a biochemical treatment device I, an advanced oxidation device I, an extraction device I, an acidification device I, a resin tank I, and an electrodialysis device I, wherein the electrodialysis device I has a water inlet, a water outlet I (which refers to discharge water with an increased inorganic concentration ratio, wherein the ratio of BA concentration to inorganic concentration is smaller than that of water inlet, i.e., BA is smaller), and a water outlet II (which refers to discharge water with a high organic concentration ratio, wherein the ratio of BA concentration to inorganic concentration is larger than that of water inlet), and the water outlet I of the electrodialysis device I is connected to the oxidation reaction system;

When the COD reduction unit I is combined by two or more of a biochemical treatment device I, an advanced oxidation device I, an extraction device I, an acidification device I, a resin tank I and an electrodialysis device I, a water outlet of the former unit is connected to a water inlet of the latter unit, for example, a water outlet of the extraction device I is connected to a water inlet of the acidification device I.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the purification and reuse system is further provided with a COD reduction unit II, a COD reduction unit III, a COD reduction unit IV or a COD reduction unit V:

the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII is connected to the water inlet of the COD reduction unit II, and the water outlet of the COD reduction unit II is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the evaporation tank I and the water inlet of the cooling device I;

or the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII is connected to the water inlet of the COD reduction unit III, and the water outlet of the COD reduction unit III is connected to the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I and the water inlet of the cooling device I;

Or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the inlet of the cooling equipment I, the outlet of the cooling equipment I is connected to the water inlet of the COD reduction unit IV, and the water outlet of the COD reduction unit IV is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the oxidation reaction system or the water inlet of the halogen generation reactor;

or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the water inlet of the COD reduction unit IV, and the water outlet of the COD reduction unit IV is connected to the water inlet of the nanofiltration unit V, the water inlet of the electrodialysis device V for purifying monovalent ions, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I or the water inlet of the cooling device I;

or the fresh water outlet of the nanofiltration unit V is connected to the water inlet of the COD reduction unit V, and the water outlet of the COD reduction unit V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer I, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

Or the water outlet I of the electrodialysis device V for purifying monovalent ions is connected to the water inlet of the COD reduction unit V, and the water outlet of the COD reduction unit V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer I, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

the purpose of the COD reduction unit II, the COD reduction unit III, the COD reduction unit IV or the COD reduction unit V is to reduce COD in the influent water.

the COD reduction unit II comprises at least one of a biochemical treatment device II, a high-grade oxidation device II, an extraction device II, an acidification device II, a resin tank II and an electrodialysis device IV; wherein, for the electrodialysis device IV, there are a water inlet, a water outlet I (which means discharge water with an increased inorganic substance concentration ratio, wherein the ratio of BA concentration to inorganic substance concentration is smaller than that of the water inlet, i.e. BA is less), and a water outlet II (which means discharge water with an increased organic substance concentration ratio, wherein the ratio of BA concentration to inorganic substance concentration is larger than that of the water inlet);

When the COD reduction unit II is combined by two or more of a biochemical treatment device II, a high-grade oxidation device II, an extraction device II, an acidification device II, a resin tank II and an electrodialysis device IV, the water outlet of the former water outlet is connected with the water inlet of the latter water outlet, for example, the water outlet of the extraction device II is connected with the water inlet of the acidification device II;

or the COD reduction unit III comprises at least one of a medium biochemical treatment device III, a high-grade oxidation device III, an extraction device III, an acidification device III, a resin tank III and an electrodialysis device III, wherein the electrodialysis device III is provided with a water inlet and a water outlet I (which means discharge water with increased inorganic substance concentration ratio, wherein the ratio of BA concentration to inorganic substance concentration is smaller than that of the water inlet, namely, the BA is less), and a water outlet II (which means discharge water with increased organic substance concentration ratio, wherein the ratio of BA concentration to inorganic substance concentration is larger than that of the water inlet);

when the COD reduction unit III is combined by two or more of a biochemical treatment device III, an advanced oxidation device III, an extraction device III, an acidification device III, a resin tank III and an electrodialysis device III, the water outlet of the former unit is connected with the water inlet of the latter unit, for example, the water outlet of the extraction device III is connected with the water inlet of the acidification device III;

Or the COD reduction unit IV comprises at least one of a medium biochemical treatment device IV, a high-grade oxidation device IV, an extraction device IV, an acidification device IV, a resin tank X and an electrodialysis device V, wherein the electrodialysis device V is provided with a water inlet, a water outlet I (the discharged water with the increased inorganic matter concentration ratio) and a water outlet II (the discharged water with the increased organic matter concentration ratio);

when the COD reduction unit IV is combined by two or more of a biochemical treatment device IV, an advanced oxidation device IV, an extraction device IV, an acidification device IV, a resin tank X and an electrodialysis device V, the water outlet of the former unit is connected with the water inlet of the latter unit, for example, the water outlet of the extraction device IV is connected with the water inlet of the acidification device IV;

or the COD reducing unit V comprises at least one of a biochemical treatment device V, a high-grade oxidation device V, an extraction device V, an acidification device V, a resin tank XI and an electrodialysis device II, wherein the electrodialysis device II is provided with a water inlet, a water outlet I (the discharged water with the increased inorganic matter concentration ratio) and a water outlet II (the discharged water with the increased organic matter concentration ratio);

when the COD reduction unit V is combined by two or more of the biochemical treatment device V, the advanced oxidation device V, the extraction device V, the acidification device V, the resin tank XI and the electrodialysis device II, a water outlet of the former is connected to a water inlet of the latter, for example, a water outlet of the extraction device V is connected to a water inlet of the acidification device V.

Based on the technical scheme, preferably, the electrodialysis device mainly comprises an anode electrode plate, a cathode electrode plate, a cation selective permeation membrane, an anion selective permeation membrane, a matched power supply, a pump, a tank, a control electric instrument and the like, and has the main functions of concentrating and converting low-concentration water into concentrated solution; namely, cations can pass through the cation selective permeation membrane to enter the concentrating chamber, anions can pass through the anion selective permeation membrane to enter the concentrating chamber, salt consisting of anions and cations which pass through corresponding membranes is obtained in the concentrating chamber, the ion migration speed and migration quantity are fixed when the voltage is fixed, the concentration of salt solution in the concentrating chamber can be controlled to reach the required concentration by controlling the discharge quantity of the concentrating chamber (the discharge quantity can be large when the flow of pure water fed into the concentrating chamber is large, the concentration of discharged water in the concentrating chamber is not increased compared with the concentration of water fed into the electrodialysis device, namely, the concentration of the concentrating chamber can be manually regulated and set, and can be regulated to be lower than the salt concentration in the water fed into the electrodialysis device;

the utility model utilizes the other effect of electrodialysis equipment, the principle of the effect is that cations can pass through the cation selective permeation membrane to enter the concentration chamber, anions can pass through the anion selective permeation membrane to enter the concentration chamber, but under the effect of an electric field, the migration speed of different ions under the effect of the electric field is different, the organic ions are obviously slower than the inorganic ions, so when the organic ions and the inorganic ions are simultaneously contained in the inlet water, the concentration liquid with the increased concentration ratio of the inorganic substances can be extracted by controlling the ion migration speed (the concentration ratio of the inorganic substances in the treated aqueous solution (inlet water) is compared with the concentration ratio of the inorganic substances in the electrodialysis equipment), the effect of extracting the inorganic substances can be achieved (the inorganic substances can contain a certain concentration of the organic substances), the concentration liquid can be the concentration of the inorganic ions of the concentration liquid is higher than the inlet water, and the inorganic ions of the concentration liquid can also be the concentration of the concentration liquid is not higher than the inlet water, namely the flow rate of the concentration chamber for feeding pure water is very large, the discharge amount is large, the concentration is not concentrated in the concentration chamber, namely the concentration is not concentrated, the concentration is higher than the concentration of the organic substances in the electrodialysis equipment (the concentration is compared with the inlet water of the concentration of the electrodialysis equipment), the inorganic substances is also called as the water outlet water, the concentration is higher than the concentration of the inlet water of the organic substances in the concentration is compared with the inlet water, namely the concentration is the inlet water.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the electrodialysis device I, the electrodialysis device II, the electrodialysis device III, the electrodialysis device IV and the electrodialysis device V may be conventional electrodialysis devices, or may be any electrodialysis devices for purifying monovalent ions (that is, the electrodialysis devices for purifying monovalent ions produce the same effect as conventional electrodialysis devices when treating a solution containing only salts composed of monovalent cations and monovalent anions), and only when the aqueous solution contains more than or equal to divalent ions, the electrodialysis devices for purifying monovalent ions produce special functions and effects of separating ions according to valence.

a resin tank V is arranged between the liquid outlet of the filter I and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

A resin tank V is arranged between a liquid outlet of the solid-liquid separator XII and a water inlet of the bipolar membrane equipment I or a water inlet of the crystallizer II:

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane device I or the water inlet of the crystallizer II along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

or a resin tank V is arranged between the liquid outlet of the filter I and the water inlet of the evaporation tank I or the water inlet of the cooling equipment I;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the evaporating tank I or the water inlet of the cooling device I along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or a resin tank V is arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the first evaporation tank or the water inlet of the first cooling device:

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the evaporation tank I or the water inlet of the cooling equipment I along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

or a resin tank V is arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit II along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or a resin tank V is arranged between the water outlet of the COD reducing unit II and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II;

or a mixing tank V and a filter V are sequentially arranged between the water outlet of the COD reducing unit II and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

or a resin tank V is arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator along the material flow direction, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or a resin tank V is arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit III;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit III along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

or a resin tank V is arranged between the water outlet of the COD reducing unit III and the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or a mixing tank V and a filter V are sequentially arranged between the water outlet of the COD reducing unit III and the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the cooling equipment I, and a resin tank V is arranged between the outlet of the cooling equipment I and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the oxidation reaction system or the water inlet of the halogen generation reactor;

or a resin tank V is arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the electrolysis device, a water inlet of the resin tank VI, a water inlet of the resin tank VIII, a water inlet of the volatile acid generator, a water inlet of the evaporation tank I or a water inlet of the cooling equipment I;

or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the cooling equipment I, a mixing tank V and a filter V are sequentially arranged between the outlet of the cooling equipment I and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II and the water inlet of the oxidation reaction system or the halogen generation reactor along the material flow direction, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a dosing port:

Or a mixing tank V and a filter V are sequentially arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the electrolysis device, a water inlet of the resin tank VI, a water inlet of the resin tank VIII, a water inlet of the volatile acid generator, a water inlet of the evaporation tank I or a water inlet of the cooling device I along the material flow direction, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

or a resin tank V is arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the COD reducing unit IV;

or a mixing tank V and a filter V are sequentially arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the COD reducing unit IV along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or a resin tank V is arranged between the water outlet of the COD reducing unit IV and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I or the water inlet of the cooling equipment I;

or a mixing tank V and a filter V are sequentially arranged between the water outlet of the COD reducing unit IV and the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I or the water inlet of the cooling device I along the material flow direction, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or a resin tank V is arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the electrolysis device, a water inlet of the resin tank VI, a water inlet of the resin tank VIII or a water inlet of the volatile acid generator;

or a mixing tank V and a filter V are sequentially arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the electrolysis device, a water inlet of the resin tank VI, a water inlet of the resin tank VIII or a water inlet of the volatile acid generator along the material flow direction, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

or a resin tank V is arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the inlet of the combustion equipment II:

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I or the liquid outlet of the solid-liquid separator XII and the inlet of the combustion equipment II along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or a resin tank V is arranged between the liquid outlet of the mixing tank XII and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the mixing tank XII and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator along the direction of material flow, the mixing tank V is provided with a water inlet and a water outlet, the filter V is provided with a water inlet and a liquid outlet, and the water outlet of the mixing tank V is connected to the water inlet of the filter V; the water inlet of the mixing tank V is connected to the upper-stage equipment of the process route, and the liquid outlet of the filter V is connected to the lower-stage equipment of the process route; the mixing tank V is also provided with a medicine adding port;

Or the water outlet of the halogen generation reactor is connected to a resin tank V, and the water outlet of the resin tank V is discharged;

or the water outlet of the halogen generation reactor is connected to a mixing tank V, the water outlet of the mixing tank V is connected to a filter V, and the water outlet of the filter V is discharged; the mixing tank V is also provided with a medicine adding port;

or the water outlet of the electrolysis device is connected to a resin tank V, and the water outlet of the resin tank V is discharged;

or the water outlet of the electrolysis device is connected to a mixing tank V, the water outlet of the mixing tank V is connected to a filter V, and the water outlet of the filter V is discharged; the mixing tank V is also provided with a medicine adding port;

or the water outlet of the volatile acid generator is connected to a resin tank V, and the water outlet of the resin tank V is discharged;

or the water outlet of the volatile acid generator is connected to a mixing tank V, the water outlet of the mixing tank V is connected to a filter V, and the water outlet of the filter V is discharged; the mixing tank V is also provided with a medicine adding port.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the solid outlet of the filter I or the solid outlet of the solid-liquid separator XII is connected to the inlet of the combustion apparatus II or the inlet of the combustion apparatus III.

Based on the above technical solution, preferably, the solid outlet of the filter I or the solid outlet of the solid-liquid separator XII is connected to the other outlet of the combustion device II or the other outlet of the mixing tank XII is connected to the dosing port of the mixing tank V.

Based on the above technical solution, preferably, the dosing port of the mixing tank V adds an alkaline substance to the mixing tank V.

Based on the above technical solution, preferably, the dosing port of the mixing tank V adds an alkaline substance, preferably a solid or an aqueous solution of an alkaline substance, to the mixing tank V.

Based on the above technical solution, preferably, the dosing port of the mixing tank V adds an alkaline substance, preferably carbonate, bicarbonate, hydroxide, to the mixing tank V.

Based on the above technical scheme, preferably, the dosing port of the mixing tank V adds an alkaline substance to the mixing tank V, wherein the alkaline substance is preferably carbonate, bicarbonate or hydroxide, and the corresponding cation is preferably sodium ion or potassium ion.

Based on the above technical solution, preferably, the solid outlet of the crystallizer V is collected, mainly as sodium carbonate solid.

Based on the above technical scheme, the mixing tank V is preferably a dissolution mixing tank (adding alkaline substances to the mixing tank to dissolve oxidation residues) of the PTA factory or a mixing tank (adding alkaline substances to the mixing tank to form insoluble substances of cobalt ions and manganese ions) of a heavy metal (for example, cobalt and manganese ions) recovery process.

Based on the above technical solution, preferably, the oxidation reaction system is preferably an oxidation reactor of the PTA plant, i.e. a reactor in which PX reacts with air (oxygen in) to form terephthalic acid.

Based on the above technical scheme, preferably, when the purification and reuse system is the pair of aqueous solution purification and reuse system,

a cooling device II is arranged between the water outlet of the evaporation tank I and the filter II; the purpose of the conveying evaporation tank I is concentration, and salt with low solubility is separated out after the concentration of the salt, and then the salt is filtered and separated; for example, sodium carbonate is far less soluble than sodium bromide, and sodium carbonate will precipitate, the solids filtered by filter II are predominantly sodium carbonate, and the filter II filtrate are predominantly aqueous sodium bromide;

or the liquid outlet of the filter II (preferably connected to the water inlet of the nanofiltration unit IV after heating and/or dilution) is connected to the water inlet of the nanofiltration unit IV, and the fresh water outlet of the nanofiltration unit IV is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane device II or the water inlet of the volatile acid generator; the filter II filtrate is separated by a nanofiltration unit IV after divalent or more than divalent ions (a small amount of carbonate ions) are added;

Or a cooling device II is arranged between the water outlet of the evaporation tank I and the filter II; the liquid outlet of the filter II is connected to the water inlet of the nanofiltration unit IV (preferably after warming and/or dilution) and the fresh water outlet of the nanofiltration unit IV is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane device II or the water inlet of the volatile acid generator; the purpose of the evaporation tank I is concentration, the temperature of the salt is reduced after concentration, the salt with low solubility at low temperature can be separated out, and then the salt is filtered and separated; for example, at low temperatures (e.g., below 15 ℃), sodium carbonate is far less soluble than sodium bromide, and sodium carbonate will precipitate, the solids filtered by filter II being predominantly sodium carbonate, and the filtrate by filter II being predominantly aqueous sodium bromide; the filter II filtrate is separated by a nanofiltration unit IV after divalent or more than divalent ions (a small amount of carbonate ions) are added;

or the liquid outlet of the filter II is connected to the water inlet of an electrodialysis device IV for purifying monovalent ions (preferably to the water inlet of the electrodialysis device IV for purifying monovalent ions after warming and/or dilution), the water outlet I of the electrodialysis device IV for purifying monovalent ions (meaning the outlet for obtaining salts composed of monovalent cations, monovalent anions) is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane device II or the water inlet of the volatile acid generator; for the filter II filtrate, divalent or more than divalent ions (a small amount of carbonate ions) are added, and then the water outlet I of electrodialysis equipment IV for purifying monovalent ions is used for obtaining an aqueous solution mainly containing sodium bromide;

Or a cooling device II is arranged between the water outlet of the evaporation tank I and the filter II; the liquid outlet of the filter II is connected to the water inlet of an electrodialysis device IV for purifying monovalent ions (preferably to the water inlet of the electrodialysis device IV for purifying monovalent ions after warming and/or dilution), the water outlet I of the electrodialysis device IV for purifying monovalent ions (meaning the outlet for obtaining salts composed of monovalent cations, monovalent anions) is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane device II or the water inlet of the volatile acid generator; the purpose of the evaporation tank I is concentration, the temperature of the salt is reduced after concentration, the salt with low solubility at low temperature can be separated out, and then the salt is filtered and separated; for example, at low temperatures (e.g., below 15 ℃), sodium carbonate is far less soluble than sodium bromide, and sodium carbonate will precipitate, the solids filtered by filter II being predominantly sodium carbonate, and the filtrate by filter II being predominantly aqueous sodium bromide; and (3) divalent or more than divalent ions (a small amount of carbonate ions) are added into the filtrate of the filter II, and then the water outlet I of electrodialysis equipment IV for purifying monovalent ions is used for obtaining the water solution mainly containing sodium bromide.

Based on the above technical scheme, preferably, when the purification and reuse system is the solid mixture purification and reuse system, when the COD reduction unit I, the COD reduction unit II, the COD reduction unit III, the COD reduction unit IV or the COD reduction unit V is the biochemical treatment device I, the biochemical treatment device II, the biochemical treatment device III, the biochemical treatment device IV or the biochemical treatment device V, respectively, the biochemical treatment will reduce COD while the alkalinity in water will increase, and the form of carbonate and/or bicarbonate will exist, so the concentration of the effluent carbonate and/or bicarbonate of the biochemical treatment device will be higher (increase), wherein the original ions in the water body are still contained, for example, if sodium ions, bromide ions, etc. are present.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for the solid mixture, a liquid outlet of the filter I is connected with a water inlet of the bipolar membrane device I, a liquid outlet of the filter I is connected with a water inlet of the crystallizer II, a liquid outlet of the solid-liquid separator XII is connected with a water inlet of the bipolar membrane device I, a liquid outlet of the solid-liquid separator XII is connected with a water inlet of the crystallizer II the water outlet of the COD reduction unit II is connected with the water inlet of the bipolar membrane device I, the water outlet of the COD reduction unit II is connected with the water inlet of the crystallizer II, the water outlet of the resin tank V is connected with the water inlet of the bipolar membrane device I, the water outlet of the resin tank V is connected with the water inlet of the crystallizer II, the liquid outlet of the filter V is connected with the water inlet of the bipolar membrane device I the water outlet of the COD reducing unit II is connected with the water inlet of the bipolar membrane equipment I, the water outlet of the COD reducing unit II is connected with the water inlet of the crystallizer II the water outlet of the resin tank V is connected with the water inlet of the bipolar membrane device I, the water outlet of the resin tank V is connected with the water inlet of the crystallizer II, the liquid outlet of the filter V is connected with the water inlet of the bipolar membrane device I, the liquid outlet of the resin tank V and the water inlet of the electrolysis device, the liquid outlet of the resin tank V and the water inlet of the resin tank VIII, the liquid outlet of the resin tank V and the water inlet of the resin tank VI, the liquid outlet of the resin tank V and the water inlet of the volatile acid generator, the liquid outlet of the filter I and the water inlet of the halogen generation reactor, the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generation reactor, the liquid outlet of the filter I and the water inlet of the electrolysis device, the liquid outlet of the solid-liquid separator XII and the water inlet of the electrolysis device, the liquid outlet of the filter I and the water inlet of the resin tank VIII, the liquid outlet of the solid-liquid separator XII and the water inlet of the resin tank VIII between the liquid outlet of the filter I and the water inlet of the resin tank VI, between the liquid outlet of the solid-liquid separator XII and the water inlet of the resin tank VI, between the liquid outlet of the filter I and the water inlet of the volatile acid generator, between the liquid outlet of the solid-liquid separator XII and the water inlet of the volatile acid generator, between the water outlet of the COD-reducing unit III and the water inlet of the halogen generation reactor, between the water outlet of the resin tank V and the water inlet of the halogen generation reactor, between the liquid outlet of the filter V and the water inlet of the halogen generation reactor, between the outlet of the cooling device I and the water inlet of the bipolar membrane device I, between the outlet of the cooling device I and the water inlet of the crystallizer II, between the outlet of the cooling device I and the oxidation reaction system, between the outlet of the cooling device I and the water inlet of the halogen generation reactor, between the outlet of the cooling device I and the water inlet of the electrolysis device, between the outlet of the cooling device I and the water inlet of the resin tank VIII, between the outlet of the cooling device I and the water inlet of the resin tank VI, between the outlet of the cooling device I and the water inlet of the volatile acid generator, between the washing liquid outlet of the esterification reactor and the water inlet of the electrolysis device, between the washing liquid outlet of the esterification reactor and the water inlet of the resin tank VIII, between the washing liquid outlet of the esterification reactor and the water inlet of the resin tank VI, between the washing liquid outlet of the esterification reactor and the water inlet of the volatile acid generator the method comprises the steps of arranging a water inlet of an electrolyzer, a water inlet of a resin tank VIII, a water outlet of a washing tank I, a water inlet of a volatile acid generator, a water outlet of a COD reduction unit IV, a water inlet of a bipolar membrane device I, a water outlet of the COD reduction unit IV, an oxidation reaction system, a water outlet of the COD reduction unit IV, a water inlet of a crystallizer II, a water outlet of the COD reduction unit IV, a water inlet of a halogen generation reactor, a liquid outlet of a solid-liquid separator XII, a water inlet of the halogen generation reactor, a water outlet of the solid-liquid separator IV, a water inlet of the bipolar membrane device I, a water outlet of the COD reduction unit IV, a water outlet of the solid-liquid separator IV and a water inlet of the halogen generation reactor, the water outlet of the COD reducing unit IV is connected with the water inlet of the electrolysis device, the water outlet of the COD reducing unit IV is connected with the water inlet of the resin tank VIII, the water outlet of the COD reducing unit IV is connected with the water inlet of the resin tank VI, the water outlet of the COD reducing unit IV is connected with the water inlet of the volatile acid generator, the water outlet of the mixing tank XII is connected with the water inlet of the bipolar membrane equipment I, the water outlet of the mixing tank XII is connected with the water inlet of the crystallizer II, the water outlet of the mixing tank XII is connected with the oxidation reaction system, the water outlet of the mixing tank XII is connected with the water inlet of the halogen generation reactor, the water outlet of the mixing tank XII is connected with the water inlet of the electrolysis device, the water outlet of the mixing tank XII is connected with the water inlet of the resin tank VI the water outlet of the mixing tank XII is connected with the water inlet of the resin tank VIII, the water outlet of the mixing tank XII is connected with the water inlet of the volatile acid generator, the outlet of the mixing tank V is connected with the oxidation reaction system, the outlet of the mixing tank V is connected with the water inlet of the halogen generation reactor, the outlet of the mixing tank V is connected with the water inlet of the electrolysis device, the outlet of the mixing tank V is connected with the water inlet of the resin tank VI, the outlet of the mixing tank V is connected with the water inlet of the volatile acid generator, the outlet of the mixing tank V is connected with the water inlet of the resin tank VIII, the water outlet of the COD reduction unit I is connected with the water inlet of the evaporation tank I, the water outlet of the COD reduction unit I is connected with the water inlet of the cooling device I, the water outlet of the COD reduction unit II is connected with the water inlet of the evaporation tank I, the water outlet of the COD reducing unit II is connected with the water inlet of the first cooling device, the water outlet of the COD reducing unit III is connected with the water inlet of the first evaporation tank, the water outlet of the COD reducing unit III is connected with the water inlet of the first cooling device, the water outlet of the COD reducing unit IV is connected with the water inlet of the first evaporation tank, the water outlet of the COD reducing unit IV is connected with the water inlet of the first cooling device, the liquid outlet of the filter I is connected with the water inlet of the first evaporation tank, the liquid outlet of the filter I is connected with the water inlet of the first cooling device, the liquid outlet of the filter XII is connected with the water inlet of the first evaporation tank, the liquid outlet of the filter V is connected with the water inlet of the first cooling device, the liquid outlet of the resin tank V is connected with the water inlet of the first evaporation tank or the liquid outlet of the resin tank V is connected with the water inlet of the first cooling device).

A nanofiltration unit I is arranged, and a fresh water outlet of the nanofiltration unit I is connected to a water inlet of the bipolar membrane equipment I, a water inlet of the crystallizer II, a water inlet of the halogen generation reactor, the oxidation reaction system, a water inlet of the electrolysis device, a water inlet of the resin tank VIII, a water inlet of the resin tank VI or a water inlet of the volatile acid generator; the most important equipment in the nanofiltration unit is a nanofiltration membrane, wherein the nanofiltration membrane can intercept divalent and more than divalent ions (cations and/or anions) under the pressure condition, and intercept the divalent and more than divalent ions (cations and/or anions) on the concentrate side, and the fresh side is mainly a salt solution composed of monovalent cations and monovalent anions which penetrate through the nanofiltration membrane; for example, if sodium carbonate and sodium bromide exist in the water, the nanofiltration fresh water is mainly sodium bromide water solution, the nanofiltration concentrated water is mainly sodium carbonate water solution, and a little sodium bromide is also contained;

or an electrodialysis device I for purifying monovalent ions is arranged, wherein a water outlet I (refers to an aqueous solution outlet for purifying monovalent ions) of the electrodialysis device I is connected to a water inlet of the bipolar membrane device I, a water inlet of the crystallizer II, a water inlet of the halogen generating reactor, the oxidation reaction system, a water inlet of the electrolysis device, a water inlet of the resin tank VIII, a water inlet of the resin tank VI or a water inlet of the volatile acid generator; for example, if sodium carbonate and sodium bromide exist in water, the water outlet I is mainly sodium bromide aqueous solution, the water outlet II is mainly sodium carbonate aqueous solution, and a little sodium bromide is also contained;

Or an evaporation tank II and a filter IX are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the filter IX, and the liquid outlet of the filter IX is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generating reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; the purpose of the evaporating pot II is to evaporate the solvent in a heating way, concentrate the solute, separate out the salt with low solubility after concentrating, and then separate by filtering; the purpose of the evaporating pot II is to evaporate the solvent in a heating way, concentrate the solute, concentrate and precipitate the salt with low solubility therein, and then separate the salt by filtration; for example, aqueous solutions containing sodium bromide and sodium carbonate are concentrated after evaporation, wherein sodium carbonate with low solubility forms solid precipitation, and sodium bromide with higher solubility is in the aqueous solution (sodium bicarbonate is also converted into sodium carbonate after heating);

or an evaporation tank II, a cooling device III and a filter IX are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the cooling device III, the water outlet of the cooling device III is connected to the water inlet of the filter IX, and the liquid outlet of the filter IX is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; the purpose of the evaporating pot II is to concentrate, the temperature of the salt is reduced after concentration, the salt with low solubility at low temperature can be separated out, and then the salt is filtered and separated; for example, at low temperatures (e.g., below 15 ℃), sodium carbonate is far less soluble than sodium bromide, and sodium carbonate precipitates, the filtered solids are mainly sodium carbonate, and the filtrate is mainly aqueous sodium bromide (sodium bicarbonate is also converted to sodium carbonate when heated);

Or an evaporation tank II, a filter IX and a nanofiltration unit II are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the nanofiltration unit II, and the fresh water outlet of the nanofiltration unit II is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; the purpose of the evaporating pot II is to evaporate the solvent in a heating mode, concentrate the solute, concentrate and precipitate the salt with low solubility therein, and then separate the salt by filtration; for divalent or more than divalent ions (carbonate ions) in the filtrate, separating by the nanofiltration unit II;

or an evaporation tank II, a cooling device III, a filter IX and a nanofiltration unit II are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the cooling device III, the water outlet of the cooling device III is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the nanofiltration unit II, and the fresh water outlet of the nanofiltration unit II is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; the purpose of the evaporating pot II is to concentrate, the temperature of the salt is reduced after concentration, the salt with low solubility at low temperature can be separated out, and then the salt is filtered and separated; for example, at low temperatures (e.g., below 15 ℃), sodium carbonate is far less soluble than sodium bromide, and sodium carbonate precipitates, the filtered solids are predominantly sodium carbonate, and the filtrate is predominantly aqueous sodium bromide (still containing a small amount of sodium carbonate); intercepting the sodium carbonate of the filtrate on the concentrated water side by using the nanofiltration unit II, and increasing the proportion of sodium bromide in nanofiltration fresh water again;

Or an evaporation tank II, a filter IX and an electrodialysis device II for purifying monovalent ions are sequentially arranged along the material flow direction, wherein the water outlet of the evaporation tank II is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the electrodialysis device II for purifying monovalent ions, and the water outlet I (the water outlet of the electrodialysis device II for purifying monovalent ions) is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; the purpose of the evaporating pot II is to evaporate the solvent by heating, concentrate the solute, concentrate the salt with low solubility therein and then separate out (such as sodium carbonate), and then separate by filtration; for divalent or more than divalent ions (e.g. carbonate) in the filtrate, separating with the electrodialysis device II for purifying monovalent ions;

or an evaporation tank II, a cooling device III, a filter IX and an electrodialysis device II for purifying monovalent ions are sequentially arranged along the material flow direction, wherein the water outlet of the evaporation tank II is connected with the water inlet of the cooling device III, the water outlet of the cooling device III is connected with the water inlet of the filter IX, the liquid outlet of the filter IX is connected with the water inlet of the electrodialysis device II for purifying monovalent ions, and the water outlet I (the water solution outlet for purifying monovalent ions) of the electrodialysis device II for purifying monovalent ions is connected with the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; the purpose of the evaporating pot II is to concentrate, the temperature of the salt is reduced after concentration, the salt with low solubility at low temperature can be separated out, and then the salt is filtered and separated; for example, at low temperatures (e.g., below 15 ℃), sodium carbonate is far less soluble than sodium bromide, and sodium carbonate precipitates, the filtered solids are predominantly sodium carbonate (sodium bicarbonate is also converted to sodium carbonate upon heating), and the filtrate is predominantly aqueous sodium bromide (still containing a small amount of sodium carbonate); separating by using the electrodialysis equipment II for purifying monovalent ions;

Or a mixing tank X and a filter X are sequentially arranged along the material flow direction, the mixing tank X is also provided with a chemical adding port, the outlet of the mixing tank X is connected to the water inlet of the filter X, and the liquid outlet of the filter X is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; for example, sodium carbonate and sodium bromide, adding calcium salt (such as calcium bromide) to convert carbonate into insoluble calcium carbonate, and filtering to remove the insoluble calcium carbonate; for example, a mixed solution of sodium carbonate, sodium bicarbonate and sodium bromide, and alkaline substances such as calcium salt (for example, calcium bromide) and sodium hydroxide are added to convert carbonate into calcium carbonate insoluble substances (alkaline substances such as sodium hydroxide can raise pH and are beneficial to converting bicarbonate into carbonate), and the carbonate is removed by filtration.

The water outlet II of the electrodialysis device I, the water outlet II of the electrodialysis device II, the water outlet II of the electrodialysis device III, the water outlet II of the electrodialysis device IV or the water outlet II of the electrodialysis device V:

directly discharging;

or connected to the water inlet of the resin tank IV, and the water outlet of the resin tank IV is discharged;

or to the water inlet of a mixing tank IV, the water outlet of which is connected to the water inlet of a filter IV, the liquid outlet of which discharges;

based on the above technical solution, preferably, the mixing tank IV further has a dosing port, and an alkaline substance, such as hydroxide, carbonate, etc., is added.

the concentrated water outlet of the nanofiltration device I is connected with the water inlet of the crystallizer VIII, the dosing port of the mixing tank V or the discharge;

or the water outlet II of the electrodialysis device I for extracting monovalent ions is connected to the water inlet of the crystallizer VIII, the drug adding port of the mixing tank V or the discharge;

or the concentrated water outlet of the nanofiltration device II is connected to the water inlet of the crystallizer VIII, the dosing port of the mixing tank V, the water inlet of the evaporation tank II, the water inlet of the cooling equipment III, the water inlet or the discharge of the filter IX;

Or the water outlet II of the electrodialysis device II for extracting monovalent ions is connected to the water inlet of the crystallizer VIII, the dosing port of the mixing tank V, the water inlet of the evaporation tank II, the water inlet of the cooling device III, the water inlet of the filter IX or the discharge.

Based on the above technical solution, preferably, when the purification and reuse system is the aqueous solution purification and reuse system, the solid outlet of the filter II is connected to the inlet of the crystallizer VI, the drying apparatus, or the dosing port of the mixing tank V.

Based on the above technical solution, preferably, when the purification and reuse system is the aqueous solution purification and reuse system, when the concentrated water outlet of the nanofiltration unit III is connected to the crystallizer V, the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or when the concentrated water outlet of the nanofiltration unit III is connected to the dosing port of the mixing tank V, the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the bipolar membrane equipment II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, or the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or when the water outlet II of the electrodialysis device III for extracting monovalent ions is connected to the crystallizer V, the water outlet I of the electrodialysis device III for extracting monovalent ions is connected to the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or when the water outlet II of the electrodialysis device III for extracting monovalent ions is connected to the dosing port of the mixing tank V, the water outlet I of the electrodialysis device III for extracting monovalent ions is connected to the water inlet of the crystallizer II, the water inlet of the halogen generating reactor, the water inlet of the bipolar membrane device II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or when the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the bipolar membrane equipment II, the water inlet of the crystallizer II or the water inlet of the volatile acid generator, the concentrated water outlet of the nanofiltration unit III is connected to the water inlet of the crystallizer V, the dosing port of the mixing tank V or the discharge;

Or when the water outlet I of the electrodialysis device III for extracting monovalent ions is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II or the water inlet of the volatile acid generator, the water outlet II of the electrodialysis device III for extracting monovalent ions is connected to the water inlet of the crystallizer V, the drug adding port or the discharge port of the mixing tank V;

or the concentrated water outlet of the nanofiltration device IV is connected to the water inlet of the crystallizer X, the dosing port of the mixing tank V, the water inlet of the evaporation tank I, the water inlet of the cooling equipment II and the water inlet or discharge of the filter II;

or the water outlet II of the electrodialysis device IV for extracting monovalent ions is connected to the water inlet of the crystallizer X, the dosing port of the mixing tank V, the water inlet of the evaporation tank I, the water inlet of the cooling device II, the water inlet of the filter II or the discharge.

Based on the above technical scheme, preferably, it is also provided with an alkali adding device I or a heating device I:

the outlet of the alkali adding device I is connected to a pipeline between a liquid outlet of the filter I, a liquid outlet of the solid-liquid separator XII, a water outlet of the COD reducing unit II, a water outlet of the resin tank V, a water outlet of the filter V, a water outlet of the COD reducing unit III, a washing liquid outlet of the esterification reactor, a washing liquid outlet of the washing tank I, an outlet of the cooling equipment I, a water outlet of the COD reducing unit IV, a water outlet of the mixing tank V or a water outlet of the mixing tank XII and a water inlet of the nanofiltration unit I, or a connection position of the pipeline is provided with a buffer tank;

Or the outlet of the alkali adding device I is connected to a pipeline between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reducing unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reducing unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling equipment I, the water outlet of the COD reducing unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the evaporation tank II, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reducing unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reducing unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling equipment I, the water outlet of the COD reducing unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the electrodialysis equipment I for purifying monovalent ions, or a buffer tank is used at the connection position of the pipeline;

The purpose of the alkali addition is that if a large amount of bicarbonate exists in the water, the monovalent bicarbonate can be converted into divalent carbonate by adding alkaline matters such as sodium hydroxide, and the carbonate is divalent and is easier to separate from monovalent bromide ions; meanwhile, if the sodium carbonate is converted into sodium carbonate, carbonate particles formed by the sodium carbonate, cobalt ions and manganese ions are larger, so that the sodium carbonate is easier to filter out and does not block a filter screen;

or a heating device I and a cooling device IV are sequentially arranged between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reduction unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reduction unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reduction unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the nanofiltration unit I along the material flow direction, and the outlet of the heating device I is connected to the inlet of the cooling device IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the inlet of the cooling equipment IV;

Or a heating device I and a cooling device IV are sequentially arranged between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reduction unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reduction unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reduction unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the electrodialysis device I for purifying monovalent ions along the material flow direction, and the outlet of the heating device I is connected to the inlet of the cooling device IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the inlet of the cooling equipment IV;

or a heating device I and a cooling device V are sequentially arranged between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reduction unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reduction unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reduction unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the mixing tank X along the material flow direction, and the outlet of the heating device I is connected to the inlet of the cooling device V; or a heating device I, a decarburization tower I and cooling equipment V are sequentially arranged along the material flow direction, wherein the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the inlet of the cooling equipment V;

The purpose of the heating is to convert bicarbonate into carbonate and carbon dioxide (released into the air) by heating if a large amount of bicarbonate exists in the water, and the carbonate is divalent and is more easily separated from monovalent bromide ions; meanwhile, if the sodium carbonate is converted into sodium carbonate, carbonate particles formed by the sodium carbonate, cobalt ions and manganese ions are larger, so that the sodium carbonate is easier to filter out and does not block a filter screen;

or the outlet of the alkali adding device I is connected to a pipeline between the water solution discharge pipeline and the water inlet of the nanofiltration unit III, the water inlet of the electrodialysis equipment III for purifying monovalent ions, the water inlet of the evaporation tank I or the water inlet of the mixing tank III, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the water solution discharge pipeline and the water inlet of the halogen generation reactor, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the water solution discharge pipeline and the water inlet of the electrolysis device, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the water solution discharge pipeline and the water inlet of the resin tank VIII, or a buffer tank is used at the connection position of the pipeline;

Or the outlet of the alkali adding device I is connected to a pipeline between the water solution discharge pipeline and the water inlet of the volatile acid generator, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the water outlet of the halogen generating reactor, the water outlet of the electrolysis device, the water outlet of the resin tank VIII or the water outlet of the volatile acid generator and the water inlet of the crystallizer III, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the water outlet of the halogen generating reactor, the water outlet of the electrolysis device, the water outlet of the resin tank VIII or the water outlet of the volatile acid generator and the medicine adding port of the mixing tank V, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the concentrated water outlet of the nanofiltration unit III and the water inlet of the crystallizer V or the medicine adding port of the mixing tank V, or a buffer tank is used at the connection position of the pipeline;

or the outlet of the alkali adding device I is connected to a pipeline between the water outlet II of the electrodialysis equipment III for purifying monovalent ions and the water inlet of the crystallizer V or the medicine adding port of the mixing tank V, or a buffer tank is used at the connection position of the pipeline;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the nanofiltration unit III, the water inlet of the electrodialysis device III for purifying monovalent ions, the water inlet of the evaporation tank I or the water inlet of the mixing tank III along the material flow direction, and the outlet of the heating device I is connected to the inlet of the cooling device IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the inlet of the cooling equipment IV;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the halogen generation reactor along the material flow direction, and the outlet of the heating device I is connected to the inlet of the cooling device IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the inlet of the cooling equipment IV;

Or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the electrolysis device along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling device IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment IV;

or a heating device I and cooling equipment IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the resin tank VIII along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling equipment IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment IV;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the volatile acid generator along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling device IV; or a heating device I, a decarburization tower I and cooling equipment IV are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment IV;

Or a heating device I is arranged between the water outlet of the halogen generation reactor, the water outlet of the electrolysis device, the water outlet of the resin tank VIII or the water outlet of the volatile acid generator and the water inlet of the crystallizer III along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the decarburization tower I; or a heating device I and cooling equipment V are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling equipment V; or a heating device I, a decarburization tower I and cooling equipment V are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment V;

or a heating device I is arranged between the water outlet of the halogen generation reactor, the water outlet of the electrolysis device, the water outlet of the resin tank VIII or the water outlet of the volatile acid generator and the medicine adding port of the mixing tank V along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the decarburization tower I; or a heating device I and cooling equipment V are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling equipment V; or a heating device I, a decarburization tower I and cooling equipment V are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment V;

Or a heating device I is arranged between the concentrated water outlet of the nanofiltration unit III and the water inlet of the crystallizer V or the medicine adding port of the mixing tank V along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the decarburization tower I; or a heating device I and cooling equipment VI are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling equipment VI; or a heating device I, a decarburization tower I and cooling equipment VI are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment VI;

or a heating device I is arranged between the water outlet II of the electrodialysis equipment III for purifying monovalent ions and the water inlet of the crystallizer V or the medicine adding port of the mixing tank V along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the decarburization tower I; or a heating device I and cooling equipment VI are sequentially arranged along the material flow direction, and the outlet of the heating device I is connected to the water inlet of the cooling equipment VI; or a heating device I, a decarburization tower I and cooling equipment VI are sequentially arranged along the material flow direction, the outlet of the heating device I is connected to the water inlet of the decarburization tower I, and the water outlet of the decarburization tower I is connected to the water inlet of the cooling equipment VI;

The purpose of the heating is to convert bicarbonate into carbonate and carbon dioxide (released into the air) by heating if a large amount of bicarbonate exists in the water, and the carbonate is divalent and is more easily separated from monovalent bromide ions; meanwhile, if the sodium carbonate is converted into sodium carbonate, carbonate particles formed by the sodium carbonate, cobalt ions and manganese ions are larger, so that the sodium carbonate is easier to filter out and does not block a filter screen.

Based on the above technical scheme, preferably, it is still equipped with alkali adding device II or heating device II:

the outlet of the alkali adding device II is connected to a pipeline between the liquid outlet of the filter IX and the water inlet of the nanofiltration unit II, or a buffer tank is used at the connection position of the pipeline;

the outlet of the alkali adding device II is connected to a pipeline between the liquid outlet of the filter IX and the water inlet of the electrodialysis device II for purifying monovalent ions, or a buffer tank is used at the connection position of the pipeline;

the outlet of the alkali adding device II is connected to a pipeline between the liquid outlet of the filter II and the water inlet of the nanofiltration unit IV, or a buffer tank is used at the connection position of the pipeline;

the outlet of the alkali adding device II is connected to a pipeline between the liquid outlet of the filter II and the water inlet of the electrodialysis device IV for purifying monovalent ions, or a buffer tank is used at the connection position of the pipeline;

Or a heating device II and cooling equipment VII are sequentially arranged between the liquid outlet of the filter IX and the water inlet of the nanofiltration unit II along the material flow direction, and the outlet of the heating device II is connected to the inlet of the cooling equipment VII; or a heating device II, a decarburization tower II and cooling equipment VII are sequentially arranged along the material flow direction, the outlet of the heating device II is connected to the water inlet of the decarburization tower II, and the water outlet of the decarburization tower II is connected to the inlet of the cooling equipment VII;

or a heating device II and cooling equipment VIII are sequentially arranged between the liquid outlet of the filter II and the water inlet of the nanofiltration unit IV along the material flow direction, and the outlet of the heating device II is connected to the inlet of the cooling equipment VIII; or a heating device II, a decarburization tower II and cooling equipment VIII are sequentially arranged along the material flow direction, the outlet of the heating device II is connected to the water inlet of the decarburization tower II, and the water outlet of the decarburization tower II is connected to the inlet of the cooling equipment VIII;

or a heating device II and a cooling device VII are sequentially arranged between the liquid outlet of the filter IX and the water inlet of the electrodialysis device II for purifying monovalent ions along the material flow direction, and the outlet of the heating device II is connected to the inlet of the cooling device VII; or a heating device II, a decarburization tower II and cooling equipment VII are sequentially arranged along the material flow direction, the outlet of the heating device II is connected to the water inlet of the decarburization tower II, and the water outlet of the decarburization tower II is connected to the inlet of the cooling equipment VII;

Or a heating device II and a cooling device VIII are sequentially arranged between the liquid outlet of the filter II and the water inlet of the electrodialysis device IV for purifying monovalent ions along the direction of material flow, and the outlet of the heating device II is connected to the inlet of the cooling device VIII; or a heating device II, a decarburization tower II and cooling equipment VIII are sequentially arranged along the material flow direction, the outlet of the heating device II is connected to the water inlet of the decarburization tower II, and the water outlet of the decarburization tower II is connected to the inlet of the cooling equipment VIII;

the purpose of the alkali addition is to convert the residual monovalent bicarbonate (or bicarbonate generated by hydrolysis of the carbonate) into divalent carbonate by adding an alkaline substance such as sodium hydroxide, and the carbonate is divalent and is easy to separate from monovalent bromide ions; meanwhile, if the sodium carbonate is converted into sodium carbonate, carbonate particles formed by the sodium carbonate, cobalt ions and manganese ions are larger, so that the sodium carbonate is easier to filter out and does not block a filter screen;

the purpose of the heating is to convert residual monovalent bicarbonate (or bicarbonate generated by hydrolysis of carbonate) into carbonate and carbon dioxide (released into the air) by a heating method, wherein the carbonate is divalent and is easy to separate from monovalent bromide ions; meanwhile, if the sodium carbonate is converted into sodium carbonate, carbonate particles formed by the sodium carbonate, cobalt ions and manganese ions are larger, so that the sodium carbonate is easier to filter out and does not block a filter screen;

Or the outlet of the alkali adding device II is connected to the water inlet of the crystallizer II, or a buffer tank is used at the connecting position, and free hydrobromic acid is neutralized by adding alkaline matters such as sodium hydroxide and the like.

Based on the above technical solution, preferably, the resin tank VIII is further provided with an inlet and an outlet for a regeneration liquid, and the regeneration liquid outlet is connected to the water inlet of the bipolar membrane device III, the water inlet of the crystallizer VII, the water inlet of the halogen generating reactor, the water inlet of the electrolysis apparatus, the water inlet of the resin tank VI, or the water inlet of the volatile acid generator.

Based on the above technical scheme, preferably, the inlet of the regeneration liquid of the resin tank VIII is fed with an alkaline solution as the regeneration liquid.

Based on the above technical scheme, preferably, the inlet of the regeneration liquid of the resin tank VIII is fed with an alkaline solution as the regeneration liquid, preferably an aqueous solution of sodium hydroxide or potassium hydroxide.

Based on the technical scheme, a neutralization tank is preferably arranged;

a neutralization tank is further arranged before the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the bipolar membrane device III or the water inlet of the bipolar membrane device I, a pipeline originally connected to the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the bipolar membrane device III or the water inlet of the bipolar membrane device I is firstly connected to the water inlet of the neutralization tank, and the water outlet of the neutralization tank is connected to the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the bipolar membrane device III or the water inlet of the bipolar membrane device I; the water solution which originally enters the bipolar membrane equipment I, the bipolar membrane equipment II, the bipolar membrane equipment III or the bipolar membrane equipment I passes through a neutralization tank and then enters the bipolar membrane equipment I, the bipolar membrane equipment II, the bipolar membrane equipment III or the bipolar membrane equipment I for treatment;

Or a neutralization tank is arranged in front of the water inlet of the electrolysis device;

or a neutralization tank is arranged in front of the water inlet of the resin tank VI;

or a neutralization tank is arranged in front of the water inlet of the resin tank VIII;

or a neutralization tank is arranged in front of the water inlet of the halogen generation reactor;

or a neutralization tank is arranged in front of the water inlet of the oxidation reaction system;

or a neutralization tank is arranged in front of the water inlet of the volatile acid generator;

or a neutralization tank is arranged in front of the medicine adding port of the mixing tank V;

or the water inlet of the crystallizer II, the water inlet of the crystallizer III, the water inlet of the crystallizer IV, the water inlet of the crystallizer V, the water inlet of the crystallizer VI, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII, the water inlet of the crystallizer X or the water inlet of the crystallizer I is also provided with a neutralization tank before, and the pipeline originally connected to the water inlet of the crystallizer II, the water inlet of the crystallizer III, the water inlet of the crystallizer IV, the water inlet of the crystallizer V, the water inlet of the crystallizer VI, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII or the water inlet of the crystallizer I is firstly connected to the water inlet of the neutralization tank, and the water outlet of the neutralization tank is connected to the water inlet of the crystallizer II, the water inlet of the crystallizer III, the water inlet of the crystallizer IV, the water inlet of the crystallizer V, the water inlet of the crystallizer VI, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII or the water inlet of the crystallizer I; namely, the aqueous solution which originally enters the crystallizer II, the crystallizer III, the crystallizer IV, the crystallizer V, the crystallizer VI, the crystallizer VII, the crystallizer VIII or the crystallizer I passes through a neutralization tank, enters the crystallizer II, the crystallizer III, the crystallizer IV, the crystallizer V, the crystallizer VI, the crystallizer VII, the crystallizer VIII or the crystallizer I for treatment after passing through the neutralization tank;

The outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank;

the purpose of the acid addition is:

if the water solution entering the water inlet of the bipolar membrane device still contains a small amount of bicarbonate and carbonate, carbonic acid can be generated in the acid chamber of the bipolar membrane device and overflows carbon dioxide gas, so that the operation stability of the bipolar membrane device is affected, and the carbonate and the bicarbonate react to generate carbon dioxide by adding acid in advance and escape into the air;

if the water solution entering the water inlet of the crystallizer still contains a small amount of bicarbonate and carbonate, sodium carbonate and sodium bicarbonate are mixed in the sodium bromide solid product of the crystallizer, so that the purity of sodium bromide is influenced, the carbonate and the bicarbonate are removed in advance by an acid adding method, meanwhile, since the acid adding is excessive for thoroughly removing the bicarbonate, in order to neutralize the free hydrobromic acid, an alkali adding unit III is needed to add alkali again to a neutralization tank to neutralize the free hydrobromic acid, and the purity of sodium bromide product of the crystallizer is improved.

Based on the above technical scheme, preferably, a hardness removal device is provided:

The hardness removing device is arranged at any position between the liquid outlet of the filter I and the water inlet of the bipolar membrane equipment I, the water inlet of the bipolar membrane equipment III, the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII, the water inlet of the crystallizer I, the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device III, the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII, the water inlet of the crystallizer I, the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or the hardness removing device is arranged at any position between the outlet of the cooling device I and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device III, the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the washing liquid outlet of the esterification reactor and the oxidation reaction system, the water inlet of the bipolar membrane equipment I, the water inlet of the bipolar membrane equipment III, the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer VII, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the washing liquid outlet of the washing tank I and the oxidation reaction system, the water inlet of the bipolar membrane equipment I, the water inlet of the bipolar membrane equipment III, the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer VII, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or the hardness removing device is arranged at any position between the water inlet of the combustion unit I to the bipolar membrane equipment I, the water inlet of the bipolar membrane equipment III, the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII, the water inlet of the crystallizer I, the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the water inlet of the combustion unit II to the bipolar membrane equipment I, the water inlet of the bipolar membrane equipment III, the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the crystallizer VII, the water inlet of the crystallizer VIII, the water inlet of the crystallizer I, the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or the hardness removal device is arranged at any position from the water solution discharge pipeline to the water inlet of the crystallizer II, the water inlet of the crystallizer III, the water inlet of the crystallizer V, the water inlet of the crystallizer VI, the water inlet of the crystallizer VII, the water inlet of the bipolar membrane device III, the water inlet of the halogen generating reactor, the water inlet of the bipolar membrane device II, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the water solution discharge pipeline and the mixing tank V;

the purpose of the hardness removal device is to design the bipolar membrane device, if the inlet water finally entering the bipolar membrane device contains hardness, scaling substances (calcium hydroxide, magnesium hydroxide and the like) can be generated in an alkali chamber to influence the operation stability; for the crystallizer, if the aqueous solution entering the crystallizer contains hardness, the purity of sodium bromide, sodium carbonate and the like products of the crystallizer is reduced (containing calcium bromide, magnesium bromide and the like); hardness also affects the oxidation reaction system; meanwhile, the hardness can also influence the operation stability of the nanofiltration unit, electrodialysis equipment (scaling) for purifying monovalent ions, and the like.

Based on the above technical scheme, preferably, the hardness removing device is preferably a resin tank VII, and the resin tank VII is filled with resin with adsorption effect on hardness.

Based on the above technical scheme, the resin with adsorption function on the hardness is preferably regenerated by dilute acid solution or salt solution after being saturated.

Based on the above technical scheme, preferably, the resin with adsorption function on hardness is saturated by adsorption and then regenerated by dilute acid solution, and the acid is hydrobromic acid or acetic acid, and the salt is sodium bromide or sodium acetate.

Based on the above technical solution, preferably, the fresh water outlet of the nanofiltration unit I, the fresh water outlet of the nanofiltration unit II, the fresh water outlet of the nanofiltration unit III, the fresh water outlet of the nanofiltration unit IV, the fresh water outlet of the nanofiltration unit V, the water outlet I of the electrodialysis device for purifying monovalent ions I, the water outlet I of the electrodialysis device for purifying monovalent ions II, the water outlet I of the electrodialysis device for purifying monovalent ions III, the water outlet I of the electrodialysis device for purifying monovalent ions V, the liquid outlet of the filter II, the liquid outlet of the filter III, the liquid outlet of the filter X, or the liquid outlet of the filter IX, and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the halogen generating reactor, or the water inlet of the volatile acid generator are arranged between:

The device is also provided with an evaporation tank I and a filter I in sequence, wherein a water inlet of the evaporation tank I is connected to the upper-stage equipment, an outlet of the evaporation tank I is connected to a water inlet of the filter I, and a liquid outlet of the filter I is connected to the lower-stage equipment; the first evaporating pot and the first filter are used for separating out, filtering and removing salt crystals with low solubility in the aqueous solution, and naturally evaporating and concentrating are used for controlling the composition and the solubility of the concentrated solution; for example, sodium chloride is relatively low in solubility and sodium bromide is relatively high in solubility, so that the solids of filter one are mainly sodium chloride solids and the liquid filtrate of filter one is mainly an aqueous solution of sodium bromide;

or the evaporator is sequentially provided with an evaporator first, a cooling device first and a filter first, wherein the water inlet of the evaporator first is connected to the upper-stage device, the outlet of the evaporator first is connected to the water inlet of the cooling device first, the water outlet of the cooling device first is connected to the water inlet of the filter first, and the liquid outlet of the filter first is connected to the lower-stage device; the first evaporating pot, the first cooling device and the first filter are used for cooling down salt with lower solubility in the aqueous solution, crystallizing, separating out, filtering and removing, and naturally evaporating and concentrating to control the composition and the solubility of the concentrated solution; for example, sodium chloride is relatively low in solubility and sodium bromide is relatively high in solubility, so that the solids of filter one are mainly sodium chloride solids and the liquid filtrate of filter one is mainly an aqueous solution of sodium bromide;

Or the cooling equipment I and the filter I are sequentially arranged, a water inlet of the cooling equipment I is connected to the upper-stage equipment, a water outlet of the cooling equipment I is connected to a water inlet of the filter I, and a liquid outlet of the filter I is connected to the lower-stage equipment; the first cooling equipment and the first filter are used for cooling substances with lower solubility in the aqueous solution, reducing the solubility, crystallizing, separating out, filtering and removing; for example, sodium chloride is relatively low in solubility and sodium bromide is relatively high in solubility, so that the solids of filter one are mainly sodium chloride solids and the liquid filtrate of filter one is mainly an aqueous solution of sodium bromide;

or the water inlet of the bipolar membrane device III, the water inlet of the bipolar membrane device IV and the water inlet of the bipolar membrane device I are also provided with an evaporation tank I and a filter I in sequence; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged, and the principle is the same as that described above.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, resin tank IV or resin tank V is filled with resin having adsorption effect on heavy metal ions.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, resin tank IV or resin tank V is filled with resin having adsorption effect on heavy metal ions (e.g. cobalt ions, manganese ions), and the resin tank is regenerated with acid solution or salt solution after adsorption saturation.

Based on the above technical solution, preferably, the inlet of the regeneration liquid of the resin tank VII is preferably connected to an acid pipeline or an acid generating tank of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, or the bipolar membrane device one.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, resin with adsorption effect on heavy metal ions is filled in the resin tank IV or the resin tank V, and the resin tank is regenerated by acid solution or salt solution after adsorption saturation, and the acid is preferably hydrobromic acid or the salt is preferably sodium bromide aqueous solution.

Based on the above technical solution, preferably, the inlet of the regeneration liquid of the resin tank IV or the resin tank V is preferably connected to an acid pipeline or an acid generating tank of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III or the bipolar membrane device one.

Based on the above technical scheme, preferably, when the treatment system is the solid mixture purifying and recycling system, a feed inlet is further formed on the mixing tank IV or the mixing tank V.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, a feed inlet is further provided on the mixing tank IV or the mixing tank V for adding alkaline substances.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, a feed port is further provided on the mixing tank IV or the mixing tank V for adding alkaline substances (solid or aqueous solution), such as sodium carbonate, sodium bicarbonate, sodium hydroxide, potassium carbonate, potassium bicarbonate, potassium hydroxide, and the like, preferably sodium carbonate.

Based on the above technical solutions, it is preferred that the mixing tank IV or mixing tank V is connected to the crystallizer III, the crystallizer V, the crystallizer VI, the crystallizer VIII or the crystallizer one.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the extraction device I, the extraction device II, the extraction device III, the extraction device IV, or the extraction device V:

Comprises an extraction tank, wherein the extraction tank is provided with an extractant inlet, a water outlet and an extractant discharge outlet (the water outlet of the extraction tank is the water outlet of the extraction device); or comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extractant inlet, an extractant inlet and an extractant outlet, the separation tank of the extraction equipment is provided with an inlet, an outlet and an extractant discharge outlet, the outlet of the extraction tank is connected to the inlet of the separation tank (the outlet of the separation tank is the outlet of the extraction device), that is, after the extraction in the extraction tank is finished, the extraction tank is fed into the separation tank to be layered up and down, and then separation is carried out;

the extraction requires the addition of an extractant.

Based on the above recovery system, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the extractant is used to extract BA in aqueous solution, so as to reduce the BA content in aqueous solution, i.e. reduce the COD content (i.e. extract BA in water into extract, extract and water are not miscible).

Based on the above treatment system, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the extractant type contains an extractant that can dissolve BA, which is insoluble in water.

Based on the above treatment system, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the extractant contains an aromatic compound or an ester or the like.

Based on the above treatment system, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the aromatic compound contains benzene or the like.

Based on the above treatment system, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the used extractant discharged from the extractant outlet is separated from BA by an extractant recovery unit (for example, separation by a principle of difference in heating boiling points, recondensing recovery of the extractant), and the extractant is reused.

Based on the above recovery system, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the extractant recovery unit is an evaporation and condensation system.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the purification and reuse system is configured to be a solid mixture purification and reuse system for the acidification device I, the acidification device II, the acidification device III, the acidification device IV, or the acidification device V:

The acidification tank is provided with a water inlet, a water outlet and an acidification pipeline, the water outlet of the acidification tank of the acidification device is connected to the water inlet of a sedimentation tank or a filter VII, and the filter VII is provided with a water outlet (the water outlet of the sedimentation tank or the water outlet of the filter VII is the water outlet of the acidification device);

organic substances such as BA in water crystallize and precipitate under acid washing conditions (hydrogen ions are supplied) and are insoluble in water.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the acidification tank is provided with an acid adding pipeline, and acid is added into the acidification tank.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the acid added in the acid adding line is hydrobromic acid or acetic acid.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the acid adding line is connected to an acid generating tank or an acid pipe or an acid pump of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III or the bipolar membrane device one.

Based on the above technical scheme, preferably, when the system is the purification and reuse system for a solid mixture, for the advanced oxidation apparatus I, the advanced oxidation apparatus II, the advanced oxidation apparatus III, the advanced oxidation apparatus IV, or the advanced oxidation apparatus V:

comprises a high-grade oxidation reactor, wherein the high-grade oxidation reactor is provided with a precipitation overflow port or a water outlet, and a filter screen is arranged on the precipitation overflow port or the water outlet (the precipitation overflow port or the water outlet is the water outlet of the high-grade oxidation equipment);

or comprises a high-grade oxidation reactor, a filter VIII or a sedimentation tank, wherein the high-grade oxidation reactor is provided with a water inlet and a water outlet, the water outlet of the high-grade oxidation reactor is connected to the water inlet of the filter VIII or the water inlet of the sedimentation tank, and the filter VIII or the sedimentation tank is provided with a water outlet (the water outlet of the filter VIII or the water outlet of the sedimentation tank is the water outlet of the high-grade oxidation equipment);

the advanced oxidation reactor is an oxidation reaction (under the condition of adding the medicament required by the advanced oxidation reaction) which is used for decomposing organic matters and reduces the content of the organic matters and the COD value, and the advanced oxidation reaction comprises Fenton reaction, fenton-like reaction and other advanced oxidation reaction and other principles.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the advanced oxidation reactor is provided with a dosing port for adding a medicament required by the advanced oxidation reactor.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the agent required by the advanced oxidation reactor has an oxidizing agent.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the oxidant needed by the advanced oxidation reactor is preferably ferrous bromide and hydrogen peroxide.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the oxidant required by the advanced oxidation reactor is preferably ferrous bromide, hydrogen peroxide, and acid (such as hydrobromic acid or acetic acid) is also required.

Based on the above technical scheme, preferably, when the purification and reuse system is the solid mixture purification and reuse system, the biochemical treatment device I, the biochemical treatment device II, the biochemical treatment device III, the biochemical treatment device IV or the biochemical treatment device V may be mixed with other water sources to perform biochemical treatment together, that is, the water sources on the route of the present utility model are mixed with other water sources to perform biochemical treatment together.

Based on the above technical solution, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the biochemical treatment device I, the biochemical treatment device II, the biochemical treatment device III, the biochemical treatment device IV, or the biochemical treatment device V:

comprises at least one of an anaerobic biochemical treatment device, an anoxic biochemical treatment device and an oxygen consumption biochemical treatment device, and reduces COD by using a biochemical sludge method, namely decomposing organic matters in water by using the activity of the biochemical sludge, and reducing COD.

Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the resin tank I, the resin tank II, the resin tank III, the resin tank X or the resin tank XI:

the resin tank is filled with resin having adsorption effect on COD.

the resin tank is filled with a resin having an adsorption effect on COD, preferably a resin having an adsorption effect on BA.

the resin tank is regenerated by alkaline solution or acetic acid solution after adsorption saturation.

the resin tank is regenerated with an alkaline solution, preferably sodium hydroxide solution, after adsorption saturation.

Based on the above technical solution, preferably, for the resin tank I, the resin tank II, the resin tank III, the resin tank X or the resin tank XI, the inlet of the regeneration liquid is preferably connected to an alkali pipeline or an alkali producing tank of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III or the bipolar membrane device one.

Based on the above technical scheme, preferably, the halogen generating reactor can be a reaction tower, even a section of a pipeline for reaction is enough, and bromine ions are oxidized into bromine simple substances in the halogen generating reactor, so that the halogen generating reactor needs to be added with an oxidant to perform oxidation reaction.

Based on the above technical solution, preferably, the halogen generating reactor is provided with a gas inlet, and an exhaust port of the halogen generating reactor is connected to an air inlet of the absorption tank; or the outlet of the halogen generation reactor is connected to a blowout tower, the gas outlet of the blowout tower is connected to the gas inlet of the absorption tank; or the vent of the halogen generating reactor is connected to the inlet of the condenser (collecting product bromine); or the discharge of the halogen generating reactor is connected to the inlet of a stratified tank, the bromine outlet of which is collected or the bromine outlet of which is connected to the inlet of an absorption tank.

Based on the above technical solution, it is preferable,

the halogen generation reactor is also provided with a feed inlet (oxidant such as chlorine, hydrogen peroxide, sulfuric acid and the like are fed, or acid required by acidification is also fed at the same time, or gas (such as air) is also required to be fed, and the feed inlet can be the same feed inlet or can be a plurality of feed inlets); blowing out elemental bromine from an exhaust port of the halogen generation reactor by using gas, and then absorbing the elemental bromine by using the absorption tank, wherein an absorbent is arranged in the absorption tank;

or the halogen generation reactor is also provided with a feed inlet (the feed inlet can be the same feed inlet or a plurality of feed inlets when oxidant such as chlorine, hydrogen peroxide, sulfuric acid and the like is fed or acid needed by acidification is also fed at the same time); the blowing tower is supplied with a gas (e.g., air) and the elemental bromine is blown out from the exhaust port of the halogen generating reactor by the gas and then absorbed by the absorption tank having an absorbent therein.

Based on the above technical scheme, preferably, the oxidant added in the halogen generating reactor is a conventional oxidant.

Based on the above technical scheme, preferably, the conventional oxidant of the halogen generation reactor is chlorine, hydrogen peroxide, sulfuric acid, etc.

Based on the above technical scheme, preferably, the absorbent of the halogen generation reactor is alkali liquor, sulfur dioxide, sodium carbonate, and the like.

Based on the above technical scheme, preferably, the halogen generating reactor is also provided with an acid generating tank or a product tank, when the absorbent of the halogen generating reactor is sulfur dioxide, the absorbing tank is provided with a heating device and/or an air inlet device and a gas phase condensing device, and the gas phase condensing product (filled into the acid generating tank) is hydrobromic acid; or the absorption tank is discharged to an evaporation tank III, the evaporation tank III is provided with a heating device and a gas phase condensing device, and a condensation product (filled into a product tank) is hydrobromic acid; or the absorption tank is discharged to an evaporation tank III, the evaporation tank III is provided with an oxidant (such as chlorine, hydrogen peroxide or sulfuric acid) inlet and a gas-phase condensing device, and a condensation product (a product tank) is elemental bromine.

Based on the above technical solution, it is preferable that the heating heater is provided before the resin tank I, the resin tank II, the resin tank III, the resin tank IV, the resin tank V, the resin tank VI, the resin tank VII, the resin tank VIII, the resin tank X, or the resin tank XI.

Based on the above technical scheme, preferably, the electrolysis device comprises an electrolysis anode plate and an electrolysis cathode plate, and the electrolysis device is bromine for generating simple substances by electrolyzing bromine ions under the condition of direct current.

Based on the above technical solution, preferably, the electrolysis device is provided with a gas inlet, and an exhaust port of the electrolysis device is connected to a gas inlet of the absorption tank; or the exhaust port of the electrolysis device is connected to a blowout tower, and the gas outlet of the blowout tower is connected to the gas inlet of the absorption tank; or the exhaust of the electrolyzer is connected to the inlet of the condenser (collecting bromine); the bromine outlet of the electrolysis device is collected or connected to the inlet of the absorption tank; or the discharge port of the electrolysis device is connected to the inlet of the layering tank, and the bromine outlet of the layering tank is collected or connected to the inlet of the absorption tank.

Based on the above technical solution, it is preferable,

the gas inlet of the electrolysis device is used for feeding gas (such as air), elemental bromine is blown out from the exhaust port of the halogen generation reactor by using the gas, and then the elemental bromine is absorbed by the absorption tank, and the absorption tank is internally provided with an absorbent.

Based on the technical scheme, preferably, the absorbent is alkali liquor, sulfur dioxide, sodium carbonate and the like.

Based on the above technical scheme, preferably, the electrolysis device is also provided with an acid production tank or a product tank, when the absorbent is sulfur dioxide, the absorption tank is provided with a heating device and/or an air inlet device and a gas phase condensing device, and the condensed product (filled into the acid production tank) is hydrobromic acid; or the absorption tank is discharged to an evaporation tank III, the evaporation tank III is provided with a heating device and a gas phase condensing device, and the condensation product (filled into a product tank) is hydrobromic acid.

Based on the above technical scheme, preferably, the non-condenser of the gas phase condensing device of the electrolysis device is hydrogen, and is recycled.

Based on the technical scheme, preferably, the volatile acid generator is provided with an acid inlet pipeline, an exhaust port and a liquid outlet; or the volatile acid generator is provided with an acid inlet pipeline, an exhaust port, a liquid outlet, an air inlet and/or a heater.

Based on the above technical solution, preferably, the acid inlet pipe of the volatile acid generator is used for feeding the non-volatile acid.

Based on the above technical solution, preferably, the acid inlet pipe of the volatile acid generator is used for feeding the non-volatile acid, such as phosphoric acid, and the following reactions are performed: sodium bromide + phosphoric acid- & gthydrobromic acid + sodium dihydrogen phosphate, the principle is that the non-volatile acid is used for preparing volatile acid, and hydrobromic acid is prepared and volatilized.

Based on the above technical solution, preferably, hydrobromic acid is discharged from the exhaust port of the volatile acid generator and is collected into the acid-producing tank by a condenser.

Based on the above technical scheme, preferably, the liquid outlet of the volatile acid generator discharges sodium dihydrogen phosphate, residual phosphoric acid and sodium bromide.

Based on the above, it is preferred that the purpose of the air inlet (feed air or inert gas) and/or heater of the volatile acid generator is to facilitate evaporation of hydrobromic acid.

Based on the above technical solution, preferably, the evaporation tank I is replaced by an electrodialysis concentration device a or a reverse osmosis concentration device a; or the evaporation tank II is replaced by an electrodialysis concentration device b or a reverse osmosis concentration device b; or the evaporation tank is replaced by an electrodialysis concentration device I or a reverse osmosis concentration device I;

based on the above technical solution, preferably, the resin tank VIII is filled with an anionic resin.

Based on the above technical scheme, preferably, the resin tank VIII is filled with an anionic resin, and the anionic resin is preferably a resin having an adsorption effect on bromide ions.

Based on the above technical solution, preferably, the resin tank VIII is further provided with an inlet for a regeneration liquid, preferably an alkaline substance such as sodium hydroxide aqueous solution, potassium hydroxide aqueous solution, etc.

Based on the above technical solution, preferably, the resin tank VIII is further provided with a regeneration liquid inlet, which is preferably connected to an alkali pipeline or the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, or the bipolar membrane device one alkali-producing tank.

Based on the above technical scheme, preferably, the resin tank VI is filled with hydrogen type cationic resin.

Based on the above technical solution, preferably, the resin tank VI is further provided with an inlet and an outlet for a regeneration liquid;

based on the above technical solution, it is preferable that the resin tank VI is further provided with an inlet for a regeneration liquid, preferably an acidic substance such as an aqueous acetic acid solution, an aqueous hydrobromic acid solution, an aqueous hydrochloric acid solution, an aqueous sulfuric acid solution, or the like.

Based on the above technical solution, preferably, the inlet of the regeneration liquid of the resin tank VI is preferably connected to an acid pipeline or an acid generating tank of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, or the bipolar membrane device one.

Based on the above technical solution, preferably, the solid outlet of the crystallizer II, the solid outlet of the crystallizer VII or the solid outlet of the crystallizer one is connected to the solid inlet of a mixing and dissolving tank, which also has a liquid inlet, and the outlet of the mixing and dissolving tank is connected to the water inlet of the bipolar membrane device IV.

Based on the above technical scheme, preferably, the mixing and dissolving tank also has a liquid inlet for feeding pure water.

Based on the above technical scheme, preferably, the bipolar membrane device IV also comprises an acid production tank and an alkali production tank.

Based on the above technical solution, preferably, the acid-producing tank of the bipolar membrane device I is connected to an oxidation reaction system; or the acid-producing tank of the bipolar membrane device II is connected to an oxidation reaction system; or the acid-producing tank of the bipolar membrane device III is connected to an oxidation reaction system; or the acid generating tank of the bipolar membrane equipment I is connected to an oxidation reaction system; or the acid-producing tank of the halogen generation reactor is connected to an oxidation reaction system; or the acid-producing tank of the electrolysis device is connected to an oxidation reaction system; or the water outlet of the resin tank VI is connected to an oxidation reaction system; or the regenerated liquid outlet of the resin tank IV is connected to an oxidation reaction system; or the regenerated liquid outlet of the resin tank V is connected to an oxidation reaction system; or the acid generating tank of the volatile acid generator is connected to an oxidation reaction system; or the solid outlet of the filter V is connected to an oxidation reaction system; or the solid outlet of the filter IV is connected to an oxidation reaction system; or the solid outlet of the filter V is connected to a blending tank, the blending tank is also provided with an acid inlet, and the outlet of the blending tank is connected to an oxidation reaction system; or the solid outlet of the filter IV is connected to a tempering tank, the tempering tank is also provided with an acid inlet, and the outlet of the tempering tank is connected to an oxidation reaction system; or the bipolar membrane device IV acid generator tank is connected to an oxidation reaction system.

Based on the above technical solution, preferably, when the treatment system is the system for purifying and recycling a solid mixture, a crystallizer XII is further provided, an outlet of the crystallizer XII is connected to an inlet of a first solid-liquid separation device (for example, a filter), a liquid outlet or one of liquid outlets of the first solid-liquid separation device (for example, a filter) is connected to an inlet of an evaporation tank IV, the evaporation tank IV is further provided with an evaporated gas discharge pipeline, an outlet of the evaporation tank IV is connected to a feed inlet of the crystallizer I, and the crystallizer XII is further provided with a feed inlet.

Based on the above technical solution, preferably, the inlet of the crystallizer XII is preferably the outlet of the oxidation reactor of the PTA plant.

Based on the above technical solution, preferably, the crystallizer I, the crystallizer II, the crystallizer III, the crystallizer IV, the crystallizer V, the crystallizer VI, the crystallizer VII, the crystallizer VIII, the crystallizer X or the crystallizer one comprises a heated evaporation type crystallizer, i.e. a crystallizer which evaporates the solvent through heating and precipitates the solute into a solid form (i.e. the product is a solid), and is provided with an exhaust port.

Based on the above technical solution, preferably, the water outlet of the evaporation tank I, the water outlet of the evaporation tank II, or the water outlet of the evaporation tank III means that an aqueous solution is discharged from the evaporation tank I, the evaporation tank II, or the evaporation tank III, and the aqueous solution may also contain insoluble solids.

Based on the above technical scheme, preferably, the heating device I or the heating device II may be any device that can perform a heating function, such as a heater or a heating tank (matched with a heater), preferably a heating tank (matched with a heater), and the generated carbon dioxide gas can be dissipated into the air during the heating process.

Based on the above technical solution, it is preferable to provide a concentrating device and/or a cooling device IX at an arbitrary position, wherein the concentrating device concentrates the aqueous solution (or the aqueous solution containing insoluble substances) in order to provide a concentrated solution for the subsequent process; the cooling device IX is used for guaranteeing the normal operation of the back-end process to cool down.

Based on the above technical solution, preferably, at least one of the cooling device I, the cooling device II, the cooling device III, the cooling device IV, the cooling device V, the cooling device VI, the cooling device VII, the cooling device VIII, the cooling device IX, or the cooling device I includes a heat exchanger, a jacket cooler, a shell-and-tube cooler, a vacuum-pumping cooler, a cooling tank with an out-of-band circulation cooler, a mixed cryogenic liquid type cooling tank (e.g., mixed cryogenic water cooling); or at least one of the cooling device I, the cooling device II, the cooling device III, the cooling device IV, the cooling device V, the cooling device VI, the cooling device VII, the cooling device VIII, the cooling device IX or the cooling device I, including a heat exchanger, a jacket cooler, a shell-and-tube cooler, a vacuum-pumping cooler, a cooling tank with an external circulation cooler, a mixed low-temperature liquid type cooling tank (for example, mixed low-temperature water cooling) (i.e., a multi-stage cooling device series connection can be designed), and then a stirring tank with chilled water is arranged for cooling again; or the temperature rising heater comprises at least one of a heat exchanger, a jacket heater, a tube array heater and a heating tank with an external circulating heater (namely, a multi-stage temperature rising heating device can be designed to be connected in series).

Based on the above technical solution, preferably, the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, the bipolar membrane device IV or the bipolar membrane device one is treated by passing the dilute brine through the concentration device and then passing the dilute brine through the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, the bipolar membrane device IV or the bipolar membrane device one again.

Based on the above technical solution, preferably, the concentration device is preferably all devices playing a role in concentration, such as evaporation concentration device, reverse osmosis concentration device, electrodialysis concentration device and the like.

Based on the above technical solution, it is preferable,

the filter I, the filter II, the filter III, the filter IV, the filter V, the filter VI, the filter VII, the filter VIII, the filter IX, the filter X, the filter one, the solid-liquid separator XI, or the solid-liquid separator XII includes at least one of a positive pressure filter, a negative pressure filter, a centrifuge, and a layering tank.

Based on the above technical solution, preferably, the combustion device I may be replaced by a catalytic decomposition organic device I; the combustion equipment II can be replaced by equipment II for catalyzing and decomposing organic matters; or the combustion device III may be replaced by a catalytic decomposition organic device III.

Based on the above technical solution, preferably, the combustion device I, the combustion device II or the combustion device III refers to a device capable of combusting organic matters at a certain temperature (at a high temperature), and preferably an RTO-type combustion device.

Based on the above technical scheme, preferably, the catalytic decomposition organic matter device I, the catalytic decomposition organic matter device II or the catalytic decomposition organic matter device III refers to a device capable of catalytically decomposing organic matters at a certain temperature, and a catalyst is added inside, so that the operation temperature required by the catalytic decomposition organic matter device is generally lower than the operation temperature required by the RTO combustion device, and the heat energy consumption is small.

Based on the above technical solution, preferably, the nanofiltration unit I, the nanofiltration unit II, the nanofiltration unit III, the nanofiltration unit IV or the nanofiltration unit V at least comprises a nanofiltration membrane of one stage and one section, and may also comprise a nanofiltration membrane combination of one stage and multiple sections or a nanofiltration membrane combination of one stage and multiple sections.

Based on the above technical scheme, preferably, the reverse osmosis concentration device at least comprises a reverse osmosis membrane of one stage and one section, and can also comprise a reverse osmosis membrane combination of one stage and multiple sections or a reverse osmosis membrane combination of one stage and one section and a reverse osmosis membrane combination of multiple stages and multiple sections.

Based on the above technical scheme, preferably, the nanofiltration unit I, the nanofiltration unit II, the nanofiltration unit III, the nanofiltration unit IV, the electrodialysis device for purifying monovalent ions I, the electrodialysis device for purifying monovalent ions II, the electrodialysis device for purifying monovalent ions III, the electrodialysis device for purifying monovalent ions IV or the electrodialysis device for purifying monovalent ions V are further provided with a dilution tank and/or a preheater with the prior art device, and the dilution tank is further provided with a liquid inlet to increase the solubility of sodium carbonate and the like therein, so as to avoid precipitation in the nanofiltration unit I, the nanofiltration unit II, the nanofiltration unit III or the nanofiltration unit IV.

Based on the above technical solution, preferably, the liquid inlet of the dilution tank is connected to a pure water line.

Based on the above technical solution, preferably, the alkali adding device I or the alkali adding device II may be connected to an alkali pipeline, an alkali adding pump, or an alkali producing tank of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, the bipolar membrane device IV, or the bipolar membrane device one.

Based on the above technical solution, preferably, the heating device I or the heating device II may be a heating tank, a jacket tank, a reheater+a heating tank, or the like.

Based on the above technical solution, preferably, the acid adding device is connected to an acid pipeline, an acid pump or an acid generating tank of the bipolar membrane device I, the bipolar membrane device II, the bipolar membrane device III, the bipolar membrane device IV or the bipolar membrane device I.

Based on the above technical scheme, preferably, the acid added by the acid adding device is preferably hydrobromic acid or acetic acid.

Based on the above technical solution, preferably, the solid outlet of the crystallizer III, the solid outlet of the crystallizer V, the solid outlet of the crystallizer VI, the solid outlet of the crystallizer VIII, the solid outlet of the first crystallizer X, the solid outlet of the filter II, the solid outlet of the filter III, the solid outlet of the filter IX, the water outlet of the halogen generating reactor, the water outlet of the electrolysis device or the water outlet of the resin tank VIII are connected to the dosing port of the mixing tank V.

Based on the above technical solution, preferably, the cathode position of the electrolysis device is connected to a gas collection device for collecting hydrogen.

Based on the above technical solution, preferably, the gas outlet of the absorption tank is connected to a gas collecting device for collecting hydrogen.

Based on the technical scheme, preferably, a pump is used as conveying power in the whole flow; or the nanofiltration unit I, the nanofiltration unit II, the nanofiltration unit III, the nanofiltration unit IV or the nanofiltration unit V is preceded by a high-pressure pump; or a high pressure pump is also required before the reverse osmosis membrane.

Based on the technical scheme, preferably, a buffer tank or a solid water adding dissolving tank is arranged at any position in the process for the stable operation of the device.

Advantageous effects

For solid materials containing organic matters and inorganic bromide ions; or an aqueous solution containing carbonate and/or bicarbonate and bromide ions, the component content of which is complex and cannot be directly used as a pure substance or can not be industrially utilized; the utility model provides a system which can purify the material to obtain a single substance and can be directly used as a product to obtain the economic value; the single substance can be reused in the working condition of required use to recycle the economic value, so the method is very significant for the energy recycling of the single substance.

For example, sodium carbonate is obtained which can be used as alkaline substance for organic matter dissolution and heavy metal precipitation; sodium bromide may be used as a product; hydrobromic acid can be used as a catalyst for the oxidation reaction.

In addition, in the system of the utility model, as the temperature of the solid outlet of the crystallizer I is high, the cooling equipment I is designed after the mixing tank I, so that the amount of cold water added into the mixing tank I can be reduced (namely, the cooling equipment I is used for cooling to replace part of the cold water added for cooling) under the aim of achieving a fixed cooling temperature value (for example, cooling to normal temperature), and the problem of high water consumption caused by adding cold water is solved; and the defects that the dilution concentration of substances is reduced and the subsequent system is difficult to treat low-concentration materials due to the fact that cold water is added are avoided.

Meanwhile, the system is simple, is easy to operate and is suitable for application.

Drawings

Fig. 1: example I-1 schematic diagram of a solid mixture purification and reuse system;

fig. 2: example I-2 schematic diagram of a solid mixture purification and reuse system;

fig. 3: example I-3 schematic diagram of a solid mixture purification and reuse system;

fig. 4: example I-4 schematic diagram of a solid mixture purification and reuse system;

fig. 5: example I-5 schematic of a solid mixture purification and reuse system;

fig. 6: example I-6 schematic diagram of a solid mixture purification and reuse system;

fig. 7: example I-7 schematic of a solid mixture purification and reuse system;

Fig. 8: example I-8 schematic diagram of a solid mixture purification and reuse system;

fig. 9: example I-9 schematic of a solid mixture purification and reuse system;

fig. 10: example I-10 schematic of a solid mixture purification and reuse system;

fig. 11: example I-11 schematic of a solid mixture purification and reuse system;

fig. 12: example I-12 schematic of a solid mixture purification and reuse system;

fig. 13: example I-13 schematic of a solid mixture purification and reuse system;

fig. 14: examples I-14 schematic illustrations of solid mixture purification and reuse systems;

fig. 15: examples I-15 schematic diagrams of solid mixture purification and reuse systems;

fig. 16: example I-16 schematic of a solid mixture purification and reuse system;

fig. 17: examples I-17 schematic diagrams of solid mixture purification and reuse systems;

fig. 18: examples I-18 schematic diagrams of solid mixture purification and reuse systems;

fig. 19: examples I-19 schematic diagrams of solid mixture purification and reuse systems;

fig. 20: example I-20 schematic of a solid mixture purification and reuse system;

fig. 21: example II-1 schematic diagram of an aqueous solution purification and reuse system;

Fig. 22: example II-2 schematic diagram of an aqueous solution purification and reuse system;

fig. 23: example II-3 schematic diagram of an aqueous solution purification and reuse system;

fig. 24: example II-4 schematic diagram of an aqueous solution purification and reuse system;

fig. 25: example II-5 schematic diagram of an aqueous solution purification and reuse system;

fig. 26: example II-6 schematic diagram of an aqueous solution purification and reuse system;

fig. 27: example II-7 schematic diagram of an aqueous solution purification and reuse system;

fig. 28: example II-8 schematic diagram of an aqueous solution purification and reuse system;

fig. 29: example II-9 schematic of an aqueous purification and reuse system;

fig. 30: example II-10 schematic of an aqueous purification and reuse system;

fig. 31: example II-11 schematic illustration of an aqueous purification and reuse system;

fig. 32: example II-12 schematic illustration of an aqueous purification and reuse system;

fig. 33: example II-13 schematic diagram of an aqueous solution purification and reuse system;

fig. 34: a schematic connection of electrodialysis equipment for purifying monovalent ions;

fig. 35: ion migration schematic diagram of electrodialysis apparatus for purifying monovalent ions.

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Detailed Description

The following non-limiting examples will enable those of ordinary skill in the art to more fully understand the utility model and are not intended to limit the utility model in any way.

Example I-1

As shown in fig. 1, the system for purifying and recycling the solid mixture mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a resin tank V34, an advanced oxidation reactor 31, a filter VIII32, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank V34, the water outlet of the resin tank V34 is connected to the water inlet of the advanced oxidation reactor 31, the advanced oxidation reactor 31 is also provided with a dosing port 33, the water outlet of the advanced oxidation reactor 31 is connected to the filter VIII32, the solid outlet of the filter VIII32 is collected, the liquid outlet of the filter VIII32 is connected to the water inlet of the bipolar membrane device I28, and the bipolar membrane device I28 is provided with an acid production tank 29 and an alkali production tank 30.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the solid is filtered by a filter I5 after being cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105, the solid is collected, filtrate enters a resin tank V34 for treatment, then enters a high-grade oxidation reactor II31 for oxidation reaction, and filtrate filtered by a filter VIII32 enters bipolar membrane equipment I28 for treatment.

The experiment was run using the above processing system: the normal-temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, and ferrous bromide and hydrogen peroxide are fed into the high-grade oxidation reactor II31 when the chemical feeding port 33 is subjected to oxidation reaction; when the oxidation reaction is terminated, 20% sodium hydroxide liquid is added, resin tank V34 is filled with resin with adsorption capacity to cobalt ions and manganese ions, and after resin tank V34 is saturated, the resin tank V34 is regenerated by 5% hydrobromic acid.

Experimental results:

the outlet of the mixing tank I3 was visually turbid and the liquid outlet 7 of the sampling filter I5 was water sample analyzed as follows: ba= 14155ppm, cobalt ion=4432 ppm, manganese ion=2879 ppm, sodium ion=1305 ppm, bromide ion=6843 ppm.

The drain water sample analysis of the resin tank V34 (filled with a resin having an adsorption effect on heavy metal ions) is as follows: ba=14001 ppm, cobalt ion=0.4 ppm, manganese ion=0.2 ppm, sodium ion=1287 ppm, bromide ion=6882 ppm.

The higher oxidation reactor 31 is used for discontinuous reaction, the PH=2.5 is controlled for half an hour in the reaction, sodium hydroxide is added after the higher oxidation reaction is finished to control the PH=10.5, the reaction is stopped, and the water sample at the liquid outlet of the filter VIII32 is: ba=664 ppm, cobalt ion undetectable, manganese ion undetectable, sodium= 13341ppm, bromine= 22122ppm.

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.53%, sodium ion 121ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.44%, bromide ion 433ppm.

Conclusion: the concentration of cobalt ions and manganese ions is reduced after the treatment of the resin tank V34, the concentration of BA is reduced after the treatment of the resin tank V34, only sodium and bromine remain in a liquid outlet water sample of the filter VIII32, and the target hydrobromic acid is obtained from the acid production tank 29 of the bipolar membrane equipment I28 and the target sodium hydroxide is obtained from the alkali production tank 30 of the bipolar membrane equipment I28;

it was demonstrated that the advanced oxidation reactor 31 can reduce BA in water and act to reduce COD.

Example I-2

As shown in fig. 2, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a higher oxidation reactor II31, a filter VIII32, a neutralization tank 94, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumizing cooler 104, the vacuumizing cooler 104 is vacuumized, the outlet of the vacuumizing cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the mixing tank V46, the mixing tank V46 is also provided with a dosing port, the water outlet of the mixing tank V46 is connected to the inlet of the filter V47, the liquid outlet of the filter V47 is connected to the water inlet of the advanced oxidation reactor II31, the advanced oxidation reactor II31 is also provided with a dosing port 33, the water outlet of the advanced oxidation reactor 31 is connected to the filter VIII32, the solid outlet of the filter VIII32, the liquid outlet of the filter VIII32 is connected to the inlet of the neutralization tank 94, the neutralization tank 94 is also provided with an acid adding device I97, the water inlet of the neutralization tank 94 is also provided with an outlet membrane device I28, the membrane device I28 is provided with an alkaline producing membrane device I28, and the bipolar acid producing device I29 is connected to the bipolar acid producing tank I29.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a mixing tank V46 to be added with chemicals, the filtrate is filtered by a filter V47 and then enters a high-grade oxidation reactor II31 to be subjected to oxidation reaction, the filtrate filtered by a filter VIII32 is neutralized by a neutralization tank 94 and then enters a bipolar membrane device I28 to be treated, and a part of hydrobromic acid in an acid production tank 29 of the bipolar membrane device I28 is returned to provide hydrobromic acid for an acid adding device I97.

The experiment was run using the above processing system: the normal-temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, and ferrous bromide and hydrogen peroxide are fed into the high-grade oxidation reactor II31 when the chemical feeding port 33 is subjected to oxidation reaction; upon termination of the oxidation reaction, 20% sodium hydroxide solution is fed, mixing tank V46 is fed with 8% sodium carbonate aqueous solution (i.e., the chemical added to mixing tank V46), and the acid addition unit 97 of neutralization tank 94 is fed with hydrobromic acid.

Experimental results:

The water sample analysis of the liquid outlet of filter V47 was as follows: ba=11023 ppm, cobalt ion=0.2 ppm, manganese ion=0.1 ppm, sodium ion=8145 ppm, bromide ion=5201 ppm.

The higher oxidation reactor 31 is used for discontinuous reaction, the PH=2.5 is controlled for half an hour in the reaction, sodium hydroxide is added after the higher oxidation reaction is finished to control the PH=10.5, the reaction is stopped, and the water sample at the liquid outlet of the filter VIII32 is: ba=711 ppm, cobalt ion undetectable, manganese ion undetectable, sodium= 18422ppm, bromine= 23233ppm.

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.57%, sodium ion 162ppm;

the caustic soda pot 30 of bipolar membrane apparatus I28 controls 1.5mo1/L hydroxide, detection: sodium ion 3.41% and bromide ion 211ppm.

Conclusion: the concentration of cobalt ions and manganese ions after treatment by the mixing tank V46 and the filter V47 is reduced, and the effect is the same as that of the resin tank V34 of the embodiment I-1, so that the mixing tank V46 and the filter V47 can be exchanged with the resin tank V34, and the effect is the same, and the mixing tank V46 and the filter V47 can be alternatively used.

The concentration of BA is reduced after passing through the advanced oxidation reactor 31, only sodium and bromine remain in a liquid outlet water sample of the filter VIII32, and hydrobromic acid and sodium hydroxide aqueous solution can be obtained after treatment by the bipolar membrane equipment I28; it has also been demonstrated that the advanced oxidation reactor 31 can reduce BA in water, and has the function of reducing COD.

Example I-3

As shown in fig. 3, the system for purifying and recycling the solid mixture mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a resin tank V34, an extraction tank 19, a separation tank 20, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumized cooler 104, a negative pressure is pumped above the vacuumized cooler 104, the outlet of the vacuumized cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6, a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the extraction tank 19, the extraction tank 19 is also connected with an extractant inlet 21, the outlet of the extraction tank 19 is connected to the separation tank 20, the separation tank 20 has an extractant outlet 22 and a water outlet 23, the water outlet 23 of the separation tank 20 is connected to the water inlet of the resin tank V34, the water outlet of the resin tank V34 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the bipolar membrane device I28, and the bipolar membrane device I28 is provided with an acid-producing tank 29, an alkali-producing tank 30.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters the mixing tank I3, pure water is fed from the liquid inlet 4 of the mixing tank I3, the solid is filtered by the filter I5 after being cooled by the vacuumizing cooler 104 and the cooling heat exchanger 105, the solid is collected, the filtrate enters the extraction tank 19 for extraction, the extraction is layered by the separation tank 20, the aqueous solution in the separation tank 20 enters the resin tank V34 for treatment after exiting from the water outlet 23, and the aqueous solution enters the bipolar membrane device I28 for treatment after being concentrated by the reverse osmosis concentration device 305.

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the outlet water of the cooling heat exchanger 105 is controlled to be 25 ℃, the benzene is fed into the extractant inlet 21 of the extracting tank 19, the resin tank V34 is filled with resin with adsorption capability to cobalt ions and manganese ions, and the resin tank V34 is regenerated by 5 percent hydrobromic acid after being saturated.

Experimental results:

Water outlet 23 of separator tank 20 tested ba=311 ppm;

the drain water sample analysis of the resin tank V34 (filled with a resin having an adsorption effect on heavy metal ions) is as follows: ba=401 ppm, cobalt ion=0.7 ppm, manganese ion=0.1 ppm, sodium ion=1221 ppm, bromide ion=6572 ppm.

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.62% and sodium ion 85ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.51 ppm and bromide ion 311ppm.

Conclusion: the concentration of BA is reduced through the extraction device, the concentration of cobalt ions and manganese ions is reduced after the treatment of the resin tank V34, and the aqueous solution of hydrobromic acid and sodium hydroxide is obtained after the treatment of the bipolar membrane equipment I28.

Meanwhile, the concentration of BA is reduced after the treatment of the extraction tank 19, and the effect of reducing COD is achieved, so that the effects of the advanced oxidation reactor and the extraction device are the same, the COD can be reduced, and the advanced oxidation reactor and the extraction device can be exchanged for use.

Example I-4

As shown in fig. 4, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a resin tank V34, an acidification tank 24, a filter VII25, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuum cooler 104, a negative pressure is applied above the vacuum cooler 104, the outlet of the vacuum cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6, a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank V34, the water outlet of the resin tank V34 is connected to the water inlet of the acidification tank 24, the acidification tank 24 is also connected with an acidification line 26, the water outlet of the acidification tank 24 is connected to the filter VII25, the solid outlet collection of the filter VII25 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the bipolar membrane device I28, the bipolar membrane device I28 is provided with an acid production tank 29, an alkali production tank 30, the acid production tank 29 of the bipolar membrane device I28 is connected to the acidification line 26.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters the mixing tank I3, pure water is fed from the liquid inlet 4 of the mixing tank I3, the solid is filtered by the filter I5 after being cooled by the vacuumizing cooler 104 and the cooling heat exchanger 105, the solid is collected, the filtrate enters the resin tank V34 for treatment, then enters the acidification tank 24 for acid addition, the filtrate after being filtered by the filter VII25 is concentrated by the reverse osmosis concentration device 305 and then enters the bipolar membrane device I28 for treatment, and part of the acid production tank 29 of the bipolar membrane device I28 provides hydrobromic acid for the acid addition pipeline 26.

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, hydrobromic acid is fed into the acid adding pipeline 26 of the acidification tank 24, the resin tank V34 is filled with resin with adsorption capability on cobalt ions and manganese ions, and the resin tank V34 is regenerated by 5 percent hydrobromic acid after being saturated.

Experimental results:

Outlet water sample from filter VII 25: ba=954 ppm, cobalt ion=0.3 ppm, manganese ion=0.4 ppm, sodium ion=966 ppm, bromide ion=4918 ppm;

the acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.67%, sodium ion 45ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.57%, bromide ion 131ppm.

Conclusion: the concentration of cobalt ions and manganese ions is reduced after the treatment of the resin tank V34, the concentration of BA is reduced after the acidification tank 24 and the filter VII25, only sodium and bromine remain in a liquid outlet water sample of the filter VII25, and hydrobromic acid can be obtained after the treatment of the bipolar membrane equipment I28;

meanwhile, the acidification tank 24 and the filter VII25 can reduce BA in water and play a role in reducing COD, so that the concentration of effluent BA of the advanced oxidation reactor, the extraction device and the acidification device is reduced to a great extent, the effects and the roles are the same, and the advanced oxidation reactor, the extraction device and the acidification device can be exchanged for alternative use.

Example I-5

As shown in fig. 5, the system for purifying and recycling the solid mixture mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a resin tank V34, a resin tank II27, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumized cooler 104, the vacuumized cooler 104 is vacuumized above, the outlet of the vacuumized cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank II27, the water outlet of the resin tank II27 is connected to the water inlet of the resin tank V34, the water outlet of the resin tank V34 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the bipolar membrane device I28, and the bipolar membrane device I28 is provided with an acid-producing tank 29 and an alkali-producing tank 30.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the mixture is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a resin tank II27 and a resin tank V34 for treatment and then enters a bipolar membrane device I28 for treatment after being concentrated by a reverse osmosis concentration device 305.

The experiment was run using the above processing system: the liquid inlet 4 of the mixing tank I3 is fed with normal-temperature pure water, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the outlet water of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank II27 is filled with resin with adsorption capability to BA, the resin tank V34 is filled with resin with adsorption capability to cobalt ions and manganese ions, the resin tank V34 is regenerated by 5 percent hydrobromic acid after being saturated, and the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated.

Experimental results:

The drain water sample of resin tank II27 (filled with a resin having adsorption effect on BA) was analyzed as follows: ba=12 ppm, cobalt ion=4412 ppm, manganese ion=2798 ppm, sodium ion=1296 ppm, bromide ion=6811 ppm.

The drain water sample of the resin tank V34 (filled with resin having adsorption effect on cobalt ion and manganese ion) was analyzed as follows: ba=7 ppm, cobalt ion=1.1 ppm, manganese ion=0.2 ppm, sodium ion=1256 ppm, bromide ion=6875 ppm.

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.55%, sodium ion 345ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.64%, bromide ion 319ppm.

Conclusion: the concentration of BA is reduced after the treatment of a resin tank II27, the concentration of cobalt ions and manganese ions is reduced after the treatment of a resin tank V34, and only sodium and bromine remain in a liquid water sample after the treatment, and hydrobromic acid and sodium hydroxide are obtained after the treatment of a bipolar membrane device I28;

meanwhile, the resin tank II27 can reduce BA in water and play a role in reducing COD, so that the concentration of effluent BA of an advanced oxidation reactor, an extraction device, an acidification device, a resin tank (filled with resin with adsorption effect on organic matters) and the like is reduced to a great extent, the effects and the roles are the same, and the advanced oxidation reactor, the extraction device, the acidification device and the resin tank (filled with resin with adsorption effect on organic matters) can be interchanged for alternative use.

Example I-6

As shown in fig. 6, the system for purifying and recycling the solid mixture mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a resin tank V34, a resin tank II27, an electrodialysis device IV35, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of a mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of a vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of a cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to a filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of an electrodialysis device IV35, the water outlet I36 of the electrodialysis device IV35 is connected to the water inlet of a resin tank II27, the water outlet of the resin tank II27 is connected to the water inlet of a resin tank V34, the water outlet of the resin tank V34 is connected to the water inlet of a reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of a bipolar membrane device I28, and the bipolar membrane device I28 is provided with an acid production tank 29 and an alkali production tank 30; the water outlet II37 of the electrodialysis device IV35 is connected to the water inlet of the mixing tank IV13, the mixing tank IV13 also has a dosing port 14, the water outlet of the mixing tank IV13 is connected to the water inlet of the filter IV15, the liquid outlet 16 of the filter IV15 discharges, and the solid outlet 17 of the filter IV15 collects.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the mixture is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters electrodialysis equipment IV35 for treatment, aqueous solution at a water outlet I36 of the electrodialysis equipment IV35 enters a resin tank II27 and then enters a resin tank V34 for treatment, and then enters bipolar membrane equipment I28 for treatment after being concentrated by a reverse osmosis concentration equipment 305; the aqueous solution at the water outlet II37 of the electrodialysis device IV35 is filtered through the filter IV15 after passing through the mixing tank IV13 (chemicals are added), and the filter cake of the filter IV15 is collected.

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank II27 is filled with the resin with adsorption capability to BA, the resin tank V34 is filled with the resin with adsorption capability to cobalt ions and manganese ions, the resin tank V34 is regenerated by 5 percent hydrobromic acid after being saturated, the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated, and the 8 percent sodium carbonate aqueous solution is fed into the feed inlet 14 of the mixing tank IV 13.

Experimental results:

The water sample at the water outlet I36 of the electrodialysis device IV35 is analyzed as follows: ba=3122 ppm, cobalt ion=5503 ppm, manganese ion=3105 ppm, sodium ion=1487 ppm, bromide ion=7612 ppm

The drain water sample of resin tank II27 (filled with a resin having adsorption effect on BA) was analyzed as follows: ba=4 ppm, cobalt ion=5515 ppm, manganese ion=3098 ppm, sodium ion=1513 ppm, bromide ion=7588 ppm.

The drain water sample analysis of the resin tank V34 (filled with a resin having an adsorption effect on heavy metal ions) is as follows: ba=8 ppm, cobalt ion=0.3 ppm, manganese ion=0.4 ppm, sodium ion=1521 ppm, bromide ion=7606 ppm.

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromide ion 9.48% and sodium ion 277ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.60%, bromide ion 188ppm.

Conclusion: the concentration of BA is reduced after the treatment of electrodialysis equipment IV35, the concentration of BA is reduced after the treatment of a resin tank II27, the concentration of cobalt ions and manganese ions is reduced after the treatment of a resin tank V34, only sodium and bromine remain in a liquid water sample, and hydrobromic acid and sodium hydroxide are obtained after the treatment of bipolar membrane equipment I28;

Meanwhile, the electrodialysis device IV35 can reduce BA in water and play a role in reducing COD, so that the concentration of discharged water BA of an advanced oxidation reactor, an extraction device, an acidification device, a resin tank (filled with resin with adsorption effect on organic matters), the electrodialysis device and the like is reduced to a great extent, the effects and the roles of the advanced oxidation reactor, the extraction device, the acidification device, the resin tank (filled with resin with adsorption effect on organic matters) and the electrodialysis device are the same, and the advanced oxidation reactor, the extraction device, the acidification device and the resin tank (filled with resin with adsorption effect on organic matters) can be interchanged for alternative use.

This example also demonstrates that for different ways of reducing the COD unit, more than one device can be selected, for example the embodiment is implemented by selecting the electrodialysis device IV35+ resin tank II 27.

Example I-7

As shown in fig. 7, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank II27, a nanofiltration unit I106, a neutralization tank 94, a bipolar membrane device I28 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuuming cooler 104, the vacuuming cooler 104 is vacuumized and the outlet of the vacuuming cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank II27, the water outlet of the resin tank II27 is connected to the water inlet of the mixing tank V46, the water inlet of the mixing tank V46 is also provided with a dosing port 48, the water outlet of the mixing tank V46 is connected to the inlet of the filter V47, the liquid outlet of the filter V47 is connected to the water inlet of the high-pressure pump 216, the water outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit I106, the fresh water outlet 107 of the nanofiltration unit I106 is connected to the inlet of the neutralization tank 94, the neutralization tank 94 is also provided with an acid dosing unit 97, the outlet of the neutralization tank 94 is connected to the water inlet of the membrane device I28, the membrane device 28 is provided with the acid producing device I28, the acid producing device 29, the acid producing unit I29 is connected to the bipolar acid outlet of the bipolar membrane device I29, and the bipolar acid producing unit I29 is connected to the bipolar acid tank I28, and the bipolar acid producing the acid outlet of the bipolar unit I29 is connected to the bipolar acid tank I29.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a resin tank II27 for treatment and then enters a mixing tank V46 for adding chemicals, the filtrate is filtered by a filter V47 and then enters a nanofiltration unit I106, and fresh water of the nanofiltration unit I106 is neutralized by a neutralization tank 94 and then enters bipolar membrane equipment I28 for treatment; the concentrated water from nanofiltration unit I106 enters mixing tank V46 (i.e., the chemicals added by mixing tank V46), and one of the outlets of acid generator tank 29 of bipolar membrane apparatus I28 provides hydrobromic acid to acid addition unit 97.

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, the resin tank II27 is filled with the resin with adsorption capacity to BA, the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated, the 8 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, and the hydrobromic acid is fed into the acid adding unit 97 of the neutralization tank 94.

Experimental results:

Liquid outlet ba=8 ppm, cobalt ion=0.6 ppm, manganese ion=0.1 ppm, sodium ion=13123 ppm, bromide ion=5725 ppm of filter V47.

And (3) discharging water from a neutralization tank 94: ph=3.1, bromide= 35413ppm.

Concentrated water outlet 108 water sample analysis of nanofiltration unit I106: ph=9.6, carbonate=11035 ppm;

the acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.33% and sodium ion 68ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.72% and bromide ion 96ppm.

Conclusion: the concentration of BA is reduced after the treatment of the resin tank II27, and then the concentration of cobalt ions and manganese ions is reduced after the treatment of the mixing tank V46 and the filter V47, and as the cobalt and manganese ions are precipitated by adding carbonate, the carbonate in the filter V47 is treated by the nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of the nanofiltration, the reflux is used for the precipitation of cobalt and manganese again, the fresh water of the nanofiltration unit I106 is mainly sodium bromide, and the residual carbonate is reacted again by the neutralization tank 94 and then enters the bipolar membrane equipment I28 for treatment.

Meanwhile, as can be deduced from examples I-1 to I-6, the replacement of the resin tank II27 with a higher oxidation, extraction, acidification, electrodialysis device also plays a role in reducing COD, and the same results as in this example are obtained.

Example I-8

As shown in fig. 8, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank II27, a nanofiltration unit I106, a neutralization tank 94, a crystallizer II49 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuum cooler 104, a negative pressure is applied above the vacuum cooler 104, the outlet of the vacuum cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6, a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank II27, the water outlet of the resin tank II27 is connected to the water inlet of the mixing tank V46, the water inlet of the mixing tank V46 also has a dosing port 48, the water outlet of the mixing tank V46 is connected to the inlet of the filter V47, the liquid outlet of the filter V47 is connected to the water inlet of the high pressure pump 216, the water outlet of the high pressure pump 216 is connected to the water inlet of the nanofiltration unit I106, the fresh water outlet 107 of the nanofiltration unit I106 is connected to the inlet of the neutralization tank 94, the neutralization tank 94 also has an acid and alkali adding unit III140, the outlet of the neutralization tank 94 is connected to the crystallizer II49, the water outlet 108 is connected to the concentrated water inlet of the mixing tank V46.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is filtered by a filter I5 after being cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105, the solid is collected, filtrate enters a resin tank II27 for treatment and then enters a mixing tank V46 for adding chemicals, the filtrate enters a nanofiltration unit I106 after being filtered by a filter V47, the fresh water of the nanofiltration unit I106 is neutralized by a neutralization tank 94 (the PH value is reduced to about 3 by an acid adding unit 97 for reaction to remove carbonate, then sodium hydroxide is added by an alkali adding unit III140 for regulating the PH value to be neutral for reaction to remove residual hydrobromic acid), and then the fresh water enters a crystallizer II49; the concentrated water of the nanofiltration unit I106 enters the mixing tank V46 (namely the chemicals added by the mixing tank V46).

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank II27 is filled with the resin with adsorption capacity to BA, the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated, the 8 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, and the hydrobromic acid is fed into the acid adding unit 97 of the neutralization tank 94 and the 10 percent sodium hydroxide is fed into the alkali adding unit III 140.

Experimental results:

And (3) discharging water from a neutralization tank 94: ph=7.0.

crystallizer II49 analyzed sodium bromide purity 98.5%.

Conclusion: the concentration of BA is reduced after the treatment of the resin tank II27, the concentration of cobalt ions and manganese ions is reduced after the treatment of the mixing tank V46 and the filter V47, and as the cobalt and manganese ions are precipitated by adding carbonate, the carbonate in the filter V47 is treated by the nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of nanofiltration, the reflux is used for precipitating cobalt and manganese again, the fresh water of the nanofiltration unit I106 is mainly sodium bromide, the residual carbonate is reacted again by the neutralization tank 94 and the free hydrobromic acid is neutralized by alkali, and then the sodium bromide enters the crystallizer II49 to be heated and evaporated to crystallize sodium bromide solid. Meanwhile, as can be deduced from examples I-1 to I-6, the replacement of the resin tank II27 with a higher oxidation, extraction, acidification, electrodialysis device also plays a role in reducing COD, and the same results as in this example are obtained.

Examples I-9

As shown in fig. 9, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuum-pumping cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank III41, a nanofiltration unit I106, a halogen generation reactor 38 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumized cooler 104, the vacuumized cooler 104 is vacuumized above, the outlet of the vacuumized cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank III41, the water outlet of the resin tank III41 is connected to the water inlet of the mixing tank V46, the water inlet of the mixing tank V46 also has a medicine adding port 48, the water outlet of the mixing tank V46 is connected to the inlet of the filter V47, the liquid outlet of the filter V47 is connected to the water inlet of the high-pressure pump 216, and the water outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit I106;

The fresh water outlet 107 of the nanofiltration unit I106 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 discharges, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the halogen generating reactor 38, the halogen generating reactor 38 is further provided with a dosing port 40, the halogen generating reactor 38 is further provided with a water outlet 103, the gas outlet of the halogen generating reactor 38 is connected to the absorption tank 39, the absorption tank 39 is further provided with a dosing port 44, the outlet of the absorption tank 39 is connected to the inlet of the evaporation tank III42, the top gas phase of the evaporation tank III42 is provided with a condenser 43, the outlet of the condenser 43 is connected to the acid production tank 45, and the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the solid is filtered by a filter I5 after being cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105, the solid is collected, filtrate enters a resin tank III41 for treatment and then enters a mixing tank V46 for adding chemicals, and after being filtered by a filter V47, the filtrate enters a nanofiltration unit I106;

fresh water of the nanofiltration unit I106 is concentrated through reverse osmosis concentration equipment 305 and then enters a halogen generation reactor 38, chlorine and sulfuric acid are fed into a dosing port 40 of the halogen generation reactor 38, and pressurized air is used for blowing out elemental bromine, elemental bromine gas is absorbed by an absorption tank 39, sulfur dioxide and water are fed into the absorption tank 39 from a dosing port 44, and aqueous solution in the absorption tank 39 is condensed by a condenser 43 after being evaporated by an evaporation tank III42 and then is collected in an acid production tank 45; the concentrated water of the nanofiltration unit I106 enters the mixing tank V46 (namely the chemicals added by the mixing tank V46).

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90%, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank III41 is filled with resin with adsorption capacity to BA, the resin tank III41 is regenerated by 5% sodium hydroxide after being saturated, the chlorine, sulfuric acid and air are fed into the medicine feeding port 40 of the halogen generating reactor 38, the sulfur dioxide and water are fed into the medicine feeding port 44 of the absorption tank 39, and the 8% sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage.

Experimental results:

The drain water sample analysis of resin tank III41 (filled with a resin having adsorption effect on BA) is as follows: ba=12 ppm, cobalt ion=4412 ppm, manganese ion=2798 ppm, sodium ion=1296 ppm, bromide ion=6811 ppm.

The acid generator tank 45 analyzes the sodium bromide for 18.1% purity.

Conclusion: the concentration of BA is reduced after being treated by a resin tank III41, and then the concentration of cobalt ions and manganese ions is reduced after being treated by a mixing tank V46 and a filter V47, and as carbonate is added to precipitate cobalt and manganese ions, the carbonate in the filter V47 is treated by a nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of nanofiltration, the reflux is used for precipitating cobalt and manganese again, fresh water of the nanofiltration unit I106 is mainly sodium bromide, residual carbonate is reacted again by a neutralization tank 94 and then enters a halogen generation reactor 38 and an accessory device thereof, and hydrobromic acid is obtained in an acid production tank 45 of the halogen generation reactor 38.

Meanwhile, as can be deduced from examples I-1 to I-6, the replacement of the resin tank III41 with an advanced oxidation, extraction, acidification, electrodialysis device also plays a role in reducing COD, and the same results as in this example are obtained.

Examples I to 10

As shown in fig. 10, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank III41, a nanofiltration unit I106, a neutralization tank 94, an electrolysis device 109 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumized cooler 104, the vacuumized cooler 104 is vacuumized above, the outlet of the vacuumized cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the resin tank III41, the water outlet of the resin tank III41 is connected to the water inlet of the mixing tank V46, the water inlet of the mixing tank V46 also has a medicine adding port 48, the water outlet of the mixing tank V46 is connected to the inlet of the filter V47, the liquid outlet of the filter V47 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit I106, the fresh water outlet 107 of the nanofiltration unit I106 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the inlet of the neutralization tank 94, the neutralization tank 94 is further provided with an acid adding unit 97, the outlet of the neutralization tank 94 is connected to the water inlet of the electrolysis device 109, the electrolysis device 109 is further provided with an air inlet 331, an anode 329, a cathode 330, the electrolysis device 109 is further provided with a water outlet 328, the air outlet of the electrolysis device 109 is connected to the absorption tank 39, the absorption tank 39 is further provided with a dosing port 44, the outlet of the absorption tank 39 is connected to the inlet of the evaporation tank III42, the top gas phase of the evaporation tank III42 is provided with a condenser 43, the outlet of the condenser 43 is connected to the acid generating tank 45, one of the outlets of the acid generating tank 45 is connected to the acid adding unit 97, and the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a resin tank III41 for treatment and then enters a mixing tank V46 for adding chemicals, the filtrate enters a nanofiltration unit I106 after being filtered by a filter V47, the fresh water of the nanofiltration unit I106 is concentrated by a reverse osmosis concentration device 305 and then neutralized by a neutralization tank 94, the concentrated fresh water enters an electrolysis device 109, an air inlet 331 of the electrolysis device 109 is fed with pressurized air, elemental bromine is blown out, the elemental bromine gas is absorbed by an absorption tank 39, sulfur dioxide and water are fed by the absorption tank 39 from a dosing port 44, the aqueous solution in the absorption tank 39 is condensed by a condenser 43 after being evaporated by an evaporation tank III42 and then is collected into an acid production tank 45, and the acid production tank 45 provides hydrobromic acid for an acid adding unit 97; the concentrated water of the nanofiltration unit I106 enters the mixing tank V46 (namely the chemicals added by the mixing tank V46).

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the temperature of 25 ℃ is controlled, the air is fed into the air inlet 331 of the electrolysis device 109, the sulfur dioxide and the water are fed into the medicine feeding port 44 of the absorption tank 39, the 15 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, and the hydrobromic acid is fed into the acid feeding unit 97 of the neutralization tank 94; the high pressure pump 216 is given a pressure of 4 MPa; loading resin with adsorption function to BA into resin tank III41, and regenerating with 8% sodium hydroxide after saturation; the anode 329 and cathode 330 of the electrolyzer 109 are given a voltage of 36V.

Experimental results:

And (3) discharging water from a neutralization tank 94: ph=3.5.

the acid generator tank 45 of the electrolyzer 109 analyzed sodium bromide for purity of 12.4%.

Conclusion: the concentration of BA is reduced after being treated by the resin tank III41, and then the concentration of cobalt ions and manganese ions is reduced after being treated by the mixing tank V46 and the filter V47, and as the cobalt and manganese ions are precipitated by adding carbonate, the carbonate in the filtrate of the filter V47 is treated by the nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of nanofiltration, the reflux is used for precipitating cobalt and manganese again, the fresh water of the nanofiltration unit I106 is mainly sodium bromide, the residual carbonate is reacted again by the neutralization tank 94 and then enters the electrolysis device 109 and the accessory device thereof, and hydrobromic acid is obtained in the acid production tank 45 of the electrolysis device 109.

Meanwhile, the previous embodiment also proves that the concentration of cobalt ions and manganese ions is reduced after the treatment of the mixing tank V46 and the filter V47, and the effect of the mixing tank V46 and the effect of the resin tank V34 are the same, and the mixing tank V46 and the filter V47 can be replaced alternatively.

Example I-11

As shown in fig. 11, a system for purifying and recycling a solid mixture mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank III41, a nanofiltration unit I106, a resin tank VIII110, a bipolar membrane device III112 and the like.

The connection mode is as follows:

The fresh water outlet 107 of the nanofiltration unit I106 is connected to the inlet of a resin tank VIII110, the outlet of the resin tank VIII110 is discharged, the resin tank VIII110 is provided with a regenerated liquid inlet 113, the regenerated liquid outlet 114 of the resin tank VIII110 is connected to the water inlet of a bipolar membrane device III112, and the bipolar membrane device III112 is provided with an acid production tank 115 and an alkali production tank 116; the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46.

The recovery process described above operates as follows:

fresh water of the nanofiltration unit I106 is discharged after bromide ions are adsorbed by the resin tank VIII110, and regenerated liquid of the resin tank VIII110 is treated by the bipolar membrane equipment III 112; the concentrated water of the nanofiltration unit I106 enters the mixing tank V46 (namely the chemicals added by the mixing tank V46).

The experiment was run using the above processing system: the inlet 4 of the mixing tank I3 is fed with normal-temperature pure water, the vacuumizing cooler 104 is vacuumized to 90% of vacuum degree, the cooling heat exchanger 105 is cooled by chilled water, the outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, the resin tank III41 is filled with resin with adsorption capacity to BA, the resin tank III41 is regenerated by 5% sodium hydroxide after being saturated, the mixing tank V46 is initially fed with 8% sodium carbonate aqueous solution, the resin tank VIII110 is filled with resin with adsorption effect to bromide ions, and the regenerated liquid inlet 113 of the resin tank VIII110 is fed with 8% sodium hydroxide aqueous solution.

Experimental results:

Outlet bromide=783 ppm of resin tank VIII 110;

regenerated liquid outlet 114 bromide= 61437ppm of resin tank VIII 110;

the acid generator tank 115 of the bipolar membrane device III112 controls hydrogen ions to 1.0mol/L, and detection is carried out: bromide ion 7.98% and sodium ion 175ppm;

the caustic soda tank 116 of bipolar membrane apparatus III112 controls 1.0mol/L hydroxyl, detection: sodium ion 2.36%, bromide ion 49ppm.

conclusion: the concentration of BA is reduced after the treatment of a resin tank III41, the concentration of cobalt ions and manganese ions is reduced after the treatment of a mixing tank V46 and a filter V47, and as carbonate is added to precipitate cobalt and manganese ions, the carbonate in the filter V47 is treated by a nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of nanofiltration, the reflux is used for precipitating cobalt and manganese again, fresh water of the nanofiltration unit I106 is mainly sodium bromide, bromide ions are adsorbed by a resin tank VIII110, the bromide ions are regenerated by sodium hydroxide after the adsorption saturation, the regenerated liquid is mainly sodium bromide and sodium hydroxide, and the target hydrobromic acid and sodium hydroxide aqueous solution are obtained by the treatment of a bipolar membrane device III 112.

Examples I-12

As shown in fig. 12, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank III41, a nanofiltration unit I106, a resin tank VI111, an oxidation reaction system 10 and the like.

The connection mode is as follows:

The fresh water outlet 107 of the nanofiltration unit I106 is connected to the inlet of a resin tank VI111, the outlet of the resin tank VI111 being connected to the oxidation reaction system 10; the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46.

The recovery process described above operates as follows:

fresh water of the nanofiltration unit I106 is adsorbed with sodium ions by the resin tank VI111 and then enters the oxidation reaction system 10; the concentrated water of the nanofiltration unit I106 enters the mixing tank V46 (namely the chemicals added by the mixing tank V46).

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent of vacuum degree, the cooling heat exchanger 105 is cooled by chilled water, the outlet water of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank III41 is filled with resin with adsorption capacity to BA, the resin tank III41 is regenerated by 5 percent sodium hydroxide after being saturated, the 8 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, the resin tank VI111 is filled with cationic resin, the resin tank VI111 is regenerated by 5 percent hydrochloric acid after being adsorbed and saturated, and the chlorine ions are washed by water and reused.

Experimental results:

Resin pot VI111 effluent: 15413ppm of bromide ion, 16ppm of sodium ion and 0.2mo1/L of hydrogen ion.

conclusion: the concentration of BA is reduced after the treatment of the resin tank III41, and then the concentration of cobalt ions and manganese ions is reduced after the treatment of the mixing tank V46 and the filter V47, and as the cobalt and manganese ions are precipitated by adding carbonate, the carbonate in the filter V47 is treated by the nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of the nanofiltration, the reflux is used for the precipitation of cobalt and manganese again, the fresh water of the nanofiltration unit I106 is mainly sodium bromide, and the sodium ions are absorbed by the resin tank VI111 and then enter the oxidation reaction system 10 to reuse the bromide ions (namely hydrobromic acid).

Examples I-13

As shown in fig. 13, 34 and 35, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank II27, an electrodialysis device I117 for purifying monovalent ions, a neutralization tank 94, a crystallizer II49 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of a mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of a vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of a cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to a filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of a resin tank II27, the water outlet of the resin tank II27 is connected to the water inlet of a mixing tank V46, the water inlet of the mixing tank V46 is also provided with a medicine adding port 48, and the water outlet of the mixing tank V46 is connected to the inlet of a filter V47;

The liquid outlet of the filter V47 enters the water inlet 212 of the electrodialysis device I117 for purifying monovalent ions, the water outlet I118 of the electrodialysis device I117 for purifying monovalent ions is connected to the inlet of the neutralization tank 94, the neutralization tank 94 is also connected to the crystallizer II49 with the acid adding unit 97 and the base adding unit III140, the outlet of the neutralization tank 94 is connected to the crystallizer II49, and the water outlet II119 of the electrodialysis device I117 for purifying monovalent ions is connected to the dosing port 48 of the mixing tank V46.

The electrodialysis device I117 for purifying monovalent ions is connected in the same manner as the conventional electrodialysis device, except that the membrane type in the membrane stack is different from that of conventional electrodialysis, 10 repeated combinations of the combination of the monovalent anion permselective membrane 214 and the cation permselective membrane 213 are arranged in the electrode positive electrode 201 and the electrode negative electrode 202 in this embodiment, specifically, the monovalent anion permselective membrane 214 and the cation permselective membrane 213 form a water supply chamber 203, the cation permselective membrane 213 and the monovalent anion permselective membrane 214 form a concentration chamber 204 before, the electrode positive electrode 201 and the closest membrane form a polar water chamber 215, and the electrode negative electrode 202 and the closest membrane form a polar water chamber 215.

The outlet of the polar water tank 205 is connected to the inlet of the polar water pump 206, the outlet of the polar water pump 206 is connected to the inlet of the polar water chamber 215, and the outlet of the polar water chamber 215 is connected to the polar water tank 205 to form a cycle;

the outlet of the water feed tank 207 is connected to the inlet of the water feed pump 208, the outlet of the water feed pump 208 is connected to the inlet of the water feed chamber 203, and the outlet of the water feed chamber 203 is connected to the water feed tank 207 to form a circulation; the water supply tank 207 is internally provided with a partition board, and the water supply tank 207 is also provided with a water inlet 212 of electrodialysis equipment I117 for purifying monovalent ions and a water outlet II119 of the electrodialysis equipment I117 for purifying monovalent ions;

the outlet of the concentration tank 209 is connected to the inlet of the concentration pump 210, the outlet of the concentration pump 210 is connected to the inlet of the concentration chamber 204, and the outlet of the concentration chamber 204 is connected to the concentration tank 209 to form a cycle; a partition board is arranged in the concentration tank 209, and the concentration tank 209 is also provided with a pure water feed port 211 and a water outlet I118 of electrodialysis equipment I117 for purifying monovalent ions;

the recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the mixture is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a resin tank II27 for treatment and then enters a mixing tank V46 for adding chemicals, the filtrate is filtered by a filter V47 and then enters an electrodialysis device I117 for purifying monovalent ions, a water outlet I118 of the electrodialysis device I117 for purifying monovalent ions is neutralized by a neutralization tank 94 (the pH value is reduced to about 3 by an acid adding unit 97 firstly, carbonate is reacted, then sodium hydroxide is added by an alkali adding unit III140 for regulating the pH value to be neutral, and residual hydrobromic acid is reacted), and then the filtrate enters a crystallizer II49; the water outlet II119 of the electrodialysis device I117 for purifying monovalent ions enters the mixing tank V46 (namely chemicals added into the mixing tank V46).

The polar water is circulated by a polar water tank 205, a polar water pump 206 and a polar water chamber 215; the water supply is circulated by a water supply tank 207, a water supply pump 208 and a water supply chamber 203; simultaneously, the aqueous solution to be treated is fed from the water inlet 212 of the electrodialysis device I117 for purifying monovalent ions and overflows from the water outlet II119 of the electrodialysis device I117 for purifying monovalent ions;

the concentrated solution is circulated by a concentration tank 209, a concentration pump 210 and a concentration chamber 204; simultaneously, pure water is fed from a pure water feed port 211 (flow rate is controlled) and overflows from a water outlet I118 of electrodialysis equipment I117 for purifying monovalent ions;

ion migration mode between membranes: cations (sodium ions) migrate toward the electrode negative electrode through the cation permselective membrane 213 into the concentrating compartment 204; monovalent anions (bromide ions) migrate toward the electrode anode through the monovalent anion permselective membrane 214 into the concentrating compartment 204; divalent anions (carbonate) migration to the electrode anode cannot be intercepted by the monovalent anion permselective membrane 214, cannot enter the concentrating compartment 204, and remains in the feedwater compartment 203; therefore, the concentration chamber 204 is filled with an aqueous solution of sodium bromide and the water supply chamber 203 is filled with an aqueous solution mainly containing sodium carbonate;

the experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank II27 is filled with the resin with adsorption capacity to BA, the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated, the 8 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, and the hydrobromic acid is fed into the acid adding unit 97 of the neutralization tank 94 and the 10 percent sodium hydroxide is fed into the alkali adding unit III 140. Starting the polar water pump 206 to circulate, starting the water feed pump 208 to circulate, and starting the concentration pump 210 to circulate; the polar water tank 205 is added with 1mol/L sodium hydroxide, the water inlet 212 of the electrodialysis device I117 for purifying monovalent ions is added with the aqueous solution to be treated, the pure water feed port 211 of the concentration tank 209 is added with pure water, and the electrode plate supplies direct current of 48V.

Experimental results:

Liquid outlet ba=9 ppm, cobalt ion=0.1 ppm, manganese ion=0.4 ppm, sodium ion=10101 ppm, bromide ion=5223 ppm of filter V47.

And (3) discharging water from a neutralization tank 94: ph=7.0.

Water sample analysis of a water outlet II119 of electrodialysis device I117 for purifying monovalent ions: ph=9.4, carbonate=9987 ppm;

crystallizer II49 analyzed sodium bromide purity 98.2%.

Conclusion: the concentration of BA is reduced after being treated by a resin tank II27, the concentration of cobalt ions and manganese ions is reduced after being treated by a mixing tank V46 and a filter V47, and as cobalt and manganese ions are precipitated by adding carbonate, the carbonate in the filter V47 is treated by electrodialysis equipment I117 for purifying monovalent ions, a water outlet II119 of the electrodialysis equipment I117 for purifying monovalent ions is mainly carbonate, reflux is used for precipitating cobalt and manganese again, a water outlet I118 of the electrodialysis equipment I117 for purifying monovalent ions is mainly sodium bromide, residual carbonate is reacted again by a neutralization tank 94, free hydrobromic acid is neutralized by alkali, and sodium bromide solid is obtained by heating and evaporating in a crystallizer II 49.

Meanwhile, the treatment effect of electrodialysis equipment I117 for purifying monovalent ions is the same as that of nanofiltration unit I106, and monovalent bromide ions and divalent carbonate ions can be separated, so that the monovalent bromide ions and the divalent carbonate ions can be used alternatively as Hu Huang;

it is also theorized that the outlet I118 of electrodialysis device I117 for purifying monovalent ions is primarily sodium bromide, and that it is possible to treat the product with bipolar membrane devices, with halogen generating reactors, with electrolytic devices, with resin VI (after entering the oxidation reaction system), with resin VIII, etc., after the residual carbonate has been reacted again in neutralization tank 94 and the free hydrobromic acid has been neutralized with base.

Examples I to 14

As shown in fig. 14, a system for purifying and recycling a solid mixture mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuum-pumping cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank II27, an evaporation tank II120, a cooler III121, a filter IX122, a neutralization tank 94, a bipolar membrane device I28, and the like.

The connection mode is as follows:

The liquid outlet of the filter V47 is connected to the inlet of the evaporation tank II120, the water outlet of the evaporation tank II120 is connected to the inlet of the cooler III121, the water outlet of the cooler III121 is connected to the inlet of the filter IX122, the liquid outlet 123 of the filter IX122 is connected to the inlet of the neutralization tank 94, the neutralization tank 94 is also provided with an acid adding unit 97, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device I28, the bipolar membrane device I28 is also provided with an acid generating tank 29, an alkali generating tank 30, the solid outlet 124 of the filter IX122 is connected to the inlet of the dissolution tank 125, the dissolution tank 125 is also provided with a liquid adding port, and the outlet of the dissolution tank 125 is connected to the liquid adding port 48 of the mixing tank V46.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is filtered by a filter I5 after being cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105, the solid is collected, filtrate enters a resin tank II27 for treatment and then enters a mixing tank V46 for adding chemicals, the filtrate is filtered by a filter V47, the filtrate is evaporated and concentrated by an evaporation tank II120 and mainly precipitates the solid in a cooler III121, the filtrate is filtered by a filter IX122 (a centrifugal filter in the embodiment), the filtrate enters a neutralization tank 94, hydrobromic acid is also added into the neutralization tank 94, and the effluent of the neutralization tank 94 is connected to a bipolar membrane device I28 for treatment; the solids of filter IX122 are dissolved by dissolution tank 125 and enter mixing tank V46 (i.e., the chemicals added to mixing tank V46).

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, the resin tank II27 is filled with the resin with adsorption capacity to BA, the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated, the 8 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, the water outlet temperature of the cooler III121 is controlled to be 3 ℃, and the pure water is fed into the liquid feeding port of the dissolving tank 125.

Experimental results:

Liquid outlet ba=19 ppm, cobalt ion=0.3 ppm, manganese ion=0.8 ppm, sodium ion=15012 ppm, bromide ion=5996 ppm, carbonate radical=14431 ppm of filter V47.

Liquid outlet 123 water sample analysis of filter IX 122: 43134ppm bromide and 25410ppm carbonate;

And (3) discharging water from a neutralization tank 94: ph=3.0, bromide 65410ppm.

Dissolving tank 125 water sample analysis: ph=9.8, carbonate=18451 ppm;

the acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromide 9.76% and sodium 357ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.47% and bromide ion 294ppm.

Conclusion: the concentration of BA is reduced after the treatment of the resin tank II27, the concentration of cobalt ions and manganese ions is reduced after the treatment of the mixing tank V46 and the filter V47, and the carbonate is added to precipitate cobalt and manganese ions, so that the bromide ions and the carbonate in the filter V47 are evaporated, concentrated, cooled and centrifugally separated, and a large amount of sodium carbonate is separated out to form the solid of the filter IX122 due to the reduced solubility of sodium carbonate, the sodium bromide has higher solubility and becomes filtrate, and the filtrate is neutralized by the neutralization tank 94 to remove free carbonate and then is treated by bipolar membrane equipment.

Meanwhile, the effect of the evaporator II120 plus the cooler III121 plus is proved to be similar to the treatment effect of electrodialysis equipment I117 for purifying monovalent ions by the filter IX122 and the nanofiltration unit I106, and monovalent bromide ions and divalent carbonate ions can be separated, so that the monovalent bromide ions and the divalent carbonate ions can be alternatively used by Hu Huang; it is also theorized that the water outlet of filter IX122 is primarily sodium bromide, and that it is feasible to treat with bipolar membrane equipment, with halogen generating reactors, with electrolytic devices, with resin VI (which then enters the oxidation reaction system), with resin VIII, and the like, after re-reacting the residual carbonate via neutralization tank 94 and neutralizing the free hydrobromic acid with base.

Examples I-15

As shown in fig. 15, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuum-pumping cooler 104, a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank II27, an evaporation tank II120, a cooler III121, a filter IX122, a buffer tank 126, an alkali adding device II127, a nanofiltration unit II128, a neutralization tank 94, a bipolar membrane device I28, and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of a mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of a vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of a cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to a filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of a resin tank II27, the water outlet of the resin tank II27 is connected to the water inlet of a mixing tank V46, the water inlet of the mixing tank V46 is also provided with a medicine adding port 48, and the water outlet of the mixing tank V46 is connected to the inlet of a filter V47; the liquid outlet of the filter V47 is connected to the inlet of the evaporation tank II120, the water outlet of the evaporation tank II120 is connected to the inlet of the cooler III121, and the water outlet of the cooler III121 is connected to the inlet of the filter IX 122;

The liquid outlet 123 of the filter IX122 is connected to the inlet of the buffer tank 126, the outlet of the alkalizing device II127 is also connected to the inlet of the buffer tank 126, the outlet of the buffer tank 126 is connected to the water inlet of the high-pressure pump 216, the water outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit II128, the fresh water outlet 129 of the nanofiltration unit II128 is connected to the inlet of the neutralization tank 94, the neutralization tank 94 is also connected to the acid adding unit 97, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device I28, the bipolar membrane device I28 is also provided with the acid generating tank 29, the alkali generating tank 30, the solid outlet 124 of the filter IX122 is connected to the inlet of the dissolution tank 125, the dissolution tank 125 is also provided with a liquid adding port, and the outlet of the dissolution tank 125 is connected to the liquid adding port 48 of the mixing tank V46; the concentrate outlet 130 of the nanofiltration unit II128 is also connected to the dosing port 48 of the mixing tank V46.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a resin tank II27 for treatment and then enters a mixing tank V46 for adding chemicals, the filtrate is filtered by a filter V47 and then is subjected to evaporation concentration by an evaporation tank II120 and mainly precipitates the solid in a cooler III121, the filtrate is filtered by a filter IX122 (a centrifugal filter in the embodiment), the filtrate is subjected to ion separation by a buffer tank 126 (an alkali adding device II127 adds alkali to the buffer tank 126 for neutralizing bicarbonate to carbonate) and then enters a nanofiltration unit II128, the fresh water of the nanofiltration unit II128 enters a neutralization tank 94, hydrobromic acid is also added into the neutralization tank 94, and the effluent of the neutralization tank 94 is connected to a bipolar membrane device I28 for treatment; the solids of filter IX122 are dissolved by dissolution tank 125 and then enter mixing tank V46 (i.e., chemicals added to mixing tank V46); the concentrated water from the nanofiltration unit II128 enters the mixing tank V46 (i.e., the chemicals added to the mixing tank V46).

The experiment was run using the above processing system: the normal-temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, the resin tank II27 is filled with the resin with adsorption capacity to BA, the resin tank II27 is regenerated by 5 percent sodium hydroxide after being saturated, the 8 percent sodium carbonate aqueous solution is fed into the mixing tank V46 at the initial stage, the water outlet temperature of the cooler III121 is controlled to be 3 ℃, and the pure water is fed into the liquid feeding port of the dissolving tank 125; the alkalizer II127 was fed with 8% sodium carbonate aqueous solution.

Experimental results:

Liquid outlet ba=21 ppm, cobalt ion=0.4 ppm, manganese ion=0.1 ppm, sodium ion= 14919ppm, bromide ion=5567 ppm, carbonate radical=12981 ppm of filter V47.

Dissolving tank 125 water sample analysis: ph=9.8, carbonate=18451 ppm;

fresh water outlet 129 water sample analysis of nanofiltration unit II 128: 48145ppm bromide and 9814ppm carbonate;

and (3) discharging water from a neutralization tank 94: ph=3.0, bromide 68133ppm.

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.44% and sodium ion 96ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.44%, bromide ion 287ppm.

Conclusion: the concentration of BA is reduced after being treated by a resin tank II27, the concentration of cobalt ions and manganese ions is reduced after being treated by a mixing tank V46 and a filter V47, and the cobalt ions and the manganese ions are precipitated by adding carbonate, so that the bromine ions and the carbonate in the filter V47 are evaporated and concentrated, cooled and centrifugally separated, a large amount of sodium carbonate is separated out to form a solid of a filter IX122 due to the reduced solubility of sodium carbonate, the sodium bromide is higher in solubility to form a filtrate, but the filtrate still contains carbonate, a small amount of bicarbonate residues in the filtrate are converted into carbonate by an alkali adding unit II127, the bromide (monovalent) and the carbonate (divalent) are separated by a nanofiltration unit II128, the carbonate content of the obtained fresh water of the nanofiltration unit II128 is lower, and the fresh water of the nanofiltration unit II128 is treated by bipolar membrane equipment after the free carbonate is neutralized by a neutralization tank 94.

Examples I-16

As shown in fig. 16, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuum-pumping cooler 104 and a cooling heat exchanger 105), a filter I5, a resin tank I18, a nanofiltration unit V131, a bipolar membrane device one 134, an oxidation reaction system 10 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of a mixing tank I3, the mixing tank I3 also has a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of a vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of a cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to a filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of a resin tank I18, the discharge outlet of the resin tank I18 is connected to the water inlet of a high-pressure pump 216, the water outlet of the high-pressure pump 216 is connected to the water inlet of a nanofiltration unit V131, and the concentrated water outlet 133 of the nanofiltration unit V131 is connected to the oxidation reaction system 10; the fresh water outlet 132 of the nanofiltration unit V131 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the bipolar membrane device one 134, and the bipolar membrane device one 134 is also provided with an acid production tank 135 and an alkali production tank 136.

The above processing system operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is filtered by a filter I5 after being cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105, the solid is collected, filtrate enters a resin tank I18 for treatment, a discharge port of the resin tank I18 is treated by a nanofiltration unit V131, concentrated water enters an oxidation reaction system 10, and the fresh water is concentrated by a reverse osmosis concentration device 305 and then is treated by a bipolar membrane device I134.

The experiment was run using the above processing system: the liquid inlet 4 of the mixing tank I3 is fed with normal-temperature pure water, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, the resin tank I18 is filled with resin with adsorption capacity to BA, and the resin tank I18 is regenerated by 5 percent sodium hydroxide after being saturated.

Experimental results:

The drain water sample of resin tank I18 (filled with a resin having adsorption to BA) was analyzed as follows: ba=36 ppm, cobalt ion=4510 ppm, manganese ion=2901 ppm, sodium ion=1268 ppm, bromide ion=6800 ppm.

Fresh water outlet 132 of nanofiltration unit V131 is water sample: 7013ppm bromide ion, 1998ppm sodium ion;

the acid generator 135 of the bipolar membrane device one 134 controls hydrogen ions 1.0mol/L, and detects: bromide ion 8.1% and sodium ion 146ppm;

the caustic soda tank 136 of the bipolar membrane apparatus one 134 controls 1.2mol/L hydroxide, detection: sodium ion 2.77%, bromide ion 95ppm;

concentrated water outlet 133 of nanofiltration unit V131 was water sample: cobalt ion=1.35%, manganese ion=0.86%, sodium ion=897 ppm, bromide ion=4732 ppm. Fresh water of nanofiltration unit V131: concentrated water ≡3:1 water amount.

Conclusion: the water sample BA at the discharge port of the resin tank I18 is reduced in proportion, and after being treated by the nanofiltration unit V131, the total sodium content in the fresh water of the nanofiltration unit V131 is reduced, so that sodium ions brought back to the oxidation reaction system 10 are not much.

Meanwhile, hydrobromic acid is obtained by treating the fresh water outlet of the nanofiltration unit V131 by using the bipolar membrane equipment I134, and it can be deduced that the fresh water outlet of the nanofiltration unit V131 can be treated by using a crystallizer I, a halogen generation reactor, an electrolysis device, a resin VIII or a resin VI.

Examples I to 17

As shown in fig. 17, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a nanofiltration unit I106, a combustion device II137, a mixing tank XII138, a neutralization tank 94, a bipolar membrane device I28, an evaporation concentration device 139 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of a mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of a vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of a cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to a filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of a mixing tank V46, the water inlet of the mixing tank V46 is also provided with a dosing port 48, and the water outlet of the mixing tank V46 is connected to the inlet of a filter V47;

the liquid outlet of the filter V47 is connected to the inlet of the evaporation concentration device 139, the concentrated liquid outlet of the evaporation concentration device 139 is connected to the combustion device II137, the solid outlet of the combustion device II137 is connected to the mixing tank XII138, the mixing tank XII138 is also provided with a liquid filling port, the water outlet of the mixing tank XII138 is connected to the water inlet of the high-pressure pump 216, the water outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit I106, the fresh water outlet 107 of the nanofiltration unit I106 is connected to the water inlet of the neutralization tank 94, the neutralization tank 94 is also provided with an acid adding unit 97, the water outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device I28, and the bipolar membrane device I28 is also provided with an acid production tank 29 and an alkali production tank 30; the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46, and one of the outlets of the acid production tank 29 of the bipolar membrane device I28 is connected to the acid addition unit 97.

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, the pure water is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, filtrate enters a mixing tank V46 to be added with chemicals, after the filtrate is filtered by a filter V47, the filtrate is concentrated by an evaporation concentration device 139 and then enters a combustion device II137 to be burnt, the solid obtained by burning enters a mixing tank XII138 to be dissolved by adding water, and then enters a nanofiltration unit I106 to be treated, and fresh water of the nanofiltration unit I106 enters a bipolar membrane device I28 to be treated after the participating carbonate is reacted by adding acid in a neutralization tank 94; the concentrate of nanofiltration unit I106 enters mixing tank V46 (i.e., the chemicals added by mixing tank V46), and the acid generator tank 29 of bipolar membrane apparatus I28 provides hydrobromic acid to the acid adding unit 97.

The experiment was run using the above processing system: pure water at normal temperature is fed into a liquid inlet 4 of a mixing tank I3, a vacuumizing cooler 104 is vacuumized to 90%, a cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be about 25 ℃, a combustion device II137 is controlled to burn at 800-1200 ℃, pure water is fed into a liquid feeding port of a mixing tank XII138, 8% sodium carbonate aqueous solution is fed into a mixing tank V46 at the initial stage, and hydrobromic acid is fed into an acid adding unit 97.

Experimental results:

The water sample analysis of the liquid outlet of filter V47 was as follows: ba= 10176ppm, cobalt ion=0.1 ppm, manganese ion=0.9 ppm, sodium ion=7991 ppm, bromide ion=5004 ppm.

The outlet of mixing tank X11138 was analyzed as follows: ba=0 ppm, sodium ion=1.6%, bromide ion=1%, carbonate 1.7%.

Concentrated water outlet 108 water sample analysis of nanofiltration unit I106: ph=9.7, carbonate=2.3%;

sampling the water outlet of the neutralization tank 94: ph=2.9, bromide=1.8%

The acid production tank 29 of the bipolar membrane device I28 controls 1.2mol/L of hydrogen ions, and detection is carried out: bromine ion 9.44%, sodium ion 235ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.5mol/L hydroxyl, and detection is carried out: sodium ion 3.53%, bromide ion 511ppm.

Conclusion: the concentration of cobalt ions and manganese ions is reduced after the treatment of a mixing tank V46 and a filter V47, all organic matters and acid radicals thereof are combusted after the treatment of a combustion device II137, a mixed solution of sodium carbonate and sodium bromide is obtained, after the treatment of a nanofiltration unit I106, concentrated water mainly contains sodium carbonate and is used for depositing cobalt and manganese ions of the mixing tank V46, and after the neutralization of residual carbonate radicals of fresh water by a neutralization tank 94, the treatment of the fresh water by a bipolar membrane device I28 can generate aqueous solution of hydrobromic acid and sodium hydroxide.

Meanwhile, it can be deduced that the sodium bromide solid can be obtained by using the crystallizer II49 after passing through the neutralization tank 94 (matched with the acid adding unit 97 and the alkali adding unit III 140) after passing through the fresh water outlet 107 of the nanofiltration unit I106; it may be inferred that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the halogen generation reactor 38 and its auxiliary systems to obtain hydrobromic acid, that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the electrolysis apparatus 109 and its auxiliary apparatuses, that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the resin VIII110 (the regenerated liquid thereof is treated by the bipolar membrane apparatus III112 to obtain hydrobromic acid and aqueous sodium hydroxide solution), that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the resin VI111 (and then enter the oxidation reaction system 10), and the like.

Examples I-18

As shown in fig. 18, a system for purifying and recycling a solid mixture mainly comprises a crystallizer I1, an esterification reactor 52, a wash tank I53, a resin tank X71, a mixing tank V46, a filter V47, a nanofiltration unit I106, a neutralization tank 94, a bipolar membrane apparatus I28, and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the feed inlet I54 of the esterification reactor 52, the esterification reactor 52 is also provided with a feed inlet II55, a steam outlet 56 and a heater 58, the discharge outlet of the esterification reactor 52 is connected to the inlet of a cooler, the outlet of the cooler is connected to the inlet of a washing tank I53, the washing tank I53 is also provided with a washing liquid inlet 59 and a product ester outlet 57, the washing liquid outlet 60 of the washing tank I53 is connected to the water inlet of a resin tank X71, the water outlet of the resin tank X71 is connected to the water inlet of a mixing tank V46, the water outlet of the mixing tank V46 is connected to the water inlet of a filter V47, the liquid outlet of the filter V47 is connected to the water inlet of a high-pressure pump 216, the water outlet of the high-pressure pump 216 is connected to the water inlet of a nanofiltration unit I106, the fresh water outlet 107 of the nanofiltration unit I106 is connected to the water inlet of a neutralization tank 94, the acid adding device 97 is also connected to the inlet of the neutralization tank 94, the water outlet of the neutralization tank 94 is connected to the water inlet of a bipolar membrane device I28, and the bipolar membrane device I28 is provided with an acid-producing tank 29 and an alkali-producing tank 30; the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46, and one of the outlets of the acid production tank 29 of the bipolar membrane device I28 is connected to the acid addition unit 97.

The above processing system operates as follows:

the solids in the crystallizer I1 enter the esterification reactor 52 through a feed port I54 of the esterification reactor 52, and alcohols (ethanol is taken as an example in this embodiment) and catalyst hydrobromic acid are fed into the esterification reactor 52 from a feed port II55 of the esterification reactor 52, while heating is performed for 2 hours by a heater 58 (produced water vapor is discharged through a water vapor outlet 56 of the esterification reactor 52 and condensed by a condenser 61 and discharged), after which the mixture of the esterification reactor 52 is cooled and then transferred to a wash tank I53, wash liquid (water is taken as an example in this embodiment) is fed into the wash tank I53 from a wash liquid inlet 59 of the wash tank I53, while standing and layering are performed in the wash tank I53, and after that the wash liquid is discharged from a wash liquid outlet 60 of the wash tank I53;

the washing liquid discharged from the washing liquid outlet 60 enters the mixing tank V46 after passing through the resin tank X71, sodium carbonate aqueous solution is added from the dosing port 48 of the mixing tank V46, the solution of the mixing tank V46 is filtered by the filter V47, the filtrate enters the nanofiltration unit I106 for treatment, the fresh water of the nanofiltration unit I106 enters the neutralization tank 94, the hydrobromic acid is added to the neutralization tank 94 by the acid adding device 97 for reaction to remove carbonate, and the effluent water of the neutralization tank 94 enters the bipolar membrane device I28 for treatment; the concentrate of nanofiltration unit I106 enters mixing tank V46 (i.e., the chemicals added by mixing tank V46), and the acid generator tank 29 of bipolar membrane apparatus I28 provides hydrobromic acid to the acid adding unit 97.

The experiment was run using the above processing system: the washing liquid inlet 59 feeds pure water to the washing tank I53, the dosing port 48 of the mixing tank V46 feeds an 8% aqueous sodium carbonate solution, the resin tank X71 feeds a resin having an adsorption effect on COD, and the resin is regenerated with 8% sodium hydroxide after saturation of adsorption.

Experimental results:

the wash solution discharged from the wash solution outlet 60 is analyzed as follows: ba=945 ppm, cobalt ion=3316 ppm, manganese ion=2201 ppm, sodium ion=955 ppm, bromide ion=5005 ppm.

Product ester outlet 57 was analyzed, principally ethyl benzoate.

The resin pot X71 outlet analysis is as follows: ba=4 ppm, cobalt ion=3355 ppm, manganese ion=2223 ppm, sodium ion=921 ppm, bromide ion=5047 ppm.

Filter V47 filtrate was analyzed as follows: ba=8 ppm, cobalt ion=0.2 ppm, manganese ion=0.3 ppm, sodium ion=7003 ppm, bromide ion=4286 ppm.

Concentrated water outlet 108 water sample analysis of nanofiltration unit I106: ph=9.4, carbonate=1.5%;

sampling the water outlet of the neutralization tank 94: ph=3.3, bromide=0.9%

The acid production tank 29 of the bipolar membrane device I28 controls hydrogen ions to be 1.0mol/L, and detection is carried out: bromide ion 8.11%, sodium ion 44ppm;

the caustic soda tank 30 of the bipolar membrane device I28 controls 1.0mol/L hydroxyl, and detection is carried out: sodium ion 2.28%, bromide ion 79ppm.

Conclusion: the BA is converted into esters after passing through the esterification reactor 52, so the concentration of the BA in the washing liquid discharged from the washing liquid outlet 60 is lower, the BA is removed from the washing liquid obtained after washing with water after passing through the resin tank X71, the concentration of cobalt ions and manganese ions is reduced after passing through the mixing tank V46 and the filter V47, after passing through the nanofiltration unit I106, the concentrated water mainly contains sodium carbonate for precipitating cobalt and manganese ions of the mixing tank V46, and after the residual carbonate is neutralized by the fresh water through the neutralization tank 94, the aqueous solution of hydrobromic acid and sodium hydroxide can be produced after being treated by the bipolar membrane equipment I28. Meanwhile, it can be deduced that the sodium bromide solid can be obtained by using the crystallizer II49 after passing through the neutralization tank 94 (matched with the acid adding unit 97 and the alkali adding unit III 140) after passing through the fresh water outlet 107 of the nanofiltration unit I106; it may be inferred that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the halogen generation reactor 38 and its auxiliary systems to obtain hydrobromic acid, that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the electrolysis apparatus 109 and its auxiliary apparatuses, that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the resin VIII110 (the regenerated liquid thereof is treated by the bipolar membrane apparatus III112 to obtain hydrobromic acid and aqueous sodium hydroxide solution), that the fresh water outlet 107 of the nanofiltration unit I106 may be treated by the resin VI111 (and then enter the oxidation reaction system 10), and the like.

Examples I to 19

As shown in fig. 19, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104 and a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a resin tank III41, a nanofiltration unit I106, a volatile acid generator 332 and the like.

The connection mode is as follows:

The fresh water outlet 107 of the nanofiltration unit I106 is connected to the water inlet of the reverse osmosis concentration device 305, the concentrate outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the volatile acid generator 332 (the fresh water outlet 307 of the reverse osmosis concentration device 305 discharges), the volatile acid generator 332 is further provided with an acid inlet pipe 333, the volatile acid generator 332 is further provided with a liquid drain 336, a heater 334, the gas outlet 335 of the volatile acid generator 332 is connected to the condenser 43, the outlet of the condenser 43 is connected to the acid production tank 45, and the concentrate outlet 108 of the nanofiltration unit I106 is connected to the dosing port 48 of the mixing tank V46.

The recovery process described above operates as follows:

fresh water of the nanofiltration unit I106 is concentrated by the reverse osmosis concentration device 305 and then enters the volatile acid generator 332, phosphoric acid is fed into the acid adding pipeline 333 of the volatile acid generator 332, and the fresh water is heated, hydrobromic acid is blown out, condensed by the condenser 43 and then collected in the acid production tank 45; the concentrated water of the nanofiltration unit I106 enters the mixing tank V46 (namely the chemicals added by the mixing tank V46).

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuumizing cooler 104 is vacuumized to 90 percent, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, the resin tank III41 is filled with the resin with adsorption capacity to BA, the resin tank III41 is regenerated by 5 percent sodium hydroxide after being saturated, the phosphoric acid solution is fed into the acid inlet pipeline 333 of the volatile acid generator 332, and the 8 percent sodium carbonate aqueous solution is fed into the initial stage of the mixing tank V46.

Experimental results:

The acid generator tank 45 analyzes the sodium bromide for a purity of 12.1%.

Conclusion: the concentration of BA is reduced after being treated by the resin tank III41, and then the concentration of cobalt ions and manganese ions is reduced after being treated by the mixing tank V46 and the filter V47, and as the cobalt and manganese ions are precipitated by adding carbonate, the carbonate in the filter V47 is treated by the nanofiltration unit I106, the carbonate is intercepted on the concentrated water side of nanofiltration, the reflux is used for precipitating cobalt and manganese again, the fresh water of the nanofiltration unit I106 is mainly sodium bromide, and enters the volatile acid generator 332 and an accessory device thereof, and hydrobromic acid is obtained in the acid generating tank 45 of the volatile acid generator 332.

At the same time, the inference can be made: the volatile acid generator 332 can be used for the treatment in the final step of this embodiment as in the bipolar membrane device I28, the crystallizer II49, the halogen generating reactor 38 and its accessories, the electrolysis device 109 and its accessories, the resin tank VIII110, the resin tank VI111, and the oxidation reaction system 10, and can be used interchangeably.

Examples I to 20

As shown in fig. 20, the solid mixture purification and reuse system mainly comprises a crystallizer I1, a mixing tank I3, a cooling device I (the cooling device I comprises a vacuumizing cooler 104, a cooling heat exchanger 105), a filter I5, a mixing tank V46, a filter V47, a biochemical treatment device II337, a nanofiltration device I106, an evaporation tank one 338, a cooling device one 339, a filter one 340, a crystallizer II49, a resin tank VII343 and the like.

The connection mode is as follows:

the solid outlet 2 of the crystallizer I1 is connected to the inlet of the mixing tank I3, the mixing tank I3 is also provided with a liquid inlet 4, the outlet of the mixing tank I3 is connected to the inlet of the vacuumizing cooler 104, negative pressure is pumped above the vacuumizing cooler 104, the outlet of the vacuumizing cooler 104 is connected to the inlet of the cooling heat exchanger 105, the outlet of the cooling heat exchanger 105 is connected to the filter I5, the filter I5 is provided with a solid outlet 6 and a liquid outlet 7, the liquid outlet 7 of the filter I5 is connected to the water inlet of the mixing tank V46, the mixing tank V46 is also provided with a dosing port 48, the water outlet of the mixing tank V46 is connected to the water inlet of the filter V47, the liquid outlet of the filter V47 is connected to the water inlet of the biochemical treatment device II337 (the biochemical treatment device II337 comprises an anaerobic device and an oxygen consumption device) (the biochemical treatment device II337 also has other sewage inlet), the water outlet of the biochemical treatment device II337 is connected to the water inlet of the reverse osmosis concentration device 305, the fresh water outlet 307 of the reverse osmosis concentration device 305 is discharged, the concentrated solution outlet 306 of the reverse osmosis concentration device 305 is connected to the water inlet of the buffer tank 126, the outlet of the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the water inlet of the resin tank VII343, the water outlet of the resin tank VII343 is connected to the water inlet of the nanofiltration device I106, the fresh water outlet 107 of the nanofiltration device I106 is connected to the water inlet of the evaporation tank I338, the water outlet of the evaporation tank I338 is connected to the water inlet of the cooling device I339, the water outlet of the cooling device I339 is connected to the water inlet of the filter I340, and the liquid outlet 341 of the filter I340 is connected to the water inlet of the crystallizer II 49; the concentrated water outlet 108 of the nanofiltration device I106 is connected to the dosing port 48 of the mixing tank V46;

The recovery process described above operates as follows:

the solid in the crystallizer I1 enters a mixing tank I3, pure water is fed from a liquid inlet 4 of the mixing tank I3, then the pure water is cooled by a vacuumizing cooler 104 and a cooling heat exchanger 105 and then filtered by a filter I5, the solid is collected, the filtrate enters the mixing tank V46, alkaline substances (sodium carbonate) are added to form insoluble substances of cobalt and manganese ions, the insoluble substances are filtered by a filter V47, the filtrate of the filter V47 enters a biochemical treatment device II337 for treatment (other sewage enters the biochemical treatment device II 337), the biochemical treatment device II337 is concentrated by a reverse osmosis concentration device 305, sodium hydroxide is added by an alkali adding device I77 in a buffer tank 126 after the biochemical treatment device II is concentrated, the hardness of the carbonate is removed by a resin tank VII (calcium and magnesium ions are adsorbed), the concentrated water of the nanofiltration device I106 is mainly sodium carbonate, the concentrated water recycled to the mixing tank V46 is reused (as alkaline substances), the fresh water of the nanofiltration device I106 is concentrated by an evaporation tank I338 and then cooled by a cooling device I, and the solid sodium chloride with low crystal content of sodium chloride of 340 is filtered by a filter I340, and the solid sodium bromide of a relatively low crystal is precipitated by a sodium bromide product II is filtered by a filter I340.

The experiment was run using the above processing system: the normal temperature pure water is fed into the liquid inlet 4 of the mixing tank I3, the vacuum degree is pumped by the vacuumizing cooler 104 to 90%, the cooling heat exchanger 105 is cooled by chilled water, the water outlet of the cooling heat exchanger 105 is controlled to be 25 ℃, 10% sodium carbonate is fed into the mixing tank V46, the biochemical treatment device II337 comprises an anaerobic device and an oxygen consumption device, the anaerobic device is firstly passed through the oxygen consumption device, the reverse osmosis concentration device 305 is fed with the inlet pressure of 4MPa, the concentration multiple is controlled to be 6-8 times, the PH=11.3-11.7 is controlled by the mixing tank 126, the resin tank VII343 is filled with resin with adsorption effect on hardness (calcium magnesium ions), the resin is regenerated by sodium chloride after adsorption saturation and washed off chloride ions and is reused, the inlet pressure of 4MPa is fed into the nanofiltration device I106, the concentration multiple is controlled to be 5 times, the evaporation tank I338 is heated to the boiling point, and the water outlet temperature is controlled to be 10 ℃ by the cooling device I.

In the present utility model, the electrodialysis apparatus used in all examples was EX-4S-ED available from Hangzhou blue technology Co., ltd; the bipolar membrane device is EX-4S provided by Hangzhou blue technology Co., ltd; the nanofiltration membrane used in the nanofiltration unit is Film of DuPont company ^TM Fortilife ^TM XC-N; the resin (resin tank I, II, III, X, X1) with adsorption effect on COD is XDA-1G of the brand of Siam blue; the resin with adsorption effect on cobalt and manganese ions (namely the resin in the resin tanks IV and V) is LSC-500 of the brand of Siam blue; the resin having adsorption effect on hardness (i.e. the resin in resin tank VII) is LSC-510 of the West Ann blue brand; the resin with adsorption effect on bromide ion (namely the resin in the resin tank VIII) is 201 x 7MB of the east brand anion resin; the resin with adsorption to sodium ions (i.e. the resin in resin tank VI) was east brand cationic resin 001 x 7mb; the electrodialysis device for purifying monovalent ions is based on EX-4S-ED provided by Hangzhou blue technology Co., ltd, and the anion selective permeation membrane is replaced by a SELEMIONASV membrane provided by monovalent anion selective permeation membrane AGC engineering Co.

Example II-1

As shown in fig. 21, the system for purifying and recycling the aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a neutralization tank 94, a bipolar membrane device II308, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97 is also connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device II308, and one of the outlets of the acid producing tank 309 of the bipolar membrane device II308 is connected to the acid adding unit 97.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water of the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305, then the pH is regulated by the neutralization tank 94, and then the concentrated fresh water enters the bipolar membrane equipment II308 for treatment, and one of outlets of an acid production tank 309 of the bipolar membrane equipment II308 provides hydrobromic acid for the acid adding unit 97.

The experiment was run using the above processing system: the alkalizing device I77 is fed with 32% sodium hydroxide aqueous solution, and automatically monitors and controls the PH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given with the pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, neutralization tank 94 is controlled to have a pH of about 3.5 and acid addition unit 97 initially feeds 47.5% of industrial hydrobromic acid.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

1007ppm carbonate, 6587ppm bicarbonate, 1225ppm bromide, 3899ppm sodium ions, ph=8.89

Buffer tank 126 water: no bicarbonate was detected, carbonate=7533 ppm, hydroxide=66 ppm, bromide=1198 ppm.

The concentrate outlet 304 of the nanofiltration unit III302 is analyzed as follows: carbonate= 34321ppm, hydroxide=301 ppm, bromide=612 ppm:

the feed line of mixing tank V46 was analyzed as follows: ta=12187 ppm, ba=8999 ppm, cobalt ion=3112 ppm, manganese ion=2325 ppm.

The liquid outlet of filter V47 was analyzed as follows: cobalt ion=0.3 ppm, manganese ion=0.2 ppm.

The fresh water outlet 303 of the nanofiltration unit III302 is analyzed as follows: carbonate=215 ppm, hydroxide=17 ppm, bromide=1323 ppm.

The neutralization tank 94 discharges water as follows: carbonate, bicarbonate and hydroxide were undetectable, and bromide was 8325ppm.

Acid production tank 309 of bipolar membrane apparatus II308 controls hydrogen ion 1.4mol/L, detection: 11.3% of bromide ion, 114ppm of sodium ion:

the caustic soda pot 310 of the bipolar membrane apparatus II308 controls 1.9mol/L hydroxyl, detection: sodium ion 4.35%, bromide ion 87ppm.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of nanofiltration unit III302 is mainly sodium bromide. Residual carbonate and bicarbonate are then removed by the neutralization tank 94 and processed by the bipolar membrane device II308 to obtain an aqueous solution of sodium hydroxide and hydrobromic acid.

Example II-2

As shown in fig. 22, the system for purifying and recycling the aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a neutralization tank 94, a crystallizer II49, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97, the alkali adding device III140 are also connected to the neutralization tank 94, and the outlet of the neutralization tank 94 is connected to the water inlet of the crystallizer II 49.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water from the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305, then the pH is regulated by the neutralization tank 94 (acid is added to remove carbonate and bicarbonate, then alkali is added to neutralize free hydrobromic acid into sodium bromide), and then the sodium bromide is treated by the crystallizer II 49.

The experiment was run using the above processing system: the alkalizing device I77 is fed with 32% sodium hydroxide aqueous solution, and automatically monitors and controls the PH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given with the pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, neutralization tank 94 acid addition process control pH is approximately 3.5, followed by base addition process control pH is approximately 7, acid addition unit 97 feeds 47.5% industrial hydrobromic acid, and base addition unit III140 feeds 32% sodium hydroxide.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

Crystallizer II49 analyzed sodium bromide=98.6%.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of nanofiltration unit III302 is mainly sodium bromide. The residual carbonate and bicarbonate are then removed by neutralization tank 94 and the free hydrobromic acid is removed again before being processed in crystallizer II49 to yield sodium bromide solids.

It has also been demonstrated that the outlet of the neutralization tank 94 can be treated with bipolar membrane apparatus II308, or alternatively with crystallizer II 49.

Example II-3

As shown in fig. 23, a system for purifying and reutilizing an aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from a previous stage nanofiltration is used as feed water for a next stage nanofiltration, and the fresh water is treated for a plurality of times, and each treatment is aimed at more thoroughly intercepting carbonate groups), a neutralization tank 94, a halogen generation reactor 38, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47, and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97 is connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the halogen generating reactor 38, the halogen generating reactor 38 is further provided with a dosing port 40, the halogen generating reactor 38 is further provided with a water outlet 103, the gas outlet of the halogen generating reactor 38 is connected to the absorption tank 39, the absorption tank 39 is further provided with a dosing port 44, the outlet of the absorption tank 39 is connected to the inlet of the evaporation tank III42, the top gas phase of the evaporation tank III42 is provided with a condenser 43, the outlet of the condenser 43 is connected to the acid generating tank 45, and one of the outlets of the acid generating tank 45 is connected to the acid adding unit 97.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water of the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305 and then is subjected to PH regulation by the neutralization tank 94, and then enters the halogen generation reactor 38, the chlorine and sulfuric acid and pressurized air are fed into the dosing port 40 of the halogen generation reactor 38, the elemental bromine is blown out, the elemental bromine gas is absorbed by the absorption tank 39, sulfur dioxide and water are fed into the absorption tank 39 from the dosing port 44, the aqueous solution in the absorption tank 39 is evaporated by the evaporation tank II142 and then is condensed by the condenser 43 and then is collected into the acid production tank 45, and one of the outlets of the acid production tank 45 provides hydrobromic acid for the acid addition unit 97.

The experiment was run using the above processing system: the alkalizing unit I77 is fed with 32% aqueous sodium hydroxide solution, and automatically monitors and controls the pH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given a pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, neutralization tank 94 acid addition process control PH is approximately 3.5, acid addition unit 97 feeds 47.5% industrial hydrobromic acid, feed port 40 of halogen generation reactor 38 feeds chlorine, sulfuric acid, air, feed port 44 of absorber tank 39 feeds sulfur dioxide, water.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The concentrate outlet 304 of the nanofiltration unit III302 is analyzed as follows: carbonate= 34321ppm, hydroxide=301 ppm, bromide=612 ppm;

The acid generator tank 45 of the halogen generating reactor 38 is analyzed as follows: hydrogen ion 2.5mol/L, bromide=20.8%.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of nanofiltration unit III302 is mainly sodium bromide, and then undergoes neutralization tank 94 to remove residual carbonate and bicarbonate, and enters halogen generation reactor 38 and its auxiliary system for treatment to obtain hydrobromic acid aqueous solution.

It has also been demonstrated that the outlet of the neutralization tank 94 can be treated with bipolar membrane apparatus II308, with crystallizer II49, or with the halogen generating reactor 38 and its auxiliary systems, alternatively.

Example II-4

As shown in fig. 24, the system for purifying and recycling an aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for a plurality of times, and each treatment is aimed at more thoroughly intercepting carbonate radicals), a neutralization tank 94, an electrolysis device 109, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97 is also connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the electrolysis device 109, the electrolysis device 109 is further provided with an anode 329, a cathode 330 and an air inlet 331, the electrolysis device 109 is further provided with a water outlet 328, the air outlet of the electrolysis device 109 is connected to the absorption tank 39, the absorption tank 39 is further provided with a chemical adding port 44, the outlet of the absorption tank 39 is connected to the inlet of the evaporation tank III42, the gas phase at the top of the evaporation tank III42 is provided with a condenser 43, the outlet of the condenser 43 is connected to the acid producing tank 45, and one of the outlets of the acid producing tank 45 is connected to the acid adding unit 97.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water of the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305 and then is subjected to PH regulation by the neutralization tank 94, and then enters the electrolysis device 109, the air inlet 331 of the electrolysis device 109 is fed with air under pressure, elemental bromine is blown out, the elemental bromine gas is absorbed by the absorption tank 39, sulfur dioxide and water are fed into the absorption tank 39 from the dosing port 44, the aqueous solution in the absorption tank 39 is evaporated by the evaporation tank III42 and then is condensed by the condenser 43 and then is collected in the acid production tank 45, and one of the outlets of the acid production tank 45 provides hydrobromic acid for the acid dosing unit 97; the anode 329 and cathode 330 of the electrolyzer 109 are given a voltage of 36V.

The experiment was run using the above processing system: the alkalizing device I77 is fed with 32% sodium hydroxide aqueous solution, and automatically monitors and controls the PH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given with the pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, neutralization tank 94 acid addition process control PH is approximately 3.5, acid addition unit 97 feeds 47.5% industrial hydrobromic acid, air inlet 331 of electrolyzer 109 feeds air, dosing port 44 of absorber tank 39 feeds sulfur dioxide, water, and neutralization tank 94 acid addition unit 97 feeds hydrobromic acid.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The acid generator tank 45 of the electrode device 109 is analyzed as follows: hydrogen ion 2.7mol/L and bromine ion 21.5%.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of nanofiltration unit III302 is mainly sodium bromide, and then the residual carbonate and bicarbonate are removed by a neutralization tank 94, and the residual carbonate and bicarbonate enter an electrolysis device 109 and an auxiliary system thereof for treatment, so that hydrobromic acid aqueous solution can be obtained.

It has also been demonstrated that the outlet of the neutralization tank 94 can be treated with bipolar membrane apparatus II308, with crystallizer II49, with halogen generating reactor 38 and its auxiliary systems, or with electrolyzer 109 and its auxiliary systems, alternatively.

Example II-5

As shown in fig. 25, the system for purifying and recycling an aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47, a resin tank VI111, an oxidation reaction system 10 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the inlet connected to the resin tank VI111, and the outlet of the resin tank VI111 is connected to the oxidation reaction system 10.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water of the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305, and then enters the oxidation reaction system 10 after sodium ions are adsorbed by the resin tank VI 111.

The experiment was run using the above processing system: the alkalizing device I77 is fed with 32% sodium hydroxide aqueous solution, and automatically monitors and controls the PH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given with the pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, the resin tank VI111 is charged with a cationic resin, and after adsorption saturation, the resin tank VI111 is regenerated with 5% hydrochloric acid, and then the chloride ions are washed with water and reused.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The resin tank VI111 effluent was analyzed as follows: hydrogen ion 0.18mol/L, bromine ion 1.4%, sodium ion 11ppm.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of the nanofiltration unit III302 is mainly sodium bromide, and then sodium ions are replaced by hydrogen ions after being treated by a resin tank VI111, so that hydrobromic acid aqueous solution is obtained.

It has also been demonstrated that the fresh water of the nanofiltration unit III302 can be treated with the bipolar membrane apparatus II308, with the crystallizer II49, with the halogen generating reactor 38 and its auxiliary systems, with the electrolysis device 109 and its auxiliary systems, or with the resin tank VI111, optionally.

Example II A6

As shown in fig. 26, the system for purifying and recycling an aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a mixing tank V46, a filter V47, a resin tank VIII110, a bipolar membrane apparatus III112, and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the inlet of the resin tank VIII110, the outlet of the resin tank VIII110 discharging; the resin tank VIII110 is provided with a regeneration liquid inlet 113, a regeneration liquid outlet 114 of the resin tank VIII110 is connected to a water inlet of the bipolar membrane device III112, and the bipolar membrane device III112 is provided with an acid production tank 115 and an alkali production tank 116.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); fresh water of the nanofiltration unit III302 is discharged after passing through the resin tank VIII 110; the regeneration liquid of the resin tank VIII110 is treated with the bipolar membrane apparatus III 112.

The experiment was run using the above processing system: the alkalizing device I77 is fed with 32% sodium hydroxide aqueous solution, and automatically monitors and controls the PH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given with the pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, the resin tank VIII110 is filled with a resin having an adsorption effect on bromide ions, and the regeneration liquid inlet 113 of the resin tank VIII110 is fed with an 8% aqueous sodium hydroxide solution.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The resin tank VIII110 effluent analysis is as follows: 68.7ppm of bromide ion;

the acid generator tank 115 of the bipolar membrane device III112 controls hydrogen ions to 1.5mol/L, and detection is carried out: bromide 12.2%, sodium 183ppm:

the caustic soda tank 116 of bipolar membrane apparatus III112 controls 1.0mol/L hydroxyl, detection: sodium ion 2.31% and bromide ion 177ppm.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of the nanofiltration unit III302 is mainly sodium bromide, then is discharged after bromide ions are adsorbed by the resin tank VIII110, the regenerated liquid obtained by regenerating the resin tank VIII110 by sodium hydroxide is aqueous solution of sodium bromide and sodium hydroxide, and the aqueous solution of hydrobromic acid and sodium hydroxide can be obtained by treating the aqueous solution by the bipolar membrane device III 112.

It has also been demonstrated that the fresh water outlet 303 of the nanofiltration unit III302 can be treated with the bipolar membrane device II308, with the crystallizer II49, with the halogen generating reactor 38 and its auxiliary systems, with the electrolysis apparatus 109 and its auxiliary systems, with the resin tank VI111, with the resin tank VIII110+ bipolar membrane device III112, the six alternatives being used.

Examples II to 7

As shown in fig. 27, the system for purifying and recycling an aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a neutralization tank 94, a bipolar membrane device II308, a reverse osmosis concentration unit 305, a crystallizer V83 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, and the concentrate outlet 304 of the nanofiltration unit III302 is connected to the water inlet of the crystallizer V83; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97 is also connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device II308, and one of the outlets of the acid producing tank 309 of the bipolar membrane device II308 is connected to the acid adding unit 97.

The recovery process described above operates as follows:

after the aqueous solution of the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, and concentrated water of the nanofiltration unit III302 is heated and evaporated through the crystallizer V83 to obtain a solid; the fresh water of the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305, then the pH is regulated by the neutralization tank 94, and then the concentrated fresh water enters the bipolar membrane device II308 to treat one of the outlets of the acid production tank 309 of the bipolar membrane device II308 to provide hydrobromic acid for the acid adding unit 97.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

Crystallizer V83 gave a solid analysis: sodium carbonate=98.3%

The neutralization tank 94 discharges water as follows: carbonate, bicarbonate, hydroxide were undetectable and bromide was 6325ppm.

Conclusion: after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and a solid sodium carbonate product is obtained by the crystallizer V83; the fresh water of nanofiltration unit III302 is mainly sodium bromide. Residual carbonate and bicarbonate are then removed by the neutralization tank 94 and processed by the bipolar membrane device II308 to obtain an aqueous solution of sodium hydroxide and hydrobromic acid.

Meanwhile, examples II-1 to 6 demonstrate that the fresh water outlet 303 of the nanofiltration unit III302 can be treated by the bipolar membrane apparatus II308, the crystallizer II49, the halogen generation reactor 38 and the auxiliary system thereof, the electrolysis device 109 and the auxiliary system thereof, the resin tank VI111, the resin tank VIII 110+the bipolar membrane apparatus III112, and the combination of the six modes and the crystallizer V83 can be deduced to be operated.

Examples II to 8

As shown in fig. 28, the system for purifying and recycling the aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a heating tank 311, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a neutralization tank 94, a bipolar membrane device II308, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of a heating tank 311, an exhaust port is arranged above the heating tank 311, the water outlet of the heating tank 311 is connected to the water inlet of a cooler IV312, the water outlet of the cooler IV312 is connected to the inlet of a high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of a nanofiltration unit III302, the concentrated water outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of a mixing tank V46, the mixing tank V46 is also provided with a feeding pipeline, and the outlet of the mixing tank V46 is connected to the water inlet of a filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97 is also connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device II308, and one of the outlets of the acid producing tank 309 of the bipolar membrane device II308 is connected to the acid adding unit 97.

The recovery process described above operates as follows:

the aqueous solution in the aqueous solution discharge pipe 301 is heated by the heating tank 311 (bicarbonate is converted into carbonate+carbon dioxide, and carbon dioxide is discharged into the atmosphere), then cooled by the cooling tank 312, and then enters the nanofiltration unit III302, and the concentrated water in the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and then is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water from the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305, then the pH is regulated by the neutralization tank 94, and then the concentrated fresh water enters the bipolar membrane device II308 to treat one of the outlets of the acid production tank 29 of the bipolar membrane device I28 to provide hydrobromic acid for the acid adding unit 97.

The experiment was run using the above processing system: the heating tank 311 is heated to boiling point (with a substantial reduction in volume) with heat exchanger steam, the chiller IV312 controls the outlet water temperature of 30 ℃, the high pressure pump 216 gives a pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡3:1, neutralization tank 94 is controlled to have a pH of about 3.5 and acid addition unit 97 initially feeds 47.5% of industrial hydrobromic acid.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

Cooler IV312 effluent: bicarbonate=365 ppm, carbonate=21519 ppm, bromide=6362 ppm.

The concentrate outlet 304 of the nanofiltration unit III302 is analyzed as follows: carbonate=65325 ppm, bromide=4929 ppm;

The liquid outlet of filter V47 was analyzed as follows: cobalt ion=0.1 ppm, manganese ion=0.6 ppm.

The fresh water outlet 303 of the nanofiltration unit III302 is analyzed as follows: carbonate=2125 ppm, bromide=8101 ppm.

The neutralization tank 94 discharges water as follows: carbonate, bicarbonate, hydroxide were undetectable, and bromide was 14893ppm.

Acid generator tank 309 of bipolar membrane apparatus II308 controls hydrogen ions 1.0mol/L, detection: bromide 7.91% and sodium 69ppm;

the caustic soda pot 310 of the bipolar membrane apparatus II308 controls 1.0mol/L hydroxyl, detection: sodium ion 2.24%, bromide ion 131ppm.

Conclusion: after the aqueous solution in the aqueous solution discharge pipeline 301 is heated, boiled and concentrated (bicarbonate is converted into carbonate+carbon dioxide, a dioxide tower is released into the air, carbonate is divalent and can be better separated from monovalent bromide ions), the aqueous solution is cooled and is treated by the nanofiltration unit III302, and concentrated water of the nanofiltration unit III302 is mainly sodium carbonate and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of nanofiltration unit III302 is mainly sodium bromide. Residual carbonate and bicarbonate are then removed by the neutralization tank 94 and processed by the bipolar membrane device II308 to obtain an aqueous solution of sodium hydroxide and hydrobromic acid.

Meanwhile, examples II-1 to 6 demonstrate that the fresh water outlet 303 of the nanofiltration unit III302 can be treated by the bipolar membrane apparatus II308, the crystallizer II49, the halogen generation reactor 38 and the auxiliary system thereof, the electrolysis device 109 and the auxiliary system thereof, the resin tank VI111, the resin tank VIII 110+bipolar membrane apparatus III112, and the other can be used alternatively, so that it can be deduced that the buffer tank 126 in the six modes can be replaced by the heating tank 311 in combination with the alkali adding device I77. While examples II-7 demonstrate that the combination of mixing tank V46+ filter V47 in this combination is also operable with crystallizer V83.

Examples II to 9

As shown in fig. 29, 34 and 35, the system for purifying and reutilizing an aqueous solution mainly comprises an aqueous solution discharge pipe 301, a buffer tank 126, an electrodialysis device III313 for purifying monovalent ions, a neutralization tank 94, a bipolar membrane device II308, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipe 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the water inlet 212 of the electrodialysis device III313 for purifying monovalent ions, the water outlet II315 of the electrodialysis device III313 for purifying monovalent ions is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the water outlet I314 of the electrodialysis device III313 for purifying monovalent ions is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the neutralization tank 94, the acid adding unit 97 is also connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device II308, and one of the outlets of the acid producing tanks 309 of the bipolar membrane device II308 is connected to the acid adding unit 97.

The electrodialysis device III313 for purifying monovalent ions is connected in the same manner as the conventional electrodialysis device, except that the membrane type in the membrane stack is different from that of the conventional electrodialysis device, 10 repeated combinations of the monovalent anion permselective membrane 214 and the cation permselective membrane 213 are arranged in the electrode positive electrode 201-electrode negative electrode 202 in this embodiment, specifically, the monovalent anion permselective membrane 214 and the cation permselective membrane 213 form a water supply chamber 203 in the direction from the electrode positive electrode to the electrode negative electrode, a concentration chamber 204 is formed before the cation permselective membrane 213 and the monovalent anion permselective membrane 214, one membrane forming the electrode water chamber 215 closest to the electrode positive electrode 201 and one membrane forming the electrode water chamber 215 closest to the electrode negative electrode 202 and the one membrane forming the electrode water chamber 215 closest to the electrode negative electrode 202.

the outlet of the water feed tank 207 is connected to the inlet of the water feed pump 208, the outlet of the water feed pump 208 is connected to the inlet of the water feed chamber 203, and the outlet of the water feed chamber 203 is connected to the water feed tank 207 to form a circulation; the water supply tank 207 is internally provided with a partition board, and the water supply tank 207 is also provided with a water inlet 212 of electrodialysis equipment III313 for purifying monovalent ions and a water outlet II315 of the electrodialysis equipment III313 for purifying monovalent ions;

The outlet of the concentration tank 209 is connected to the inlet of the concentration pump 210, the outlet of the concentration pump 210 is connected to the inlet of the concentration chamber 204, and the outlet of the concentration chamber 204 is connected to the concentration tank 209 to form a cycle; a partition board is arranged in the concentration tank 209, and the concentration tank 209 is also provided with a pure water feed port 211 and a water outlet I314 of electrodialysis equipment III313 for purifying monovalent ions;

the recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali addition and tempering through the buffer tank 126, the aqueous solution enters an electrodialysis device III313 for purifying monovalent ions, a water outlet II315 (throttled divalent anion carbonate) of the electrodialysis device III313 for purifying monovalent ions is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to a filter V47 for filtration (solids are trapped in the filter V47); the outlet I314 of the electrodialysis device III313 for purifying monovalent ions (permeated monovalent anion bromide ions) is concentrated by the reverse osmosis concentration unit 305, the pH is regulated by the neutralization tank 94, and the concentrated monovalent ion is fed into the bipolar membrane device II308 to treat one of the outlets of the acid production tank 309 of the bipolar membrane device II308 to provide hydrobromic acid for the acid adding unit 97.

The polar water is circulated by a polar water tank 205, a polar water pump 206 and a polar water chamber 215; the water supply is circulated by a water supply tank 207, a water supply pump 208 and a water supply chamber 203; simultaneously, the aqueous solution to be treated is fed from the water inlet 212 of the electrodialysis device III313 for purifying monovalent ions and overflows from the water outlet II315 of the electrodialysis device III313 for purifying monovalent ions;

The concentrated solution is circulated by a concentration tank 209, a concentration pump 210 and a concentration chamber 204; simultaneously, pure water is fed from a pure water feed port 211 (flow rate is controlled) and overflows from a water outlet I314 of electrodialysis device III313 for purifying monovalent ions;

the experiment was run using the above processing system: the addition unit I77 is fed with 32% aqueous sodium hydroxide solution and automatically monitors and controls the pH of buffer tank 126 to approximately 11.5 and neutralization tank 94 to approximately 3.5, with the addition unit 97 initially fed with 47.5% commercial hydrobromic acid.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The outlet II315 of the electrodialysis device III313 for purifying monovalent ions is analyzed as follows: carbonate=54124 ppm, hydroxide=488 ppm, bromide=177 ppm;

The liquid outlet of filter V47 was analyzed as follows: cobalt ion=0.4 ppm, manganese ion=undetectable.

The outlet I314 of the electrodialysis device III for purifying monovalent ions is analyzed as follows: carbonate=168 ppm, hydroxide=23 ppm, bromide= 15480ppm.

The neutralization tank 94 discharges water as follows: carbonate, bicarbonate, hydroxyl were undetectable and bromide was 16113ppm.

Acid production tank 309 of bipolar membrane apparatus II308 controls hydrogen ion 1.2mol/L, detection: bromine ion 9.5% and sodium ion 99ppm;

the caustic soda pot 310 of the bipolar membrane apparatus II308 controls 1.2mol/L hydroxyl, detection: sodium ion 2.7%, bromide ion 38ppm.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the electrodialysis device III313 for purifying monovalent ions, the water outlet II315 of the electrodialysis device III313 for purifying monovalent ions is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the outlet I314 of the electrodialysis device III313 for purifying monovalent ions is mainly sodium bromide. Residual carbonate and bicarbonate are then removed by the neutralization tank 94 and processed by the bipolar membrane device II308 to obtain an aqueous solution of sodium hydroxide and hydrobromic acid.

Meanwhile, examples II-1 to 6 demonstrate that the aqueous solution of sodium bromide can be treated with the bipolar membrane device II308, the crystallizer II49, the halogen generation reactor 38 and its auxiliary system, the electrolysis device 109 and its auxiliary system, the resin tank VI111, the resin tank VIII110+ bipolar membrane device III112, or alternatively, the nanofiltration unit III302 in the above six modes can be replaced with the electrodialysis device III313 for purifying monovalent ions. While examples II-7 demonstrate that the combination of mixing tank V46+ filter V47 in this combination is also operable with crystallizer V83.

Examples II to 10

As shown in fig. 30, the system for purifying and recycling the aqueous solution mainly comprises an aqueous solution discharge pipeline 301, an evaporation tank I316, a cooler II344, a filter II317, a nanofiltration unit IV318 (a second-stage nanofiltration is designed, fresh water from a previous-stage nanofiltration is used as water for a next-stage nanofiltration, and is treated for multiple times, and each treatment aims at more thoroughly intercepting carbonate), a neutralization tank 94, a bipolar membrane device II308, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the inlet of the evaporation tank I316, an exhaust port is further arranged above the evaporation tank I316, the outlet of the evaporation tank I316 is connected to the inlet of the cooler II344, the outlet of the cooler II344 is connected to the inlet of the filter II317, the liquid outlet of the filter II317 is connected to the inlet of the preheater 322, the outlet of the preheater 322 is connected to the inlet of the dilution tank 323, the outlet of the dilution tank 323 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit IV318, the concentrate outlet 320 of the nanofiltration unit IV318 is connected to the water inlet of the agitation tank 321, the solid outlet of the agitation tank II317 is also connected to the inlet 48 of the agitation tank 321, the water outlet of the agitation tank 321 is connected to the dosing port 48 of the agitation tank V46, the agitation tank V46 is also provided with a feed line, and the outlet of the agitation tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 319 of the nanofiltration unit IV318 is connected to the neutralization tank 94, the acidification unit 97 is also connected to the neutralization tank 94, the outlet of the neutralization tank 94 is connected to the water inlet of the bipolar membrane device II308, and one of the outlets of the acidogenesis tank 309 of the bipolar membrane device II308 is connected to the acidification unit 97.

The recovery process described above operates as follows:

the concentrated solution of the aqueous solution in the aqueous solution discharge pipeline 301 after being concentrated by the reverse osmosis concentration unit 305 is heated and concentrated again by the evaporation tank I316, the concentrated solution of the evaporation tank I316 is cooled by the cooler II344 and then filtered by the filter II317, the filtrate of the filter II317 is preheated and diluted and then is subjected to separation of monovalent anions and divalent anions by the nanofiltration unit IV318, the concentrated water of the nanofiltration unit IV318 and the solid of the filter II317 are mixed by the stirring tank 321 and then are used as additive chemicals required by the mixing tank V46, mixed with the feed of the mixing tank V46, and then discharged to the filter V47 for filtration (the solid is trapped in the filter V47);

the fresh water from the nanofiltration unit IV318 is subjected to PH adjustment by the neutralization tank 94 and then enters the bipolar membrane apparatus II308 for treatment, and one of the outlets of the acid generator 309 of the bipolar membrane apparatus II308 provides hydrobromic acid to the acid adding unit 97.

The experiment was run using the above processing system: the evaporation tank I316 is heated to boiling point (actual measurement 104-105 ℃) by steam, the cooler II344 is cooled by a refrigerator to ensure that the material outlet temperature is 3 ℃, the preheating tank 322 controls the outlet temperature to be 30 ℃, the diluting tank 323 is fed with pure water, the high-pressure pump 216 gives 4MPa of pressure, and the nanofiltration unit IV318 controls fresh water: concentrate flow (per stage) ≡3:1, neutralization tank 94 is controlled to have a pH of about 3.5 and acid addition unit 97 initially feeds 47.5% of industrial hydrobromic acid.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The solids outlet of filter II317 was analyzed as follows: the moisture content is 45 percent, and the sodium carbonate content is 43.2 percent

The liquid outlet of filter II317 was analyzed as follows: 5.7% of bromide ion, 3.4% of carbonate and 0.5% of bicarbonate.

The concentrate outlet 320 of the nanofiltration unit IV318 is analyzed as follows: 7.98% of carbonate radical and 0.69% of bromide ion;

The liquid outlet of filter V47 was analyzed as follows: cobalt ion=0.1 ppm, manganese ion=0.8 ppm.

The fresh water outlet 319 of the nanofiltration unit IV318 is analyzed as follows: carbonate radical 0.33%, bromide ion 3.2%

The neutralization tank 94 discharges water as follows: carbonate, bicarbonate and hydroxide are undetectable, and bromide ion is 5.15%.

Acid generator tank 309 of bipolar membrane apparatus II308 controls hydrogen ions 1.0mol/L, detection: bromide ion 8.3%, sodium ion 132ppm;

the caustic soda pot 310 of the bipolar membrane apparatus II308 controls 1.0mol/L hydroxyl, detection: sodium ion 2.3%, bromide ion 255ppm.

Conclusion: the aqueous solution in the aqueous solution discharge pipeline 301 is concentrated and heated by the evaporation tank I316, bicarbonate is converted into carbonate and carbon dioxide (which are dissipated to the atmosphere), the sodium carbonate is reduced in solubility after being cooled and separated from sodium bromide by the filter II317, the filtrate of the filter II317 is mainly sodium bromide (and sodium carbonate with relatively low concentration) with high solubility, the sodium bromide is separated again by the nanofiltration unit IV318, the proportion of sodium carbonate is reduced again by fresh water of the nanofiltration unit IV318, and then residual carbonate and bicarbonate are removed by the neutralization tank 94, and then the sodium bromide and hydrobromic acid are treated by the bipolar membrane device II308 to obtain aqueous solution of sodium hydroxide and hydrobromic acid; the solids of filter II317 are mainly sodium carbonate, and the concentrate of nanofiltration unit IV318 is also mainly sodium carbonate, which can be used for dissolving TA, BA and precipitating cobalt manganese ions.

Meanwhile, as examples II-1 to 6 prove that the aqueous sodium bromide solution can be treated by the bipolar membrane device II308, the crystallizer II49, the halogen generation reactor 38 and the auxiliary system thereof, the electrolysis device 109 and the auxiliary system thereof, the resin tank VI111 and the resin tank VIII110 plus bipolar membrane device III112, the other one is selected for use; it has also been demonstrated that the nanofiltration unit IV318 of these six modes can be operated with electrodialysis apparatus IV for purification of monovalent ions. While examples II-7 demonstrate that the combination of mixing tank V46+ filter V47 in this combination is also operable with crystallizer V83.

Examples II to 11

As shown in fig. 31, a system for purifying and recycling an aqueous solution mainly comprises an aqueous solution discharge pipe 301, a mixing tank III324, a filter III325, a resin tank VIII110, a bipolar membrane apparatus III112, and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of a mixing tank III324, the mixing tank III324 is further provided with a dosing port 326, the water outlet of the mixing tank III324 is connected to the inlet of a filter III325, the liquid outlet of the filter III325 is connected to the inlet of a resin tank VIII110, and the outlet of the resin tank VIII110 is discharged; the resin tank VIII110 is provided with a regeneration liquid inlet 113, a regeneration liquid outlet 114 of the resin tank VIII110 is connected to a water inlet of the bipolar membrane device III112, and the bipolar membrane device III112 is provided with an acid production tank 115 and an alkali production tank 116.

The recovery process described above operates as follows:

the aqueous solution in the aqueous solution discharge pipeline 301 is mixed by adding alkali and calcium bromide in the mixing tank III324, filtered by the filter III325, the filtrate is discharged after being adsorbed with bromide ions by the resin tank VIII110, and the regenerated solution regenerated by the resin tank VIII110 by sodium hydroxide is treated by the bipolar membrane equipment III112 to obtain hydrobromic acid aqueous solution and sodium hydroxide aqueous solution.

The experiment was run using the above processing system: the dosing port 326 of mixing tank III324 was fed with an aqueous solution of calcium bromide and also with sodium hydroxide to adjust the pH to approximately 11.5, resin tank VIII110 was charged with a resin having adsorption of bromide ions, and the regeneration liquid inlet 113 of resin tank VIII110 was fed with an aqueous solution of 8% sodium hydroxide.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

Liquid outlet of filter III 325: bicarbonate was undetectable, carbonate=83 ppm, calcium 1335ppm, bromide=2.83%.

Resin tank VIII110 outlet: bromide=1435 ppm

The acid generator tank 115 of the bipolar membrane device III112 controls 2mol/L of hydrogen ions, and detection is carried out: bromide ion 16.2% and sodium ion 164ppm;

The caustic soda tank 116 of bipolar membrane apparatus III112 controls 1.0mol/L hydroxyl, detection: sodium ion 2.29% and bromide ion 85ppm.

Conclusion: the aqueous solution in the aqueous solution discharge line 301 is subjected to calcium bromide and sodium hydroxide addition, calcium carbonate insoluble substances are formed and removed by filtration, the filtrate is subjected to adsorption of bromide ions by the resin tank VIII110, and then the regenerated solution obtained by regenerating the resin tank VIII110 by sodium hydroxide is treated by the bipolar membrane device III112 to obtain aqueous solution of hydrobromic acid and sodium hydroxide.

Meanwhile, since examples II-1 to 6 show that the liquid outlet of the filter III325 can be treated with the bipolar membrane device II308, the crystallizer II49, the halogen generating reactor 38 and its auxiliary system, the electrolysis device 109 and its auxiliary system, the resin tank VI111, the resin tank VIII110+ bipolar membrane device III112, or both.

Examples II to 12

As shown in fig. 32, the system for purifying and recycling an aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a resin tank VIII110, a bipolar membrane apparatus III112, a crystallizer III327, an alkali adding device IV326, and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge line 301 is connected to the inlet of the resin tank VIII110, the outlet of the resin tank VIII110 is connected to the inlet of the buffer tank 126, the alkalizing device IV326 is also connected to the inlet of the buffer tank 126, and the outlet of the buffer tank 126 is connected to the inlet of the crystallizer III 327;

The resin tank VIII110 is provided with a regeneration liquid inlet 113, a regeneration liquid outlet 114 of the resin tank VIII110 is connected to a water inlet of the bipolar membrane device III112, and the bipolar membrane device III112 is provided with an acid production tank 115 and an alkali production tank 116.

The recovery process described above operates as follows:

the aqueous solution in the aqueous solution discharge line 301 is subjected to alkali addition (conversion of bicarbonate into carbonate) after bromide ion adsorption in the resin tank VIII110, and then is crystallized in the crystallizer III 327;

the regenerated liquid of the resin tank VIII110 regenerated by sodium hydroxide is treated by a bipolar membrane device III112 to obtain hydrobromic acid aqueous solution and sodium hydroxide aqueous solution.

The experiment was run using the above processing system: the resin tank VIII110 is filled with resin with the adsorption effect on bromide ions, and the regenerated liquid inlet 113 of the resin tank VIII110 is fed with 8 percent sodium hydroxide aqueous solution; buffer 126 controls ph≡11.5.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

Resin tank VIII110 outlet: bromide=37 ppm, carbonate 901ppm, bicarbonate 6105ppm;

crystallizer III327 analysis, sodium carbonate=95.3%;

the acid generator tank 115 of the bipolar membrane device III112 controls 1mol/L of hydrogen ions, and detection is carried out: bromide ion 8.1% and sodium ion 33ppm;

The caustic soda tank 116 of bipolar membrane apparatus III112 controls 2.0mol/L hydroxyl, detection: sodium ion 4.53%, bromide ion 122ppm.

Conclusion: the aqueous solution in the aqueous solution discharge line 301 is treated with a bipolar membrane device III112 by a method in which bromide ions are adsorbed in a resin tank VIII110, then bicarbonate is regulated to carbonate by regulating pH, and then sodium carbonate solid is obtained by crystallization, and the regenerated solution obtained by regenerating the resin tank VIII110 by sodium hydroxide is treated by the bipolar membrane device III112 to obtain aqueous solution of hydrobromic acid and sodium hydroxide.

Meanwhile, since examples II-1 to 6 prove that the resin tank VIII110+ bipolar membrane apparatus III112 treatment can be replaced by the halogen generating reactor 38 and its auxiliary system treatment, or by the electrolysis device 109 and its auxiliary system treatment, etc., it is deduced that the resin tank VIII110+ bipolar membrane apparatus III112 treatment in this embodiment is also feasible by the halogen generating reactor 38 and its auxiliary system treatment, or by the electrolysis device 109 and its auxiliary system treatment, etc.;

also, examples II-7 demonstrate that the decrystallization tank can be replaced with the dosing port of the decrystallization tank V46, and it can be deduced that the portion of sodium carbonate is not crystallized into sodium carbonate solids, but that the addition of the mixing tank V46 as the chemical (sodium carbonate) required by the mixing tank V46 is also feasible.

Examples II to 13

As shown in fig. 33, the system for purifying and recycling the aqueous solution mainly comprises an aqueous solution discharge pipeline 301, a buffer tank 126, a nanofiltration unit III302 (three-stage nanofiltration is designed, fresh water from the previous stage nanofiltration is used as water for the next stage nanofiltration, and the fresh water is treated for multiple times, and the purpose of each treatment is to more thoroughly intercept carbonate radicals), a volatile acid generator 332, a reverse osmosis concentration unit 305, a mixing tank V46, a filter V47 and the like.

The connection mode is as follows:

the outlet of the aqueous solution discharge pipeline 301 is connected to the water inlet of the buffer tank 126, the alkali adding device I77 is also connected to the buffer tank 126, the water outlet of the buffer tank 126 is connected to the inlet of the high-pressure pump 216, the outlet of the high-pressure pump 216 is connected to the water inlet of the nanofiltration unit III302, the concentrate outlet 304 of the nanofiltration unit III302 is connected to the dosing port 48 of the mixing tank V46, the mixing tank V46 is also provided with a feed line, and the outlet of the mixing tank V46 is connected to the water inlet of the filter V47; the fresh water outlet 303 of the nanofiltration unit III302 is connected to the water inlet of the reverse osmosis concentration unit 305, the concentrate outlet 306 of the reverse osmosis concentration unit 305 is connected to the water inlet of the volatile acid generator 332 (the fresh water outlet 307 of the reverse osmosis concentration device 305 discharges), the volatile acid generator 332 is further provided with an acid inlet pipe 333, the volatile acid generator 332 is further provided with a liquid drain 336 and a heater 334, the gas outlet 335 of the volatile acid generator 332 is connected to the condenser 43, and the outlet of the condenser 43 is connected to the acid production tank 45.

The recovery process described above operates as follows:

after the aqueous solution in the aqueous solution discharge pipeline 301 is subjected to alkali adding and blending through the buffer tank 126, the aqueous solution enters the nanofiltration unit III302, the concentrated water of the nanofiltration unit III302 is used as an additive chemical required by the mixing tank V46, is mixed with the feed of the mixing tank V46, and is discharged to the filter V47 for filtration (solids are trapped in the filter V47); the fresh water of the nanofiltration unit III302 is concentrated by the reverse osmosis concentration unit 305 and then enters the volatile acid generator 332, phosphoric acid is fed into the acid adding pipeline 333 of the volatile acid generator 332, and the fresh water is heated, hydrobromic acid is blown out, condensed by the condenser 43 and then collected in the acid production tank 45.

The experiment was run using the above processing system: the alkalizing unit I77 is fed with 32% aqueous sodium hydroxide solution, and automatically monitors and controls the pH of the buffer tank 126 to be approximately 11.5, the high-pressure pump 216 is given a pressure of 4MPa, and the nanofiltration unit III302 controls fresh water: concentrate flow (per stage) ≡4:1, the acid feed line 333 of the volatile acid generator 332 feeds the phosphoric acid solution.

Experimental results:

the aqueous solution discharge line 301 is analyzed as follows:

The acid generator tank 45 of the volatile acid generator 332 is analyzed as follows: hydrogen ion 2.1mol/L, bromide=16.5%.

Conclusion: after the aqueous solution in the aqueous solution discharge pipe 301 is subjected to PH elevation (bicarbonate is converted into carbonate, and carbonate is divalent and can be better separated from monovalent bromide ions) and is treated by the nanofiltration unit III302, the concentrated water in the nanofiltration unit III302 is mainly sodium carbonate, and can be used for dissolving TA, BA and precipitating cobalt and manganese ions; the fresh water of the nanofiltration unit III302 is mainly sodium bromide, and then is treated by the volatile acid generator 332 and its auxiliary systems to obtain hydrobromic acid aqueous solution. At the same time, the inference can be made: the volatile acid generator 332 may be used in the last step of the present embodiment as the bipolar membrane device II308, the crystallizer II49, the halogen generating reactor 38 and its accessories, the electrolysis apparatus 109 and its accessories, the resin tank VIII10, the resin tank VI111, and the oxidation reaction system 10, and may be used interchangeably.

Claims

1. A purification and reuse system is characterized in that,

when the purification and reuse system is a purification and reuse system for a solid mixture:

the solid discharge port of the crystallizer I is connected to the inlet of a mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of a cooling device I, the outlet of the cooling device I is connected to the inlet of a filter I, and the liquid outlet of the filter I is connected to the water inlet of a bipolar membrane device I; or the liquid outlet of the filter I is connected to the water inlet of the crystallizer II; or the liquid outlet of the filter I is connected with the water inlet of the COD reduction unit I, and the water outlet of the COD reduction unit I is connected with the oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of the halogen generation reactor;

or the solid discharge port of the crystallizer I is connected to the inlet of the mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of the filter I, the liquid outlet of the filter I is connected to the water inlet of the evaporation tank I, and the water outlet of the evaporation tank I is connected to the water inlet of the filter I; or the liquid outlet of the filter I is connected to the water inlet of the first evaporation tank, the water outlet of the first evaporation tank is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the filter I; or the liquid outlet of the filter I is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the filter I;

The liquid outlet of the first filter is connected to the water inlet of the bipolar membrane device I; or the liquid outlet of the filter I is connected to the water inlet of the crystallizer II; or the liquid outlet of the filter I is connected with the water inlet of the COD reduction unit I, and the water outlet of the COD reduction unit I is connected with the oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of the halogen generation reactor;

or the solid discharge port of the crystallizer I is connected to the inlet of the mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of the filter I, the liquid outlet of the filter I is connected to the water inlet of the COD reduction unit I, the water outlet of the COD reduction unit I is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of the COD reduction unit I, the water outlet of the COD reduction unit I is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to the oxidation reaction system; or the liquid outlet of the filter I is connected to the water inlet of the electrolysis device; or the liquid outlet of the filter I is connected to the water inlet of the resin tank VIII; or the liquid outlet of the filter I is connected to the water inlet of the resin tank VI; or the liquid outlet of the filter I is connected to the water inlet of the volatile acid generator;

Or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the esterification reactor is also provided with a washing liquid inlet, the washing liquid outlet of the esterification reactor is connected to the inlet of the cooling device I, and the outlet of the cooling device I is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system or the halogen generation reactor;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the esterification reactor is also provided with a washing liquid inlet, the washing liquid outlet of the esterification reactor is connected to the water inlet of the evaporation tank I, and the water outlet of the evaporation tank I is connected to the water inlet of the filter I; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the first evaporation tank, the water outlet of the first evaporation tank is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the first filter; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the first filter;

the liquid outlet of the first filter is connected with the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, and the water inlet of the oxidation reaction system or the halogen generation reactor;

Or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the discharge port of the esterification reactor is connected to the inlet of a washing tank I, the washing tank I is also provided with a washing liquid inlet, the washing liquid outlet of the washing tank I is connected to the inlet of a cooling device I, and the outlet of the cooling device I is connected to the water inlet of a bipolar membrane device I, the water inlet of a crystallizer II, an oxidation reaction system or the water inlet of a halogen generation reactor;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the discharge port of the esterification reactor is connected to the inlet of a washing tank I, the washing tank I is also provided with a washing liquid inlet, the washing liquid outlet of the washing tank I is connected to the water inlet of an evaporation tank I, and the water outlet of the evaporation tank I is connected to the water inlet of a filter I; or the washing liquid outlet of the washing tank I is connected to the water inlet of the evaporating tank I, the water outlet of the evaporating tank I is connected to the water inlet of the cooling device I, and the water outlet of the cooling device I is connected to the water inlet of the filter I; or the washing liquid outlet of the washing tank I is connected to the water inlet of the first cooling device, and the water outlet of the first cooling device is connected to the water inlet of the first filter;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the esterification reactor is also provided with a washing liquid inlet, the washing liquid outlet of the esterification reactor is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the washing liquid outlet of the esterification reactor is connected to the water inlet of electrodialysis equipment V for purifying monovalent ions, and the water outlet II of the electrodialysis equipment V for purifying monovalent ions is connected to an oxidation reaction system; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the electrolysis device; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the resin tank VIII; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the resin tank VI; or the washing liquid outlet of the esterification reactor is connected to the water inlet of the volatile acid generator;

or the solid discharge port of the crystallizer I is connected to the feed port I of the esterification reactor, the discharge port of the esterification reactor is connected to the inlet of a washing tank I, the washing tank I is also provided with a washing liquid inlet, the washing liquid outlet of the washing tank I is connected to the water inlet of a nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to an oxidation reaction system; or the washing liquid outlet of the washing tank I is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to the oxidation reaction system; or the washing liquid outlet of the washing tank I is connected to the water inlet of the electrolysis device; or the washing liquid outlet of the washing tank I is connected to the water inlet of the resin tank VIII; or the washing liquid outlet of the washing tank I is connected to the water inlet of the resin tank VI; or the washing liquid outlet of the washing tank I is connected to the water inlet of the volatile acid generator;

Or the solid discharge port of the crystallizer I is connected to the inlet of a mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of a filter I, and the solid outlet of the filter I is connected to an oxidation reaction system;

or the solid discharge port of the crystallizer I is connected to the inlet of the combustion equipment I, the outlet of the combustion equipment I is connected to the water inlet of the mixing tank V, the mixing tank V is also provided with a liquid inlet, and the outlet of the mixing tank V is connected to the oxidation reaction system; or the outlet of the combustion device I is connected to the water inlet of the mixing tank V, the mixing tank V is also provided with a liquid inlet, the outlet of the mixing tank V is connected to the water inlet of the filter V, and the water outlet of the filter V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; or the water outlet of the filter V is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the water outlet of the filter V is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to an oxidation reaction system; or the outlet of the mixing tank V is connected to the water inlet of the resin tank V, and the water outlet of the resin tank V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; or the water outlet of the resin tank V is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to the oxidation reaction system; or the water outlet of the resin tank V is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to an oxidation reaction system; or the outlet of the mixing tank V is connected to the water inlet of the resin tank VIII; or the outlet of the mixing tank V is connected to the water inlet of the resin tank VI; or the outlet of the mixing tank V is connected to an oxidation reaction system; or the outlet of the mixing tank V is connected to the water inlet of the halogen generation reactor; or the outlet of the mixing tank V is connected to the water inlet of the electrolysis device; or the outlet of the mixing tank V is connected to the water inlet of the volatile acid generator;

Or the solid discharge port of the crystallizer I is connected to the inlet of the mixing tank I, the mixing tank I is also provided with a liquid inlet, the outlet of the mixing tank I is connected to the inlet of the filter I, the liquid outlet of the filter I is connected to the inlet of the combustion equipment II, the outlet of the combustion equipment II is connected to the inlet of the mixing tank XII, the mixing tank XII is also provided with a liquid inlet, and the outlet of the mixing tank XII is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator; or the outlet of the mixing tank XII is connected to the water inlet of the nanofiltration unit V, and the concentrated water outlet of the nanofiltration unit V is connected to an oxidation reaction system; or the outlet of the mixing tank XII is connected to the water inlet of the electrodialysis device V for purifying monovalent ions, and the water outlet II of the electrodialysis device V for purifying monovalent ions is connected to an oxidation reaction system;

or the solid discharge port of the crystallizer I is connected to the water inlet of the volatile acid generator, and the water outlet of the volatile acid generator is discharged.

2. A purification and reuse system is characterized in that,

when the purification and reuse system is a purification and reuse system for an aqueous solution:

the water solution discharge pipeline is connected to the water inlet of the nanofiltration unit III, and the concentrated water outlet of the nanofiltration unit III is connected to the dosing port of the crystallizer V or the mixing tank V;

or the water solution discharge pipeline is connected to the water inlet of electrodialysis equipment III for purifying monovalent ions, and the water outlet II of the electrodialysis equipment III for purifying monovalent ions is connected to the drug adding port of the crystallizer V or the mixing tank V;

or the water solution discharge pipeline is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the inlet of the filter II, and the solid outlet of the filter II is connected to the dosing port of the drying equipment or the mixing tank V;

or the water solution discharge pipeline is connected to the water inlet of the nanofiltration unit III, and the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the crystallizer II, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator;

Or the water solution discharge pipeline is connected to the water inlet of electrodialysis equipment III for purifying monovalent ions, and the water outlet I of the electrodialysis equipment III for purifying monovalent ions is connected to the water inlet of an electrolysis device, the water inlet of a resin tank VI, the water inlet of a resin tank VIII, the water inlet of a crystallizer II, the water inlet of a bipolar membrane equipment II or the water inlet of a volatile acid generator;

or the water solution discharge pipeline is connected to the water inlet of the evaporation tank I, the water outlet of the evaporation tank I is connected to the inlet of the filter II, and the liquid outlet of the filter II is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the crystallizer II, the water inlet of the resin tank VI, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator;

or the water solution discharge pipeline is connected to the water inlet of the mixing tank III, the mixing tank III is also provided with a dosing port, the outlet of the mixing tank III is connected to the inlet of the filter III, and the liquid outlet of the filter III is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the bipolar membrane equipment II, the water inlet of the crystallizer II or the water inlet of the volatile acid generator;

Or the water solution discharge pipeline is connected to the water inlet of the halogen generation reactor, and the water outlet of the halogen generation reactor is connected to the dosing port or the discharge of the mixing tank V;

or the water solution discharge pipeline is connected to the water inlet of the electrolysis device, and the water outlet of the electrolysis device is connected to the water inlet of the crystallizer III, the dosing port of the mixing tank V or the discharge;

or the water solution discharge pipeline is connected to the water inlet of the resin tank VIII, and the water outlet of the resin tank VIII is connected to the water inlet of the crystallizer III, the dosing port of the mixing tank V or the discharge;

or the water solution discharge pipeline is connected with the water inlet of the volatile acid generator, and the water outlet of the volatile acid generator is connected with the water inlet of the crystallizer III, the dosing port of the mixing tank V or the discharge.

3. The system of claim 1, wherein when the purification and reuse system is a purification and reuse system for a solid mixture,

the device is also provided with gasification equipment, wherein the solid discharge port of the crystallizer I is connected to the inlet of the gasification equipment, and the solid discharge port of the gasification equipment is connected to the inlet of the mixing tank I, the inlet of the combustion equipment I, the feed port I of the esterification reactor, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device or the water inlet of the volatile acid generator;

Or the filter I is also provided with a washing device I;

or a washing device II is also arranged, the outlet of the mixing tank I is connected to the inlet of the solid-liquid separator XI, the solid outlet of the solid-liquid separator XI is connected to the inlet of the washing tank II, the washing device II is also connected to the washing tank II, and the outlet of the washing tank II is connected to the filter I;

or further provided with a washing device III, the outlet of the mixing tank I is connected to the inlet of a solid-liquid separator XI, the liquid outlet of the solid-liquid separator XI is connected to the inlet of a crystallizer IV, the solid outlet of the crystallizer IV is connected to a washing tank III, the washing device III is also connected to the washing tank III, and the outlet of the washing tank III is connected to a filter I; or the outlet of the washing tank III is connected to a solid-liquid separator XII, and the liquid outlet of the solid-liquid separator is connected to the water inlet of the COD reduction unit I, the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the evaporation tank I, the water inlet of the cooling device I or the water inlet of the volatile acid generator.

4. The system according to claim 1, characterized in that when the purification and reuse system is the purification and reuse system for solid mixtures, the fresh water outlet of the nanofiltration unit v or the water outlet i of the electrodialysis device v for purifying monovalent ions is connected to the water inlet of the bipolar membrane device one, the water inlet of the crystallizer one, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank viii, the water inlet of the resin tank vi or the water inlet of the volatile acid generator.

5. The system according to claim 1, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the COD reduction unit i includes at least one of a biochemical treatment device i, a higher oxidation device i, an extraction device i, an acidification device i, a resin tank i, and an electrodialysis device i.

6. The system of claim 1, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, further comprising a COD-reducing unit ii, a COD-reducing unit iii, a COD-reducing unit iv, or a COD-reducing unit v:

the liquid outlet of the filter I is connected to the water inlet of the COD reduction unit II, and the water outlet of the COD reduction unit II is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the evaporation tank I or the water inlet of the cooling device I;

Or the liquid outlet of the filter I is connected to the water inlet of the COD reduction unit III, and the water outlet of the COD reduction unit III is connected to the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I and the water inlet of the cooling equipment I;

or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the inlet of the cooling device I, the outlet of the cooling device I is connected to the water inlet of the COD reduction unit IV, and the water outlet of the COD reduction unit IV is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the evaporation tank I and the water inlet of the cooling device I;

or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the water inlet of the COD reduction unit IV, and the water outlet of the COD reduction unit IV is connected to the water inlet of the nanofiltration unit V, the water inlet of the electrodialysis device V for purifying monovalent ions, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

Or the fresh water outlet of the nanofiltration unit V is connected to the water inlet of the COD reduction unit V, and the water outlet of the COD reduction unit V is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer I, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or the water outlet I of the electrodialysis device V for purifying monovalent ions is connected to the water inlet of the COD reduction unit V, and the water outlet of the COD reduction unit V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer I, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator.

7. The system of claim 3, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, further comprising a COD reduction unit ii or a COD reduction unit iii:

the liquid outlet of the solid-liquid separator XII is connected to the water inlet of the COD reduction unit II, and the water outlet of the COD reduction unit II is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the evaporation tank I or the water inlet of the cooling device I;

Or the liquid outlet of the solid-liquid separator XII is connected to the water inlet of the COD reduction unit III, and the water outlet of the COD reduction unit III is connected to the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I and the water inlet of the cooling device I.

8. The system according to claim 4, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, there is further provided a COD reduction unit v:

the fresh water outlet of the nanofiltration unit V is connected to the water inlet of the COD reduction unit V, and the water outlet of the COD reduction unit V is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer I, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

9. The system according to claim 6 or 7, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the COD reduction unit ii includes at least one of a biochemical treatment device ii, a higher oxidation device ii, an extraction device ii, an acidification device ii, a resin tank ii, and an electrodialysis device iv; or the COD reducing unit III comprises at least one of a biochemical treatment device III, a higher oxidation device III, an extraction device III, an acidification device III, a resin tank III and an electrodialysis device III.

10. The system according to claim 6 or 8, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the COD reduction unit v comprises at least one of a biochemical treatment device v, a higher oxidation device v, an extraction device v, an acidification device v, a resin tank xi, and an electrodialysis device ii.

11. The system of claim 6, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the COD reduction unit iv comprises at least one of a biochemical treatment device iv, a higher oxidation device iv, an extraction device iv, an acidification device iv, a resin tank x, and an electrodialysis device v.

12. The system of claim 1, wherein when the purification and reuse system is the purification and reuse system for a solid mixture,

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II along the direction of material flow;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the evaporation tank I or the water inlet of the cooling equipment I along the direction of material flow;

or a resin tank V is arranged between the liquid outlet of the filter I and the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator along the direction of material flow;

or the washing liquid outlet of the esterification reactor or the washing liquid outlet of the washing tank I is connected to the cooling equipment I, and a mixing tank V and a filter V are sequentially arranged between the outlet of the cooling equipment I and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the oxidation reaction system or the water inlet of the halogen generation reactor along the direction of material flow;

or a mixing tank V and a filter V are sequentially arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the electrolysis device, a water inlet of the resin tank VI, a water inlet of the resin tank VIII or a water inlet of the volatile acid generator, a water inlet of the evaporation tank I or a water inlet of the cooling equipment I along the direction of material flow;

or a mixing tank V and a filter V are sequentially arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the electrolysis device, a water inlet of the resin tank VI, a water inlet of the resin tank VIII or a water inlet of the volatile acid generator along the direction of material flow;

or a resin tank V is arranged between the liquid outlet of the filter I and the inlet of the combustion equipment II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the inlet of the combustion equipment II along the direction of material flow;

Or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the mixing tank XII and the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator along the direction of material flow;

or the water outlet of the halogen generation reactor is connected to a mixing tank V, the water outlet of the mixing tank V is connected to a filter V, and the water outlet of the filter V is discharged;

or the water outlet of the electrolysis device is connected to a mixing tank V, the water outlet of the mixing tank V is connected to a filter V, and the water outlet of the filter V is discharged;

or the water outlet of the volatile acid generator is connected to a mixing tank V, the water outlet of the mixing tank V is connected to a filter V, and the water outlet of the filter V is discharged.

13. The system of claim 3, wherein when the purification and reuse system is the purification and reuse system for a solid mixture,

a resin tank V is arranged between a liquid outlet of the solid-liquid separator XII and a water inlet of the bipolar membrane equipment I or a water inlet of the crystallizer II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II along the direction of material flow;

or a resin tank V is arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the first evaporation tank or the water inlet of the first cooling device;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the evaporation tank I or the water inlet of the cooling equipment I along the direction of material flow;

or a resin tank V is arranged between the liquid outlet of the solid-liquid separator XII and the inlet of the combustion equipment II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the inlet of the combustion equipment II along the direction of material flow;

Or a resin tank V is arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator along the direction of material flow;

14. The system of claim 6, wherein when the purification and reuse system is the purification and reuse system for a solid mixture,

a resin tank V is arranged between the liquid outlet of the filter I and the water inlet of the COD reduction unit II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the COD reduction unit II along the direction of material flow;

or a mixing tank V and a filter V are sequentially arranged between the water outlet of the COD reducing unit II and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer II along the direction of material flow;

or a resin tank V is arranged between the liquid outlet of the filter I and the water inlet of the COD reduction unit III;

Or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the filter I and the water inlet of the COD reduction unit III along the direction of material flow;

or a mixing tank V and a filter V are sequentially arranged between the water outlet of the COD reducing unit III and the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator along the direction of material flow;

or a resin tank V is arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the COD reduction unit IV;

or a mixing tank V and a filter V are sequentially arranged between a washing liquid outlet of the esterification reactor or a washing liquid outlet of the washing tank I and a water inlet of the COD reduction unit IV along the direction of material flow;

Or a resin tank V is arranged between the water outlet of the COD reducing unit IV and the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the volatile acid generator, the water inlet of the evaporation tank I or the water inlet of the cooling device I;

or a mixing tank V and a filter V are sequentially arranged between the water outlet of the COD reducing unit IV and the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the volatile acid generator, the water inlet of the evaporating tank I or the water inlet of the cooling device I along the material flow direction;

15. The system of claim 7, wherein when the purification and reuse system is the purification and reuse system for a solid mixture,

a resin tank V is arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit II;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit II along the direction of material flow;

or a resin tank V is arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit III;

or a mixing tank V and a filter V are sequentially arranged between the liquid outlet of the solid-liquid separator XII and the water inlet of the COD reduction unit III along the direction of material flow;

16. The system according to claim 1, characterized in that when the purification and reuse system is the purification and reuse system for a solid mixture, the solid outlet of the filter i or the solid outlet of the solid-liquid separator XII is connected to the inlet of the combustion device II or the inlet of the combustion device III.

17. The system of claim 2, wherein when the purification reuse system is the aqueous solution purification reuse system,

A cooling device II is arranged between the water outlet of the evaporation tank I and the filter II;

or the liquid outlet of the filter II is connected to the water inlet of the nanofiltration unit IV, and the fresh water outlet of the nanofiltration unit IV is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator;

or a cooling device II is arranged between the water outlet of the evaporation tank I and the filter II; the liquid outlet of the filter II is connected to the water inlet of the nanofiltration unit IV, and the fresh water outlet of the nanofiltration unit IV is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator;

or the liquid outlet of the filter II is connected to the water inlet of electrodialysis equipment IV for purifying monovalent ions, and the water outlet I of the electrodialysis equipment IV for purifying monovalent ions is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator;

Or a cooling device II is arranged between the water outlet of the evaporation tank I and the filter II; the liquid outlet of the filter II is connected to the water inlet of electrodialysis equipment IV for purifying monovalent ions, and the water outlet I of the electrodialysis equipment IV for purifying monovalent ions is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI, the water inlet of the crystallizer II, the water inlet of the bipolar membrane equipment II or the water inlet of the volatile acid generator.

18. The system of claim 1, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the liquid outlet of the filter I and the water inlet of the bipolar membrane device I, the liquid outlet of the filter I and the water inlet of the crystallizer II, the liquid outlet of the filter I and the water inlet of the halogen generation reactor, the liquid outlet of the filter I and the water inlet of the electrolysis device, the liquid outlet of the filter I and the water inlet of the resin tank VIII, the liquid outlet of the filter I and the water inlet of the resin tank VI, the liquid outlet of the filter I and the water inlet of the volatile acid generator, the outlet of the cooling device I and the water inlet of the bipolar membrane device I, the outlet of the cooling device I and the water inlet of the crystallizer II the method comprises the steps of connecting an outlet of cooling equipment I with an oxidation reaction system, connecting an outlet of the cooling equipment I with a water inlet of a halogen generation reactor, connecting an outlet of the cooling equipment I with a water inlet of an electrolysis device, connecting an outlet of the cooling equipment I with a water inlet of a resin tank VIII, connecting an outlet of the cooling equipment I with a water inlet of a resin tank VI, connecting an outlet of the cooling equipment I with a water inlet of a volatile acid generator, connecting a washing liquid outlet of an esterification reactor with a water inlet of the electrolysis device, connecting a washing liquid outlet of the esterification reactor with a water inlet of the resin tank VIII, connecting a washing liquid outlet of the esterification reactor with a water inlet of the resin tank VI, the method comprises the steps of connecting a washing liquid outlet of an esterification reactor with a water inlet of a volatile acid generator, connecting a washing liquid outlet of a washing tank I with a water inlet of an electrolysis device, connecting a washing liquid outlet of the washing tank I with a water inlet of a resin tank VIII, connecting a washing liquid outlet of the washing tank I with a water inlet of a resin tank VI, connecting a washing liquid outlet of the washing tank I with a water inlet of a volatile acid generator, connecting a water outlet of the mixing tank with a water inlet of bipolar membrane equipment I, connecting a water outlet of the mixing tank with a water inlet of a crystallizer II, connecting a water outlet of a mixing tank XII with an oxidation reaction system, and connecting a water inlet of a bipolar membrane equipment II with a water inlet of a resin tank VI. The water outlet of the mixing tank XII is connected with the water inlet of the halogen generation reactor, the water outlet of the mixing tank XII is connected with the water inlet of the electrolysis device, the water outlet of the mixing tank XII is connected with the water inlet of the resin tank VI, the water outlet of the mixing tank XII is connected with the water inlet of the resin tank VIII, the water outlet of the mixing tank XII is connected with the water inlet of the volatile acid generator, the water outlet of the COD reduction unit I is connected with the water inlet of the cooling device I, the liquid outlet of the filter I is connected with the water inlet of the evaporation tank I or the liquid outlet of the filter I is connected with the water inlet of the cooling device I:

The device is provided with a nanofiltration unit I, wherein a fresh water outlet of the nanofiltration unit I is connected with a water inlet of the bipolar membrane equipment I, a water inlet of the crystallizer II, a water inlet of the halogen generation reactor, the oxidation reaction system, a water inlet of the electrolysis device, a water inlet of the resin tank VIII, a water inlet of the resin tank VI or a water inlet of the volatile acid generator;

or provided with an electrodialysis device I for purifying monovalent ions, the water outlet I of which is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or an evaporation tank II and a filter IX are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the filter IX, and the liquid outlet of the filter IX is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

Or an evaporation tank II, a cooling device III and a filter IX are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the cooling device III, the water outlet of the cooling device III is connected to the water inlet of the filter IX, and the liquid outlet of the filter IX is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or an evaporation tank II, a filter IX and a nanofiltration unit II are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the nanofiltration unit II, and the fresh water outlet of the nanofiltration unit II is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

Or an evaporation tank II, a cooling device III, a filter IX and a nanofiltration unit II are sequentially arranged along the material flow direction, the water outlet of the evaporation tank II is connected to the water inlet of the cooling device III, the water outlet of the cooling device III is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the nanofiltration unit II, and the fresh water outlet of the nanofiltration unit II is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or an evaporation tank II, a filter IX and electrodialysis equipment II for purifying monovalent ions are sequentially arranged along the flow direction of the material, the water outlet of the evaporation tank II is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the electrodialysis equipment II for purifying monovalent ions, and the water outlet I of the electrodialysis equipment II for purifying monovalent ions is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

Or an evaporation tank II, a cooling device III, a filter IX and an electrodialysis device II for purifying monovalent ions are sequentially arranged along the flow direction of the material, the water outlet of the evaporation tank II is connected to the water inlet of the cooling device III, the water outlet of the cooling device III is connected to the water inlet of the filter IX, the liquid outlet of the filter IX is connected to the water inlet of the electrodialysis device II for purifying monovalent ions, and the water outlet I of the electrodialysis device II for purifying monovalent ions is connected to the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or a mixing tank X and a filter X are sequentially arranged along the material flow direction, the mixing tank X is also provided with a chemical adding port, the outlet of the mixing tank X is connected to the water inlet of the filter X, and the liquid outlet of the filter X is connected to the water inlet of the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the oxidation reaction system, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator.

19. The system of claim 3, wherein when the purification reuse system is the pair of solid mixture purification reuse system, between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane device I, between the liquid outlet of the solid-liquid separator XII and the water inlet of the crystallizer II, between the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generating reactor, between the liquid outlet of the solid-liquid separator XII and the water inlet of the electrolysis device, between the liquid outlet of the solid-liquid separator XII and the water inlet of the resin tank VIII, between the liquid outlet of the solid-liquid separator XII and the water inlet of the resin tank VI, between the liquid outlet of the solid-liquid separator XII and the water inlet of the volatile acid generator, between the liquid outlet of the solid-liquid separator XII and the water inlet of the halogen generating reactor, between the liquid outlet of the solid-liquid separator XII and the water inlet of the evaporation tank I or between the liquid outlet of the solid-liquid separator XII and the water inlet of the cooling device I:

20. The system according to claim 12, 13, 14 or 15, wherein when the purification and reuse system is the solid mixture purification and reuse system, between the water outlet of the resin tank v and the water inlet of the bipolar membrane device i, between the water outlet of the resin tank v and the water inlet of the crystallizer ii, between the water outlet of the filter v and the water inlet of the bipolar membrane device i, between the water outlet of the filter v and the water inlet of the crystallizer ii, between the water outlet of the filter v and the water inlet of the electrolysis device, between the water outlet of the filter v and the water inlet of the resin tank viii, between the water outlet of the filter v and the water inlet of the resin tank vi, between the water outlet of the filter v and the water inlet of the volatile acid generator, between the water outlet of the resin tank v and the water inlet of the electrolysis device, between the water outlet of the resin tank v and the water inlet of the bipolar membrane device v, between the water outlet of the resin tank v and the water inlet of the resin tank viii, between the water outlet of the resin tank v and the water inlet of the crystallizer ii, between the water outlet of the halogen generating reaction tank v and the water inlet of the halogen generating system, between the water inlet of the reactor and the water inlet of the resin tank v, between the water outlet of the halogen generating system and the water inlet of the resin tank v and the water inlet of the reactor, between the outlet of the mixing tank v and the water inlet of the volatile acid generator, between the outlet of the mixing tank v and the water inlet of the resin tank viii, between the liquid outlet of the filter v and the water inlet of the evaporation tank one, between the liquid outlet of the filter v and the water inlet of the cooling device one, between the liquid outlet of the resin tank v and the water inlet of the evaporation tank one, or between the liquid outlet of the resin tank v and the water inlet of the cooling device one:

21. The system of claim 6, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the water outlet of the COD reduction unit II is connected with the water inlet of the bipolar membrane device I, the water outlet of the COD reduction unit II is connected with the water inlet of the crystallizer II, the water outlet of the COD reduction unit III is connected with the water inlet of the electrolysis device, the water outlet of the COD reduction unit III is connected with the water inlet of the resin tank VIII, the water outlet of the COD reduction unit III is connected with the water inlet of the resin tank VI, the water outlet of the COD reduction unit III is connected with the water inlet of the volatile acid generator, the water outlet of the COD reduction unit III is connected with the water inlet of the halogen generation reactor, the water outlet of the COD reduction unit IV is connected with the water inlet of the bipolar membrane device I the water outlet of the COD reduction unit IV is connected with the oxidation reaction system, the water outlet of the COD reduction unit IV is connected with the water inlet of the crystallizer II, the water outlet of the COD reduction unit IV is connected with the water inlet of the halogen generation reactor, the water outlet of the COD reduction unit IV is connected with the water inlet of the electrolysis device, the water outlet of the COD reduction unit IV is connected with the water inlet of the resin tank VIII, the water outlet of the COD reduction unit IV is connected with the water inlet of the resin tank VI, the water outlet of the COD reduction unit IV is connected with the water inlet of the volatile acid generator, the water outlet of the COD reduction unit II is connected with the water inlet of the evaporation tank I, the water outlet of the COD reduction unit II is connected with the water inlet of the cooling device I, the water outlet of the COD reduction unit III is connected with the water inlet of the evaporation tank I, the water outlet of the COD reduction unit III is connected with the water inlet of the cooling equipment I, the water outlet of the COD reduction unit IV is connected with the water inlet of the evaporation tank I or the water outlet of the COD reduction unit IV is connected with the water inlet of the cooling equipment I:

22. The system of claim 7, wherein when the purification and reuse system is the solid mixture purification and reuse system, the water outlet of the COD reduction unit ii and the water inlet of the bipolar membrane device i, the water outlet of the COD reduction unit ii and the water inlet of the crystallizer ii, the water outlet of the COD reduction unit iii and the water inlet of the electrolyzer, the water outlet of the COD reduction unit iii and the water inlet of the resin tank viii, the water outlet of the COD reduction unit iii and the water inlet of the resin tank vi, the water outlet of the COD reduction unit iii and the water inlet of the volatile acid generator, the water outlet of the COD reduction unit iii and the water inlet of the halogen generating reactor, the water outlet of the COD reduction unit ii and the water inlet of the evaporator tank one, the water outlet of the COD reduction unit ii and the water inlet of the cooling device one, the water outlet of the COD reduction unit iii and the water inlet of the evaporator tank one, or the water outlet of the COD reduction unit iii and the water inlet of the cooling device one, the COD reduction unit iii and the water inlet of the cooling device.

23. The system of claim 5, wherein the system further comprises a controller configured to control the controller,

and a water outlet II of the electrodialysis device I:

directly discharging;

or is connected to the water inlet of the resin tank IV, and the water outlet of the resin tank IV is discharged;

or to the water inlet of a mixing tank IV, the water outlet of which is connected to the water inlet of a filter IV, the liquid outlet of which discharges.

24. The system of claim 9, wherein the system further comprises a controller configured to control the controller,

the water outlet II of the electrodialysis device III or the water outlet II of the electrodialysis device IV:

directly discharging;

25. The system of claim 10, wherein the system further comprises a controller configured to control the controller,

and a water outlet II of the electrodialysis device II:

directly discharging;

26. The system of claim 11, wherein the system further comprises a controller configured to control the controller,

and a water outlet II of the electrodialysis device V:

directly discharging;

27. The system of claim 2, wherein the system further comprises a controller configured to control the controller,

the solid outlet of the filter II is connected with the water inlet of the crystallizer VI, the drying equipment or the dosing port of the mixing tank V;

or when the concentrated water outlet of the nanofiltration unit III is connected to the crystallizer V, the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the bipolar membrane equipment II, the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or when the concentrated water outlet of the nanofiltration unit III is connected to the dosing port of the mixing tank V, the fresh water outlet of the nanofiltration unit III is connected to the water inlet of the crystallizer II, the water inlet of the halogen generation reactor, the water inlet of the bipolar membrane equipment II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or when the water outlet II of the electrodialysis device III for purifying monovalent ions is connected to the crystallizer V, the water outlet I of the electrodialysis device III for purifying monovalent ions is connected to the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or when the water outlet I of the electrodialysis device III for purifying monovalent ions is connected to the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II or the water inlet of the volatile acid generator, the water outlet II of the electrodialysis device III for purifying monovalent ions is connected to the water inlet of the crystallizer V, the medicine feeding port or the discharge port of the mixing tank V.

28. The system of claim 17, wherein the system further comprises a controller configured to control the controller,

the concentrated water outlet of the nanofiltration unit IV is connected with the water inlet of the crystallizer X, the dosing port of the mixing tank V, the water inlet of the evaporation tank I, the water inlet of the cooling equipment II and the water inlet or discharge of the filter II;

or the water outlet II of the electrodialysis device IV for purifying monovalent ions is connected with the water inlet of the crystallizer X, the dosing port of the mixing tank V, the water inlet of the evaporation tank I, the water inlet of the cooling device II, the water inlet of the filter II or the discharge.

29. The system of claim 20, wherein when the purification and reuse system is the purification and reuse system for a solid mixture, the method comprises the steps of connecting a water outlet of a resin tank V with a water inlet of bipolar membrane equipment I, connecting a water outlet of the resin tank V with a water inlet of a crystallizer II, connecting a liquid outlet of the filter V with a water inlet of the bipolar membrane equipment I, connecting a liquid outlet of the filter V with a water inlet of an electrolysis device, connecting a liquid outlet of the filter V with a water inlet of the resin tank VIII, connecting a liquid outlet of the filter V with a water inlet of the resin tank VI, connecting a liquid outlet of the filter V with a water inlet of a volatile acid generator, connecting a liquid outlet of the resin tank V with a water inlet of an electrolysis device, connecting a liquid outlet of the resin tank V with a water inlet of the resin tank VI, connecting a liquid outlet of the resin tank V with a water inlet of a volatile acid generator, connecting a liquid outlet of the resin tank V with a water inlet of a halogen reaction vessel, connecting a liquid outlet of the resin tank V with a water inlet of the halogen reaction vessel, connecting a liquid outlet of the reaction vessel, and a mixed reaction vessel, and a liquid outlet of the mixed reaction vessel, and a liquid, and connecting the mixed reaction vessel between the liquid and the liquid, between the outlet of the mixing tank v and the water inlet of the volatile acid generator, between the outlet of the mixing tank v and the water inlet of the resin tank viii, between the liquid outlet of the filter v and the water inlet of the evaporation tank one, between the liquid outlet of the filter v and the water inlet of the cooling device one, between the liquid outlet of the resin tank v and the water inlet of the evaporation tank one, or between the liquid outlet of the resin tank v and the water inlet of the cooling device one:

30. The system of claim 18, 19, 21, 22 or 29, wherein,

or the water outlet II of the electrodialysis device I for extracting monovalent ions is connected with the water inlet of the crystallizer VIII, the dosing port of the mixing tank V or the discharge;

or the concentrated water outlet of the nanofiltration device II is connected to the water inlet of the crystallizer VIII, the dosing port of the mixing tank V, the water inlet of the evaporation tank II, the water inlet of the cooling equipment III and the water inlet or discharge of the filter IX;

or the water outlet II of the electrodialysis device II for extracting monovalent ions is connected to the water inlet of the crystallizer VIII, the dosing port of the mixing tank V, the water inlet of the evaporation tank II, the water inlet of the cooling device III, and the water inlet or discharge of the filter IX.

31. The system according to claim 18, 19, 21, 22 or 29, further comprising an alkali adding device i or a heating device i;

the outlet of the alkali adding device I is connected to a liquid outlet of the filter I, a liquid outlet of the solid-liquid separator XII, a water outlet of the COD reduction unit II, a water outlet of the resin tank V, a water outlet of the filter V, a water outlet of the COD reduction unit III, a washing liquid outlet of the esterification reactor, a washing liquid outlet of the washing tank I, an outlet of the cooling equipment I, a water outlet of the COD reduction unit IV, a water outlet of the mixing tank V or a water outlet of the mixing tank XII and a water inlet of the nanofiltration unit I, or a buffer tank is used at a connection position of the pipelines;

Or the outlet of the alkali adding device I is connected to a pipeline between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reducing unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reducing unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling equipment I, the water outlet of the COD reducing unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the evaporation tank II, or the connection position of the pipeline is provided with a buffer tank;

or the outlet of the alkali adding device I is connected to a pipeline between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reducing unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reducing unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reducing unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the electrodialysis device I for purifying monovalent ions, or the connection position of the pipeline is provided with a buffer tank;

Or a heating device I and a cooling device IV are sequentially arranged between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reduction unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reduction unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reduction unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the nanofiltration unit I along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

or a heating device I and a cooling device IV are sequentially arranged between the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reduction unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reduction unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reduction unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the electrodialysis device I for purifying monovalent ions along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

Or the liquid outlet of the filter I, the liquid outlet of the solid-liquid separator XII, the water outlet of the COD reduction unit II, the water outlet of the resin tank V, the water outlet of the filter V, the water outlet of the COD reduction unit III, the washing liquid outlet of the esterification reactor, the washing liquid outlet of the washing tank I, the outlet of the cooling device I, the water outlet of the COD reduction unit IV, the water outlet of the mixing tank V or the water outlet of the mixing tank XII and the water inlet of the mixing tank X are sequentially provided with a heating device I and a cooling device V along the material flow direction, or a heating device I, a decarburization tower I and a cooling device V along the material flow direction.

32. The system according to claim 2 or 17, characterized in that an alkali adding device i or a heating device i is also provided;

the outlet of the alkali adding device I is connected to a pipeline between the water solution discharge pipeline and the water inlet of the nanofiltration unit III, the water inlet of the electrodialysis equipment III for purifying monovalent ions, the water inlet of the evaporation tank I or the water inlet of the mixing tank III, or a buffer tank is used at the connection position of the pipeline;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the nanofiltration unit III, the water inlet of the electrodialysis device III for purifying monovalent ions, the water inlet of the evaporation tank I or the water inlet of the mixing tank III along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the halogen generation reactor along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

Or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the electrolysis device along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the resin tank VIII along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

or a heating device I and a cooling device IV are sequentially arranged between the water solution discharge pipeline and the water inlet of the volatile acid generator along the material flow direction, or a heating device I, a decarburization tower I and a cooling device IV are sequentially arranged along the material flow direction;

or a heating device I is arranged between the water outlet of the halogen generation reactor, the water outlet of the electrolysis device, the water outlet of the resin tank VIII or the water outlet of the volatile acid generator and the water inlet of the crystallizer III along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the flow direction of the material; or a heating device I and a cooling device V are sequentially arranged along the flow direction of the material; or a heating device I, a decarburization tower I and a cooling device V are sequentially arranged along the flow direction of the material;

Or a heating device I is arranged between the water outlet of the halogen generation reactor, the water outlet of the electrolysis device, the water outlet of the resin tank VIII or the water outlet of the volatile acid generator and the dosing port of the mixing tank V along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the flow direction of the material; or a heating device I and a cooling device V are sequentially arranged along the flow direction of the material; or a heating device I, a decarburization tower I and a cooling device V are sequentially arranged along the flow direction of the material;

or a heating device I is arranged between the concentrated water outlet of the nanofiltration unit III and the water inlet of the crystallizer V or the medicine adding port of the mixing tank V along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the flow direction of the material; or a heating device I and a cooling device VI are sequentially arranged along the flow direction of the material; or a heating device I, a decarburization tower I and cooling equipment VI are sequentially arranged along the flow direction of the material;

or a heating device I is arranged between the water outlet II of the electrodialysis equipment III for purifying monovalent ions and the water inlet of the crystallizer V or the medicine adding port of the mixing tank V along the direction of material flow; or a heating device I and a decarburization tower I are sequentially arranged along the flow direction of the material; or a heating device I and a cooling device VI are sequentially arranged along the flow direction of the material; or a heating device I, a decarburization tower I and a cooling device VI are sequentially arranged along the flow direction of the material.

33. The system according to claim 18, 19, 21, 22 or 29, further comprising an alkali adding device ii or a heating device ii;

or the outlet of the alkali adding device II is connected to a pipeline between the liquid outlet of the filter IX and the water inlet of the electrodialysis device II for purifying monovalent ions, or a buffer tank is used at the connection position of the pipeline;

or a heating device II and a cooling device VII are sequentially arranged between the liquid outlet of the filter IX and the water inlet of the nanofiltration unit II along the material flow direction, or the heating device II, the decarburization tower II and the cooling device VII are sequentially arranged along the material flow direction;

or a heating device II and a cooling device VII are sequentially arranged between the liquid outlet of the filter IX and the water inlet of the electrodialysis device II for purifying monovalent ions along the material flow direction, or the heating device II, the decarburization tower II and the cooling device VII are sequentially arranged along the material flow direction.

34. The system according to claim 17, further comprising an alkali adding device ii or a heating device ii;

or the outlet of the alkali adding device II is connected to a pipeline between the liquid outlet of the filter II and the water inlet of the electrodialysis device IV for purifying monovalent ions, or a buffer tank is used at the connection position of the pipeline;

or a heating device II and cooling equipment VIII are sequentially arranged between the liquid outlet of the filter II and the water inlet of the nanofiltration unit IV along the material flow direction, or the heating device II, the decarburization tower II and the cooling equipment VIII are sequentially arranged along the material flow direction;

or a heating device II and a cooling device VIII are sequentially arranged between the liquid outlet of the filter II and the water inlet of the electrodialysis device IV for purifying monovalent ions along the material flow direction, or the heating device II, the decarburization tower II and the cooling device VIII are sequentially arranged along the material flow direction.

35. The system of claim 17, 18, 19, 21, 22 or 29, further comprising an alkali addition device ii or a heating device ii; or the outlet of the alkali adding device II is connected to the water inlet of the crystallizer II, or a buffer tank is used at the connecting position.

36. The system according to claim 1, 2, 3, 4, 6, 7, 8, 12, 13, 14, 15, 17, 18, 19, 21, 22, 27 or 29, characterized in that the resin tank viii is further provided with an inlet and an outlet for regeneration liquid, the regeneration liquid outlet being connected to the water inlet of the bipolar membrane device iii, the water inlet of the crystallizer vii, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank vi or the water inlet of the volatile acid generator.

37. The system according to claim 1, 6, 7, 12, 13, 14, 15, 18, 19, 21, 22 or 29, characterized in that a neutralization tank is also provided;

the water inlet of the bipolar membrane device I is also provided with a neutralization tank, and the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

38. The system according to claim 2, 7 or 17, characterized in that a neutralization tank is also provided; the water inlet of the bipolar membrane equipment II is also provided with a neutralization tank, and the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

39. The system of claim 36, further comprising a neutralization tank; the water inlet of the bipolar membrane device III is also provided with a neutralization tank, and the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

40. The system according to claim 4, 6 or 8, further comprising a neutralization tank; the water inlet of the bipolar membrane equipment I is also provided with a neutralization tank, and the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

41. The system according to claim 1, 2, 3, 4, 6, 7, 8, 12, 13, 14, 15, 17, 18, 19, 21, 22, 27 or 29, characterized in that a neutralization tank is also provided;

a neutralization tank is arranged in front of the water inlet of the electrolysis device;

the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

42. The system according to claim 1, 2, 12, 13, 14, 15, 27, 28 or 29, characterized in that a neutralization tank is also provided; a neutralization tank is arranged in front of the medicine adding port of the mixing tank V; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

43. The system according to claim 1, 2, 3, 6, 7, 12, 13, 14, 15, 17, 18, 19, 21, 22, 27 or 29, characterized in that a neutralization tank is also provided; a neutralization tank is arranged in front of the water inlet of the crystallizer II; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

44. The system of claim 2, further comprising a neutralization tank; a neutralization tank is arranged in front of the water inlet of the crystallizer III; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

45. A system according to claim 3, further comprising a neutralization tank; a neutralization tank is arranged in front of the water inlet of the crystallizer IV; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

46. The system according to claim 2 or 27, wherein a neutralization tank is further provided; a neutralization tank is arranged in front of the water inlet of the crystallizer V; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

47. The system of claim 27, further comprising a neutralization tank; a neutralization tank is arranged in front of the water inlet of the crystallizer VI; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

48. The system of claim 36, further comprising a neutralization tank; a neutralization tank is arranged in front of the water inlet of the crystallizer VII; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

49. The system of claim 30, further comprising a neutralization tank; a neutralization tank is further arranged in front of the water inlet of the crystallizer VIII; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

50. The system of claim 28, further comprising a neutralization tank; a neutralization tank is arranged in front of the water inlet of the crystallizer X; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

51. The system of claim 4, 6, 7 or 8, further comprising a neutralization tank; a neutralization tank is arranged in front of the water inlet of the crystallizer I; the outlet of the acid adding unit and/or the outlet of the alkali adding unit III are/is connected to the water inlet of the neutralization tank.

52. The system according to claim 1 or 4, characterized in that an evaporation tank I and a filter I are arranged between the fresh water outlet of the nanofiltration unit V or the water outlet I of the electrodialysis device V for purifying monovalent ions and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the halogen generation reactor or the water inlet of the volatile acid generator in sequence; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

53. The system according to claim 18, 19, 21, 22 or 29, wherein an evaporation tank one and a filter one are further provided in sequence between the fresh water outlet of the nanofiltration unit i, the fresh water outlet of the nanofiltration unit ii, the water outlet of the electrodialysis device for purifying monovalent ions i or the water outlet of the electrodialysis device for purifying monovalent ions ii, and the water inlet of the bipolar membrane device i, the water inlet of the bipolar membrane device ii, the water inlet of the crystallizer ii, the water inlet of the electrolysis device, the water inlet of the resin tank vi, the water inlet of the resin tank viii, the water inlet of the halogen generating reactor or the water inlet of the volatile acid generator; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

54. The system according to claim 2, characterized in that an evaporation tank I and a filter I are sequentially arranged between the fresh water outlet of the nanofiltration unit III or the water outlet I of the electrodialysis device III for purifying monovalent ions and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the halogen generation reactor or the water inlet of the volatile acid generator; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

55. The system according to claim 17, wherein an evaporation tank I and a filter I are sequentially arranged between the fresh water outlet of the nanofiltration unit IV or the water outlet I of the electrodialysis device IV for purifying monovalent ions and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the halogen generation reactor or the water inlet of the volatile acid generator; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

56. The system according to claim 2 or 17, wherein an evaporation tank one and a filter one are sequentially provided between the liquid outlet of the filter ii and the water inlet of the bipolar membrane device i, the water inlet of the bipolar membrane device ii, the water inlet of the crystallizer ii, the water inlet of the electrolysis device, the water inlet of the resin tank vi, the water inlet of the resin tank viii, the water inlet of the halogen generating reactor or the water inlet of the volatile acid generator; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

57. The system according to claim 2, wherein an evaporation tank I and a filter I are sequentially arranged between the liquid outlet of the filter III and the water inlet of the bipolar membrane device I, the water inlet of the bipolar membrane device II, the water inlet of the crystallizer II, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII, the water inlet of the halogen generation reactor or the water inlet of the volatile acid generator; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

58. The system according to claim 18, 19, 21, 22 or 29, characterized in that between the liquid outlet of the filter x or the liquid outlet of the filter ix and the water inlet of the bipolar membrane device i, the water inlet of the bipolar membrane device ii, the water inlet of the crystallizer ii, the water inlet of the electrolysis device, the water inlet of the resin tank vi, the water inlet of the resin tank viii, the water inlet of the halogen generating reactor or the water inlet of the volatile acid generator, there is further provided an evaporation tank one, a filter one in sequence; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

59. The system of claim 4, wherein the system further comprises a controller configured to control the controller,

an evaporation tank I and a filter I are arranged in front of the water inlet of the bipolar membrane equipment I in sequence; or an evaporation tank I, a cooling device I and a filter I are sequentially arranged; or a first cooling device and a first filter are sequentially arranged.

60. The system according to claim 1, characterized in that hardness removal means are provided;

the hardness removing device is arranged at any position between the liquid outlet of the filter I and the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the outlet of the cooling device I and the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the oxidation reaction system, the water inlet of the halogen generating reactor or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position from the washing liquid outlet of the esterification reactor to the oxidation reaction system, the water inlet of the bipolar membrane device I, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

Or the hardness removing device is arranged at any position between the washing liquid outlet of the washing tank I and the oxidation reaction system, the water inlet of the bipolar membrane device I, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the water inlet of the combustion unit I to the bipolar membrane equipment I, the water inlet of the crystallizer II, the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the water inlet of the combustion unit II to the bipolar membrane equipment I, the water inlet of the crystallizer II, the water inlet of the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator.

61. A system according to claim 3, wherein hardness removal means are provided;

The hardness removing device is arranged at any position between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane device I, the water inlet of the crystallizer II, the oxidation reaction system, the water inlet of the halogen generating reactor, the water inlet of the electrolysis device, the water inlet of the resin tank VI, the water inlet of the resin tank VIII or the water inlet of the volatile acid generator.

62. A system according to claim 2, characterized in that hardness removal means are provided;

the hardness removing device is arranged at any position from the water solution discharge pipeline to the water inlet of the crystallizer II, the water inlet of the crystallizer III, the water inlet of the crystallizer V, the water inlet of the halogen generating reactor, the water inlet of the bipolar membrane equipment II, the water inlet of the electrolysis device, the water inlet of the resin tank VIII, the water inlet of the resin tank VI or the water inlet of the volatile acid generator;

or the hardness removing device is arranged at any position between the water solution discharge pipeline and the mixing tank V.

63. The system according to claim 36, wherein hardness removal means are provided;

The hardness removing device is arranged at any position between the liquid outlet of the filter I and the water inlet of the bipolar membrane device III;

or the hardness removing device is arranged at any position between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane device III;

or the hardness removing device is arranged at any position between the outlet of the cooling equipment I and the water inlet of the bipolar membrane equipment III;

or the hardness removing device is arranged at any position between the washing liquid outlet of the esterification reactor and the water inlet of the bipolar membrane equipment III;

or the hardness removing device is arranged at any position between the washing liquid outlet of the washing tank I and the water inlet of the bipolar membrane equipment III;

or the hardness removing device is arranged at any position between the combustion unit I and the water inlet of the bipolar membrane equipment III;

or the hardness removing device is arranged at any position between the combustion unit II and the water inlet of the bipolar membrane equipment III;

or the hardness removing device is arranged at any position between the water solution discharge pipeline and the water inlet of the bipolar membrane device III.

64. The system according to claim 36, wherein hardness removal means are provided;

The hardness removing device is arranged at any position between the liquid outlet of the filter I and the water inlet of the crystallizer VII;

or the hardness removing device is arranged at any position between the liquid outlet of the solid-liquid separator XII and the water inlet of the crystallizer VII;

or the hardness removing device is arranged at any position between the washing liquid outlet of the esterification reactor and the water inlet of the crystallizer VII;

or the hardness removing device is arranged at any position between the washing liquid outlet of the washing tank I and the water inlet of the crystallizer VII;

or the hardness removing device is arranged at any position between the combustion unit I and the water inlet of the crystallizer VII;

or the hardness removing device is arranged at any position between the combustion unit II and the water inlet of the crystallizer VII;

or the hardness removing device is arranged at any position between the water solution discharge pipeline and the water inlet of the crystallizer VII.

65. The system according to claim 30, wherein hardness removal means are provided;

the hardness removing device is arranged at any position between the liquid outlet of the filter I and the water inlet of the crystallizer VIII;

Or the hardness removing device is arranged at any position between the liquid outlet of the solid-liquid separator XII and the water inlet of the crystallizer VIII;

or the hardness removing device is arranged at any position between the combustion unit I and the water inlet of the crystallizer VIII;

or the hardness removing device is arranged at any position between the combustion unit II and the water inlet of the crystallizer VIII.

66. A system according to claim 4, 6 or 8, characterized in that hardness removal means are provided;

the hardness removing device is arranged at any position between the liquid outlet of the filter I and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer I;

or the hardness removing device is arranged at any position between the liquid outlet of the solid-liquid separator XII and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer I;

or the hardness removing device is arranged at any position between the outlet of the cooling equipment I and the water inlet of the bipolar membrane equipment I;

or the hardness removing device is arranged at any position between the washing liquid outlet of the esterification reactor and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer I;

Or the hardness removing device is arranged at any position between the washing liquid outlet of the washing tank I and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer I;

or the hardness removing device is arranged at any position between the combustion unit I and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer I;

or the hardness removing device is arranged at any position between the combustion unit II and the water inlet of the bipolar membrane equipment I or the water inlet of the crystallizer I.

67. The system according to claim 27, wherein hardness removal means are provided;

the hardness removing device is arranged at any position between the water solution discharge pipeline and the water inlet of the crystallizer VI.

68. The system of claim 5, wherein when the treatment system is the purification and reuse system for solid mixtures,

the extraction device I comprises: comprises an extraction tank, wherein the extraction tank is provided with an extractant inlet, a water outlet and an extractant discharge outlet; or comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extractant inlet, a water inlet and an outlet, the separation tank of the extraction equipment is provided with an inlet, a water outlet and an extractant discharge liquid outlet, and the outlet of the extraction tank is connected to the inlet of the separation tank;

Or the acidification device I: the acidification tank is provided with a water inlet, a water outlet and an acid adding pipeline, the water outlet of the acidification tank of the acidification equipment is connected to the water inlet of a sedimentation tank or a filter VII, and the filter VII is provided with a water outlet;

or the advanced oxidation unit I: the device comprises a high-grade oxidation reactor, wherein the high-grade oxidation reactor is provided with a precipitation overflow port or a water outlet and is provided with a filter screen; or comprises a high-grade oxidation reactor, a filter VIII or a sedimentation tank, wherein the high-grade oxidation reactor is provided with a water inlet and a water outlet, the water outlet of the high-grade oxidation reactor is connected to the water inlet of the filter VIII or the water inlet of the sedimentation tank, and the filter VIII or the sedimentation tank is provided with a water outlet.

69. The system of claim 9, wherein when the treatment system is the solid mixture purification and reuse system,

the extraction device II or the extraction device III: comprises an extraction tank, wherein the extraction tank is provided with an extractant inlet, a water outlet and an extractant discharge outlet; or comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extractant inlet, an extractant inlet and an extractant outlet, the separation tank of the extraction device II or the extraction device III is provided with an inlet, a water outlet and an extractant discharge outlet, and the outlet of the extraction tank is connected to the inlet of the separation tank;

Or said acidification device ii or said acidification device iii: the device comprises an acidification tank, wherein the acidification tank is provided with a water inlet, a water outlet and an acid adding pipeline, the water outlet of the acidification tank of the acidification device II or the acidification device III is connected to the water inlet of a sedimentation tank or a filter VII, and the filter VII is provided with a water outlet;

or said advanced oxidation unit ii or said advanced oxidation unit iii: the device comprises a high-grade oxidation reactor, wherein the high-grade oxidation reactor is provided with a precipitation overflow port or a water outlet and is provided with a filter screen; or comprises a high-grade oxidation reactor, a filter VIII or a sedimentation tank, wherein the high-grade oxidation reactor is provided with a water inlet and a water outlet, the water outlet of the high-grade oxidation reactor is connected to the water inlet of the filter VIII or the water inlet of the sedimentation tank, and the filter VIII or the sedimentation tank is provided with a water outlet.

70. The system of claim 10, wherein when the treatment system is the solid mixture purification and reuse system,

the extraction device V: comprises an extraction tank, wherein the extraction tank is provided with an extractant inlet, a water outlet and an extractant discharge outlet; or comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extractant inlet, an extractant inlet and an extractant outlet, the separation tank of the extraction device V is provided with an inlet, a water outlet and an extractant discharge liquid outlet, and the outlet of the extraction tank is connected to the inlet of the separation tank;

Or the acidifying device V: the acidification tank is provided with a water inlet, a water outlet and an acid adding pipeline, the water outlet of the acidification tank of the acidification device V is connected to the water inlet of a sedimentation tank or a filter VII, and the filter VII is provided with a water outlet;

or the advanced oxidation unit v: the device comprises a high-grade oxidation reactor, wherein the high-grade oxidation reactor is provided with a precipitation overflow port or a water outlet and is provided with a filter screen; or comprises a high-grade oxidation reactor, a filter VIII or a sedimentation tank, wherein the high-grade oxidation reactor is provided with a water inlet and a water outlet, the water outlet of the high-grade oxidation reactor is connected to the water inlet of the filter VIII or the water inlet of the sedimentation tank, and the filter VIII or the sedimentation tank is provided with a water outlet.

71. The system of claim 11, wherein when the treatment system is the solid mixture purification and reuse system,

the extraction device IV: comprises an extraction tank, wherein the extraction tank is provided with an extractant inlet, a water outlet and an extractant discharge outlet; or comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extractant inlet, an extractant inlet and an extractant outlet, the separation tank of the extraction device IV is provided with an inlet, a water outlet and an extractant discharge liquid outlet, and the outlet of the extraction tank is connected to the inlet of the separation tank;

Or the acidification device IV: the acidification tank is provided with a water inlet, a water outlet and an acid adding pipeline, the water outlet of the acidification tank of the acidification device IV is connected to the water inlet of a sedimentation tank or a filter VII, and the filter VII is provided with a water outlet;

or the advanced oxidation unit IV: the device comprises a high-grade oxidation reactor, wherein the high-grade oxidation reactor is provided with a precipitation overflow port or a water outlet and is provided with a filter screen; or comprises a high-grade oxidation reactor, a filter VIII or a sedimentation tank, wherein the high-grade oxidation reactor is provided with a water inlet and a water outlet, the water outlet of the high-grade oxidation reactor is connected to the water inlet of the filter VIII or the water inlet of the sedimentation tank, and the filter VIII or the sedimentation tank is provided with a water outlet.

72. The system of claim 1, 2, 3, 4 or 17, wherein,

the exhaust port of the halogen generation reactor is connected to the gas inlet of the absorption tank; or the exhaust port of the halogen generating reactor is connected to the inlet of the condenser; or the discharge port of the halogen generating reactor is connected to the inlet of a layering tank, the bromine outlet of the layering tank is collected or the bromine outlet of the layering tank is connected to the inlet of an absorption tank;

Or the electrolysis device comprises an electrolysis anode plate and an electrolysis cathode plate, and an exhaust port of the electrolysis device is connected to an air inlet of the absorption tank; or the exhaust port of the electrolysis device is connected to the inlet of the condenser; or the discharge port of the electrolysis device is connected to the inlet of the layering tank, and the bromine outlet of the layering tank is collected or connected to the inlet of the absorption tank;

or the volatile acid generator is provided with an acid inlet pipeline and an air outlet; or the volatile acid generator is provided with an acid inlet pipeline, an exhaust port, an air inlet and/or a heater.

73. A system according to claim 1, 2 or 3, characterized in that the solid outlet of the crystallizer ii is connected to the solid inlet of a mixing dissolution tank, which also has a liquid inlet, the outlet of which is connected to the water inlet of the bipolar membrane device iv.

74. The system according to claim 36, characterized in that the solid outlet of the crystallizer vii is connected to the solid inlet of a mixing dissolution tank, which also has a liquid inlet, the outlet of which is connected to the water inlet of the bipolar membrane device iv.

75. The system of claim 4, wherein the solid outlet of the first crystallizer is connected to the solid inlet of a mixing and dissolving tank, the mixing and dissolving tank further having a liquid inlet, and the outlet of the mixing and dissolving tank is connected to the water inlet of the bipolar membrane apparatus iv.

76. The system of claim 1, 2, 3, 4, 6, 7, 8, 12, 13, 14, 15, 17, 18, 19, 21, 22, 27, or 29, wherein the acid generator tank of the halogen generating reactor is connected to an oxidation reaction system; or the acid-producing tank of the electrolysis device is connected to an oxidation reaction system; or the water outlet of the resin tank VI is connected to an oxidation reaction system; or the regenerated liquid outlet of the resin tank IV is connected to an oxidation reaction system; or the acid generating tank of the volatile acid generator is connected to an oxidation reaction system.

77. The system of claim 1, 6, 7, 12, 13, 14, 15, 18, 19, 21, 22 or 29, wherein the acid generator tank of bipolar membrane device i is connected to an oxidation reaction system.

78. The system of claim 2, 17 or 27, wherein the acid generator tank of bipolar membrane device ii is connected to an oxidation reaction system.

79. The system of claim 36, wherein the acid generator tank of bipolar membrane apparatus iii is connected to an oxidation reaction system.

80. The system of claim 4, 6 or 8, wherein the acid generator tank of the bipolar membrane device one is connected to an oxidation reaction system.

81. The system according to claim 1, 12, 13, 14, 15 or 29, characterized in that the regeneration liquid outlet of the resin tank v is connected to an oxidation reaction system; or the solid outlet of the filter V is connected to an oxidation reaction system; or the solid outlet of the filter V is connected to a tempering tank, the tempering tank is also provided with an acid inlet, and the outlet of the tempering tank is connected to an oxidation reaction system.

82. The system of any one of claims 23, 24, 25 or 26, wherein the solids outlet of the filter iv is connected to an oxidation reaction system; or the solid outlet of the filter IV is connected to a blending tank, the blending tank is also provided with an acid inlet, and the outlet of the blending tank is connected to an oxidation reaction system.

83. The system of claim 73, wherein the acid generator tank of bipolar membrane apparatus iv is connected to an oxidation reaction system.

84. The system of claim 74, wherein the acid generator tank of bipolar membrane apparatus iv is connected to an oxidation reaction system.

85. The system of claim 75, wherein the acid generator tank of bipolar membrane apparatus iv is connected to an oxidation reaction system.

86. The system of claim 1, wherein the crystallizer i or the crystallizer ii is a heated evaporative crystallizer.

87. The system according to claim 1, 2, 12, 13, 14 or 15, characterized in that the solid outlet of the crystallizer iii, the solid outlet of the crystallizer V, the solid outlet of the crystallizer vi, the solid outlet of the crystallizer x, the solid outlet of the crystallizer viii, the solid outlet of the crystallizer one, the solid outlet of the filter ii, the solid outlet of the filter iii, the solid outlet of the filter ix, the water outlet of the halogen generating reactor, the water outlet of the electrolysis device or the water outlet of the resin tank viii is connected to a mixing tank V.

88. The system of claim 1, wherein the combustion device i is replaced by a catalytic organic decomposition device i.

89. The system of claim 16, wherein the combustion device ii is replaced with a catalytic organic decomposition device ii.

90. The system of claim 16, wherein the combustion apparatus iii is replaced with a catalytic decomposition organic apparatus iii.

91. The system according to claim 1, characterized in that between the electrodialysis device v for purifying monovalent ions and the preceding device in the direction of flow of the material there is also provided a dilution tank and/or a preheater, the dilution tank also being provided with a liquid inlet.

92. The system according to claim 2, 17 or 28, characterized in that the evaporation tank i is replaced by an electrodialysis concentration device a or a reverse osmosis concentration device a.

93. The system of claim 18, 19, 21, 22 or 29, wherein the evaporation tank ii is replaced by an electrodialysis concentration device b or a reverse osmosis concentration device b.

94. The system of claim 1, 12, 13, 14, 15, 18, 19, 21, 22 or 29, wherein the evaporation tank is replaced with an electrodialysis concentration device or a reverse osmosis concentration device.

95. System according to claim 1, characterized in that a concentrating device and/or a cooling device ix are provided.

96. The system of claim 1, wherein the cooling device i or the cooling device i comprises at least one of a heat exchanger, a jacket cooler, a tube array cooler, a vacuum cooler, a cooling tank with an out-of-band circulation cooler, and a mixed cooling medium type cooling tank.