CN217230452U

CN217230452U - Processing system for mixed solution containing benzene series and bromine

Info

Publication number: CN217230452U
Application number: CN202123188174.XU
Authority: CN
Inventors: 李玉宽
Original assignee: Best Tech Water Treatment Environmental Technology Dalian Co ltd
Current assignee: Dalian Huaxing Honghai Environmental Protection Technology Co ltd
Priority date: 2021-12-17
Filing date: 2021-12-17
Publication date: 2022-08-19
Anticipated expiration: 2031-12-17

Abstract

The utility model discloses a to containing benzene series thing and bromine element's mixed solution's processing system, benzene series thing, bromine element in to mixed solution through this system draw out, have reduced the concentration of benzene series thing, bromine element in mixed solution, have just also reduced the adverse effect that benzene series thing and bromine element in this mixed solution caused sewage treatment, turn into hydrobromic acid material with bromine simultaneously and retrieve, kill two birds with one stone.

Description

Processing system for mixed solution containing benzene series and bromine

Technical Field

The utility model belongs to the technical field of the processing of mixed solution, concretely relates to contain benzene series thing and bromine element's mixed solution's processing system.

Background

For the mixed solution containing the benzene series and the bromine, the biochemical performance of the benzene series is poor and COD contributed by the benzene series is not easily degraded by biochemistry for sewage treatment; meanwhile, bromine also has negative influence on biochemical treatment to inhibit the activity of biochemical flora and interfere with the increase of COD analysis results, so that the biochemical treatment of sewage containing benzene series and bromine is difficult.

If a system (equipment) can be provided, the system (equipment) is used for treating the mixed solution containing the benzene series and the bromine, so that the concentration of the benzene series and the bromine in the mixed solution is reduced, the adverse effect of the benzene series and the bromine in the mixed solution on sewage treatment is reduced, and the sewage treatment can reach the standard more easily; at the same time, bromine is valuable, and if the value of the bromine can be recovered, the bromine has larger significance and better effect.

For example, the sewage in the terephthalic acid industry often contains benzene series (mainly, the benzene series is benzoic acid, phthalic acid (mainly, terephthalic acid), p-toluic acid, p-carboxybenzaldehyde, etc.) and bromine, and is suitable for being treated by the system, so as to reduce the concentrations of the benzene series and the bromine in the mixed solution (also called as the sewage), and simultaneously convert the bromine in the mixed solution into a hydrobromic acid form, and recover the bromine (note that one of the catalysts of the oxidation reaction in the oxidation process of the terephthalic acid plant is the bromine and the hydrobromic acid form, if the bromine extracted from the mixed solution (also called as the sewage) can be converted into the hydrobromic acid by the utility model, the purchase amount of the hydrobromic acid in the plant can be reduced, and the operation cost can be reduced).

SUMMERY OF THE UTILITY MODEL

The utility model discloses a to containing benzene series thing and bromine element's mixed solution's processing system, through this system benzene series thing and bromine element in to mixed solution draw out, reduced benzene series thing, bromine element concentration in mixed solution, just also reduced the adverse effect that benzene series thing, bromine element in this mixed solution caused sewage treatment, turn into hydrobromic acid material with bromine element simultaneously and retrieve, kill two birds with one stone.

A treatment system for a mixed solution containing benzene series and bromine elements comprises a bromine element absorption device, a regeneration unit I, a debenzolization unit I or a debenzolization unit II:

the benzene removal unit I is provided with a water inlet and a water outlet, the mixed solution containing the benzene and the bromine enters the water inlet of the benzene removal unit I, the water outlet of the benzene removal unit I is connected to the water inlet of the bromine absorption equipment, and the water outlet of the bromine absorption equipment is discharged out of the system; an outlet of the regeneration unit I is connected to a regeneration liquid inlet of the bromine element absorption equipment, and a regeneration liquid outlet of the bromine element absorption equipment is connected to a circulation regeneration tank I or a regeneration liquid collection tank I of the regeneration unit I (the regeneration unit I is provided with the circulation regeneration tank I or the regeneration liquid collection tank I);

the benzene removal unit I is used for removing part or all of benzene in the mixed solution containing the benzene and bromine to reduce the concentration of the benzene in the mixed solution containing the benzene and bromine and reduce the pollution or load influence on the bromine absorption equipment at the later stage;

for example, an aqueous solution (mainly containing benzene series including phthalic acid and acid groups thereof, benzoic acid and acid groups thereof, p-toluic acid and acid groups thereof, p-carboxybenzaldehyde and acid groups thereof, and ions such as cobalt, manganese, bromine, sodium, iron, chromium, and nickel, hereinafter referred to as an aqueous solution i) obtained by filtering the oxidation residue of the oxidation step of the terephthalic acid production apparatus with water and removing iron ions (hereinafter referred to as an aqueous solution ii), or an aqueous solution (hereinafter referred to as an aqueous solution iii) obtained by adding water and removing iron, cobalt, and manganese ions from the oxidation residue of the oxidation step of the terephthalic acid production apparatus:

the aqueous solution (namely the aqueous solution II) obtained by adding water to the oxidation residue in the oxidation process of the terephthalic acid production device and removing iron ions is a residual aqueous solution (mainly containing benzene series including phthalic acid, benzoic acid, p-toluic acid, p-carboxybenzaldehyde, cobalt, manganese, bromine, sodium and the like ions) obtained by adding water to the oxidation residue and adding alkaline substances (sodium hydroxide, sodium carbonate, sodium bicarbonate and the like) to raise the pH to 4-6.5 and filtering the residual aqueous solution;

the aqueous solution (i.e. the aqueous solution III) obtained by adding water to the oxidation residue in the oxidation process of the terephthalic acid production device and removing iron, cobalt and manganese ions is obtained by adding water to the oxidation residue and adding alkaline substances (sodium hydroxide, sodium carbonate, sodium bicarbonate and the like) to raise the pH to be more than 8.5, wherein iron, chromium, nickel, cobalt, manganese and the like form solid insoluble substances, and the residual aqueous solution (mainly containing benzene series including phthalic acid, benzoic acid, p-toluic acid, p-carboxybenzaldehyde, bromine, sodium and the like) obtained after filtration is prepared by the following steps: the iron, chromium, nickel, cobalt and manganese ions can also be removed step by step, the PH value is firstly raised to 4-6.5, the iron, chromium and nickel ions form solid insoluble substances, the solid insoluble substances are removed by filtration, the PH value of the aqueous solution is raised to more than 8.5, the cobalt, manganese and other ions form solid insoluble substances, and the solid insoluble substances are removed by filtration; or the water solution (namely the water solution III) obtained by adding water to the oxidation residue in the oxidation process of the terephthalic acid production device and removing iron, cobalt and manganese ions is the water solution left after the water solution obtained by adding water to the oxidation residue and filtering is subjected to cobalt-manganese adsorption resin to adsorb the cobalt, manganese and other cation ions in the water solution;

after the benzene series contained in the mixed solution containing the benzene series and the bromine passes through the benzene series removing unit I, the concentration of the benzene series in the aqueous solution is reduced;

or the bromine element absorption equipment is provided with a water inlet and a water outlet, the mixed solution containing the benzene series and the bromine element enters the water inlet of the bromine element absorption equipment, and the water outlet of the bromine element absorption equipment is discharged out of the system; an outlet of the debenzolization unit II is connected to a solvent inlet of the bromine element absorption equipment, and a solvent outlet of the bromine element absorption equipment is connected to a circulating solvent tank or a solvent recovery tank of the debenzolization unit II (the debenzolization unit II is provided with a circulating solvent tank or a solvent recovery tank); an outlet of the regeneration unit I is connected to a regeneration liquid inlet of the bromine element absorption equipment, and a regeneration liquid outlet of the bromine element absorption equipment is connected to a circulation regeneration tank I or a regeneration liquid collection tank I of the regeneration unit I (the regeneration unit I is provided with the circulation regeneration tank I or the regeneration liquid collection tank I);

the reason for designing the debenzolization unit II is as follows: when the mixed solution containing the benzene series and the bromine passes through the bromine element absorption equipment, the bromine element is partially absorbed by the bromine element absorption equipment, and meanwhile, the benzene series in the mixed solution containing the benzene series and the bromine element is partially absorbed by the bromine element absorption equipment, so that the regenerated liquid rich in bromine obtained in the regeneration process of the regeneration unit I on the bromine element absorption equipment also contains the benzene series (which is impurities), so that the benzene series adsorbed on the bromine element absorption equipment is dissolved and washed away by the benzene series removal unit II, and the concentration of the benzene series contained in the regenerated liquid rich in bromine obtained by the regeneration of the regeneration unit I on the bromine element absorption equipment is reduced; the purpose of the debenzolization unit II is to dissolve and wash a part of the benzene series adsorbed on the bromine element absorption equipment, the debenzolization unit II is not to reduce the benzene series in the debenzolization unit II, but the debenzolization unit II is to provide a solvent for the bromine element absorption equipment, and the solvent provided by the debenzolization unit II is used for dissolving the benzene series adsorbed on the bromine element absorption equipment in the bromine element absorption equipment;

for example, when the mixed solution containing the benzene series and the bromine passes through the bromine absorption device, besides the bromine, phthalic acid and acid radicals thereof, benzoic acid and acid radicals thereof, p-toluic acid and acid radicals thereof, and p-carboxybenzaldehyde and acid radicals thereof are adsorbed, a part of the benzene series on the bromine absorption device is dissolved out into the solvent by the solvent of the benzene series removal unit ii, the solvent is discharged from a solvent outlet of the bromine absorption device (the inside of the bromine absorption device is emptied first), and then the benzene series concentration in the regenerated solution rich in bromine, which is regenerated by the bromine absorption device by the regeneration unit i, is reduced;

the debenzolization unit ii can be circularly dissolved (the solvent refers to the dissolution of the benzene series adsorbed on the bromine absorption equipment), for example, the solvent is pumped from a circulating solvent tank of the debenzolization unit ii to a solvent inlet of the bromine absorption equipment, a solvent outlet of the bromine absorption equipment is connected to an inlet of a circulating solvent tank of the debenzolization unit ii, so as to form a circulation for circularly dissolving the bromine absorption equipment (the solvent refers to the dissolution of the benzene series adsorbed on the bromine absorption equipment); the solvent can also be used for one time, namely the solvent is pumped from the outlet of the debenzolization unit II to the solvent inlet of the bromine absorption device, the solvent outlet of the bromine absorption device is connected to the inlet of the solvent recovery tank of the debenzolization unit II, and the bromine absorption device always receives the fresh solvent provided from the outlet of the debenzolization unit II;

the regeneration unit I provides regeneration liquid, provides the regeneration liquid for the bromine element absorption equipment, and regenerates bromine adsorbed on the bromine element absorption equipment into the regeneration liquid, wherein the regeneration process can be a cyclic regeneration mode or a disposable regeneration mode; the regeneration unit I is used for regenerating bromine adsorbed on the bromine absorption equipment into a regeneration liquid, the regeneration unit I does not perform regeneration in the regeneration unit I, but provides the regeneration liquid for the bromine absorption equipment, and the regeneration liquid provided by the regeneration unit I is used for regenerating the bromine adsorbed on the bromine absorption equipment into the regeneration liquid in the bromine absorption equipment;

the regeneration unit I can be recycled, for example, a regeneration liquid is pumped from a recycling regeneration tank I of the regeneration unit I to a regeneration liquid inlet of the bromine element absorption equipment, and a regeneration liquid outlet of the bromine element absorption equipment is connected to an inlet of the recycling regeneration tank I, so that the bromine element absorption equipment is regenerated by the circulation; the regenerated liquid can also be used for one time, namely the regenerated liquid is pumped from an outlet of the regeneration unit I to a regenerated liquid inlet of the bromine absorption device, a regenerated liquid outlet of the bromine absorption device is connected to an inlet of a regenerated liquid collecting tank I of the regeneration unit I, and the bromine absorption device always receives fresh regenerated liquid provided from the outlet of the regeneration unit I.

Based on the above treatment system, preferably, the debenzolization unit ii comprises at least one of a circulating solvent tank, a fresh solvent pressurized supplementary pipeline and a solvent buffer tank, or the debenzolization unit ii further comprises a solvent recovery tank. When the benzene removal unit II is the circulating solvent tank, the outlet of the benzene removal unit II is the outlet of the circulating solvent tank (including the solvent in the circulating solvent tank conveyed by the solvent pump, the outlet of the solvent pump), and the inlet of the benzene removal unit II is the inlet of the circulating solvent tank (for solvent supplement, such as fresh solvent supplement); or when the benzene removal unit II is the fresh solvent pressurized supplementary pipeline, the outlet of the benzene removal unit II is the outlet of the fresh solvent pressurized supplementary pipeline, and the inlet of the benzene removal unit II is the inlet of the fresh solvent pressurized supplementary pipeline; or when the benzene removal unit II is a solvent buffer tank, the outlet of the benzene removal unit II is the outlet of the solvent buffer tank (including the solvent in the solvent buffer tank conveyed by a pump, and the outlet of the pump), and the inlet of the benzene removal unit II is the inlet of the solvent buffer tank (for solvent supplement, such as fresh solvent supplement).

Based on above processing system, it is preferred that regeneration unit I includes circulation regeneration jar I, fresh regeneration liquid area and presses at least one in supplementary pipeline, I buffer tank of regeneration unit, the I blending tank of regeneration unit, or regeneration unit I still includes regeneration liquid collecting tank I. When the regeneration unit I is the circulation regeneration tank I, the outlet of the regeneration unit I is the outlet of the circulation regeneration tank I (the regeneration liquid in the circulation regeneration tank I is conveyed by the regeneration pump I, the outlet of the regeneration pump I) and the inlet of the regeneration unit I is the inlet of the circulation regeneration tank I (the regeneration liquid is supplemented); or when the regeneration unit I is the fresh regeneration liquid pressurized supplement pipeline, the outlet of the regeneration unit I is the outlet of the fresh regeneration liquid pressurized supplement pipeline, and the inlet of the regeneration unit I is the inlet of the fresh regeneration liquid pressurized supplement pipeline; or when the regeneration unit I is a regeneration unit I buffer tank, the outlet of the regeneration unit I is the outlet of the regeneration unit I buffer tank (including the outlet of a pump for conveying the regeneration liquid in the regeneration unit I buffer tank), and the inlet of the regeneration unit I is the inlet of the regeneration unit I buffer tank (replenishing the regeneration liquid); or when regeneration unit I is regeneration unit I blending tank, regeneration unit I's export does regeneration unit I's export (contain regeneration liquid in the regeneration unit I blending tank is carried with the pump, the export of this pump), regeneration unit I's import is the import of regeneration unit I blending tank (the import make-up water and the regeneration liquid of high concentration (or the solid form of the material that regeneration liquid contains of regeneration liquid of regeneration unit I blending tank) for the regeneration liquid of the required concentration of mixing.

Based on the above treatment system, preferably, the bromine element absorption equipment includes an absorption tower, an absorption tank, a resin tank, or the like, and the absorption tower, the absorption tank, or the resin tank is filled with a resin having an adsorption capacity for bromine to adsorb bromine elements (including bromide ions).

Based on the above treatment system, it is preferable that the solvent used in the debenzolization unit II is a solvent capable of dissolving part or all of the benzene compound in the solvent;

based on the above treatment system, the solvent of the debenzolization unit II preferably includes organic acids, alcohols, ethers, aromatic compounds, esters, and the like.

Based on the above treatment system, preferably, the solvent types of the debenzolization unit II comprise: water-containing small molecular carboxylic acid with the content of more than 40 percent, anhydrous small molecular carboxylic acid, water-containing methanol with the methanol content of more than 40 percent, anhydrous methanol, water-containing ethanol or anhydrous ethanol with the ethanol content of more than 40 percent, benzene and the like.

Based on the above treatment system, it is preferable that the regeneration liquid of the regeneration unit I is selected from basic substances such as hydroxide, carbonate, bicarbonate, etc.

Based on the above treatment system, it is preferable that the cation of the hydroxide, carbonate or bicarbonate is potassium ion, sodium ion, or the like.

Based on the above treatment system, preferably, the debenzolization unit i is: benzene series absorption equipment, extraction equipment or acidification equipment; the benzene removal unit I is used for removing a part of the benzene in the mixed solution containing the benzene and the bromine during the process of passing through the benzene removal unit I and reducing the concentration of the benzene before entering the subsequent bromine adsorption equipment;

the benzene series absorption equipment comprises an absorption tower, an absorption tank or a resin tank and the like, wherein the absorption tower, the absorption tank or the resin tank is filled with resin with adsorption capacity on benzene series, and the benzene series substances (including ions of the benzene series) in the solution are adsorbed to reduce the concentration of the benzene series in the mixed solution;

the extraction equipment is conventional extraction equipment and comprises an extraction tank or an extraction tank and a separation tank, wherein an extracting agent is used for extracting part or all of benzene series in the mixed solution containing the benzene series and bromine (namely, part or all of the benzene series is dissolved in the extracting agent), the extracting agent is insoluble in water, and the obtained extracting agent discharge liquid (consisting of the extracting agent and the extracted benzene series) of the extraction equipment is insoluble in water and is separated from the mixed solution (aqueous solution) in a layering manner; and the mixed solution containing the benzene series and the bromine is extracted and then enters the bromine absorption equipment for treatment.

The acidification device is a conventional acidification device, namely, acid is added into the mixed solution containing the benzene series and the bromine element, the solubility of the benzene series in the mixed solution (aqueous solution) is reduced to separate out the benzene series (a sedimentation tank I or a filtering device I is designed between the acidification device and the bromine element absorption device to remove solid), and the mixed solution containing the benzene series and the bromine element enters the bromine element absorption device for treatment after being acidified and the solid is removed (the solid is the benzene series).

Based on the above treatment system, it is preferable that the kind of the extractant includes an extractant that can dissolve benzene series.

Based on the above treatment system, preferably, the extraction agent contains aromatic compounds, esters, or the like.

Based on the above treatment system, preferably, the aromatic compound contains benzene or the like.

Based on the above treatment system, preferably, the acidification device is used for adding acid into the mixed solution containing the benzene series and the bromine.

Based on the above treatment system, it is preferable that the acidification device comprises an acidification tank or the like (control of PH to control the amount of acid added).

Based on the above treatment system, it is preferable that the acidification tank is further connected with an acid addition pump or an acid addition pipeline, and the like, and the acid addition pump or the acid addition pipeline is connected to the acidification tank.

Based on the above treatment system, preferably, the acid used in the acidification device is acetic acid, hydrobromic acid, or the like.

Based on the treatment system, preferably, a bipolar membrane electrodialysis device is further arranged, and a liquid outlet of the circulation regeneration tank I or the regeneration liquid collecting tank I is connected to a water inlet of the bipolar membrane electrodialysis device;

the bipolar membrane electrodialysis device utilizes a bipolar membrane to electrolyze water into hydrogen ions and hydroxyl ions under the action of a direct current electric field, and can convert concentrated brine into acid and alkali and convert cations in the brine into hydroxides corresponding to the cations, namely alkali by means of ingenious combination of the bipolar membrane, an anode membrane and a cathode membrane; converting the anion in the brine to the hydride, i.e., the acid, to which the anion corresponds; meanwhile, the anions and cations in the concentrated saline are converted into corresponding alkali and acid concentrations, and the corresponding alkali and acid concentrations are reduced, so that the dilute saline is called;

the bipolar membrane electrodialysis device (see the attached figures 4 and 5 for details): the bipolar membrane electrodialysis is a device capable of decomposing salts in source water to obtain corresponding acids and bases (cations in salts in source water are converted into corresponding bases, anions in salts in source water are converted into corresponding acids, for example, the salts in source water contain sodium bromide, so that the bases obtained by conversion are sodium hydroxide corresponding to sodium ions, and the acids obtained by conversion are hydrobromic acid corresponding to bromide ions). Firstly, the bipolar membrane can electrolyze water into hydrogen ions and hydroxyl ions, the bipolar membrane, the negative membrane and the positive membrane are sequentially arranged to form a plurality of alternate membrane stacks, under the action of a direct current electric field, for all ions, cations migrate to a negative electrode and anions migrate to a positive electrode, the cations in the salt losing chamber move to the negative electrode and penetrate through the positive membrane to enter the alkali chamber, and the anions in the salt losing chamber move to the positive electrode and penetrate through the negative membrane to enter the acid chamber, so the ions in the salt losing chamber are lost all the time. And hydroxide ions generated by the bipolar membrane electrolyzed water move to the positive electrode and enter the alkali chamber (form alkali with cations from the salt losing chamber), hydrogen ions generated by the bipolar membrane electrolyzed water move to the negative electrode and enter the acid chamber (form acid with anions from the salt losing chamber), and the acid concentration of the acid chamber is gradually increased and the alkali concentration of the alkali chamber is also gradually increased because the direct current electric field is always present. Please refer to fig. 4 and 5 for the specific principle.

Based on the above processing system, preferably, a concentration device is also provided,

a liquid outlet of the circulating regeneration tank I is connected to a water inlet of the concentration device, and a concentrated solution water outlet of the concentration device is connected to a water inlet of the bipolar membrane electrodialysis equipment;

or the liquid outlet of the regeneration liquid collecting tank I is connected to the water inlet of the concentration device, and the concentrated liquid outlet of the concentration device is connected to the water inlet of the bipolar membrane electrodialysis equipment.

Based on the above treatment system, preferably, a filtering device ii or a sedimentation tank ii is further arranged in front of the water inlet of the bipolar membrane electrodialysis device, specifically:

when the liquid outlet of the circulation regeneration tank I or the regeneration liquid collecting tank I is connected to the water inlet of the bipolar membrane electrodialysis equipment, the filtering device II or the sedimentation tank II is arranged between the liquid outlet of the circulation regeneration tank I or the regeneration liquid collecting tank I and the water inlet of the bipolar membrane electrodialysis equipment;

when the liquid outlet of the cyclic regeneration tank I or the regenerated liquid collecting tank I is connected to the water inlet of the concentrating device, and the concentrated liquid outlet of the concentrating device is connected to the water inlet of the bipolar membrane electrodialysis equipment, the filtering device II or the sedimentation tank II is arranged between the concentrated liquid outlet of the concentrating device and the water inlet of the bipolar membrane electrodialysis equipment.

Based on the above treatment system, preferably, the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the concentration device, and the dilute brine of the bipolar membrane electrodialysis device is concentrated again and enters the bipolar membrane electrodialysis device for treatment again, so that bromine in the dilute brine of the bipolar membrane electrodialysis device is not wasted (the dilute brine outlet of the bipolar membrane electrodialysis device is preferably the dilute brine tank water outlet of the bipolar membrane electrodialysis device or the dilute brine pump water outlet arranged on the dilute brine tank of the bipolar membrane electrodialysis device).

Based on the above treatment system, preferably, the acid production tank outlet of the bipolar membrane electrodialysis device is collected and recycled;

based on the above treatment system, it is preferable that the acid production tank of the bipolar membrane electrodialysis apparatus is designed with a heating device (for example, heated to a boiling temperature of 20 ℃ to the hydrobromic acid concentration) and/or an air blowing device, when a small amount of chlorine is mixed in the mixed solution containing the benzene series and the bromine, the chlorine is also adsorbed on the bromine absorbing device along with the bromine, the bromine-rich regenerated solution obtained by regenerating the bromine absorbing device through the regeneration unit i is mainly sodium bromide and is also mixed with a small amount of sodium chloride, then the low-concentration hydrogen chloride is mixed in the hydrobromic acid obtained by the bipolar membrane electrodialysis apparatus or the concentrated hydrogen bromide treated by the bipolar membrane electrodialysis apparatus, the hydrogen chloride is more volatile than the hydrogen bromide, so the hydrogen chloride can be discharged into the gas phase through the heating device and/or the air blowing device, the concentration of hydrogen chloride impurities in the liquid-phase hydrobromic acid is reduced, and the liquid-phase hydrobromic acid is purer;

based on the above treatment system, preferably, the acid production tank of the bipolar membrane electrodialysis device is discharged to a chlorine removal tank, the chlorine removal tank is provided with a heating device (for example, heated to a boiling temperature of 20 ℃ to the hydrobromic acid concentration) and/or an air blowing device, when a small amount of chlorine is mixed in the mixed solution containing the benzene series and the bromine, the chlorine is also adsorbed on the bromine absorption device along with the bromine, the bromine-rich regenerated solution obtained by regenerating the bromine absorption device by the regeneration unit i is mainly sodium bromide and also is mixed with a small amount of sodium chloride, and then the hydrobromic acid obtained by the bipolar membrane electrodialysis device or the concentrated treatment by the bipolar membrane electrodialysis device is mixed with low-concentration hydrogen chloride which is more volatile than hydrogen bromide, so that the hydrogen chloride can be discharged to the gas phase by the heating device and/or the air blowing device, the concentration of hydrogen chloride impurities in the liquid-phase hydrobromic acid is reduced, the liquid-phase hydrobromic acid is purer, and the chlorine removal tank outlet is collected and recycled.

Based on the above treatment system, it is preferable that the concentration device includes a reverse osmosis concentration device, an electrodialysis concentration apparatus, or an evaporation concentration device;

the reverse osmosis concentration device is a concentrated solution of the concentration device, wherein reverse osmosis concentrated water is obtained after reverse osmosis treatment;

the electrodialysis device (see the attached figures 2 and 3 for details): the electrodialysis is a device capable of concentrating source water, and the structure and operation principle of one electrodialysis are listed as follows, and the electrodialysis mainly comprises electrode plates, a negative membrane, a positive membrane, a corresponding circulating system (comprising a circulating tank and a circulating pump), a power supply system, a control system and the like. The anion and cation exchange membranes have selective permeability to anions and cations in the solution. The negative and positive membranes are alternately stacked (with a partition plate between them) to form a plurality of membrane stacks with the negative and positive membranes alternately, electrodes are arranged at two ends of the membrane stacks, ions are directionally migrated under the action of a direct current electric field, the anions migrate to the positive pole, the cations migrate to the negative pole, the anions can penetrate through the negative membrane and cannot penetrate through the positive membrane, and the cations can penetrate through the positive membrane and cannot penetrate through the negative membrane in the same way. In the design, cations from the positive membrane and anions from the negative membrane can continuously enter the concentration chamber, and the cations and the anions are combined to form salt (the cations in the concentration chamber migrate to the negative electrode but cannot escape from the concentration chamber due to the obstruction of the negative membrane, and the anions in the concentration chamber migrate to the positive electrode but cannot escape from the concentration chamber due to the obstruction of the positive membrane, so that the cations and the anions in the concentration chamber can only be trapped in the concentration chamber), and the salt concentration in the concentration chamber is higher and higher due to the continuous action of the direct current electric field, so that the purpose of concentration is achieved. The specific principle refers to that with reference to fig. 2 and 3, the salt concentration of the concentration chamber is higher and higher, and the part of high-concentration brine is discharged from the electrodialysis device to be the concentrated solution of the concentration device;

the evaporation concentration device is a conventional evaporation device, such as a jacket evaporator, a coil evaporator, a heat exchanger evaporator, an evaporation reboiler, an evaporator and the like, and the concentrated solution remaining after part of water vapor is evaporated by the evaporation device is the concentrated solution of the concentration device.

Based on the above processing system, preferably, a cooling device is further provided:

a concentrated solution outlet of the evaporation concentration device is connected to a water inlet of the cooling device, and a water outlet of the cooling device is connected to a water inlet of the bipolar membrane electrodialysis equipment;

or a concentrated solution outlet of the evaporation concentration device is connected to a water inlet of the cooling device, a water outlet of the cooling device is connected to a water inlet of the filtering device II or the sedimentation tank II, and a water outlet of the filtering device II or the sedimentation tank II is connected to a water inlet of the bipolar membrane electrodialysis equipment;

or a concentrated solution outlet of the evaporation concentration device is connected to a water inlet of the filtering device II or the sedimentation tank II, a water outlet of the filtering device II or the sedimentation tank II is connected to a water inlet of the cooling device, and a water outlet of the cooling device is connected to a water inlet of the bipolar membrane electrodialysis equipment;

when the mixed solution containing the benzene series and the bromine is treated by the system, the regenerated solution obtained by regenerating the bromine absorption equipment by the regeneration unit I contains sodium bromide and sodium terephthalate, after the mixed solution is concentrated by the concentration device, the sodium terephthalate is separated out beyond the saturation solubility of the concentrated solution, after the mixed solution is treated by the filtering device II or the sedimentation tank II or cooled, the mixed solution is treated by the filtering device II or the sedimentation tank II, the sodium terephthalate insoluble substances are separated and removed by solid-liquid separation, and the aqueous solution obtained by the solid-liquid separation enters the bipolar membrane electrodialysis equipment for treatment.

Based on the above processing system, preferably, the cooling device is a cooling heat exchanger.

Based on the above processing system, it is preferable that,

when the benzene series removal unit I is benzene series absorption equipment, the mixed solution containing the benzene series and bromine enters a water inlet of the benzene series absorption equipment, a regeneration unit II is further arranged, an outlet of the regeneration unit II is connected to a regeneration liquid inlet of the benzene series absorption equipment, and a regeneration liquid outlet of the benzene series absorption equipment is connected to a circulating regeneration tank II or a regeneration liquid collection tank II of the regeneration unit II or is discharged out of the system through a regeneration liquid discharge port (the regeneration unit II comprises a circulating regeneration tank II or a regeneration liquid collection tank II or a regeneration liquid discharge port);

the regeneration unit II provides a regeneration liquid, the regeneration liquid is provided for the benzene series absorption equipment, the regeneration process can be a circulating regeneration mode or a disposable regeneration mode, and the regenerated regeneration liquid contains the benzene series regenerated from the benzene series absorption equipment; the purpose of the regeneration unit II is to regenerate the benzene series adsorbed on the benzene series absorption equipment into a regeneration liquid, the regeneration unit II does not regenerate in the regeneration unit II, but the regeneration unit II provides the regeneration liquid for the benzene series absorption equipment, and the regeneration liquid provided by the regeneration unit II is used in the benzene series absorption equipment to regenerate the benzene series adsorbed on the benzene series absorption equipment into the regeneration liquid;

the regeneration unit II can be cyclically regenerated, for example, a regeneration liquid is pumped from a cyclic regeneration tank II of the regeneration unit II to a regeneration liquid inlet of the benzene series absorption equipment, and a regeneration liquid outlet of the benzene series absorption equipment is connected to an inlet of the cyclic regeneration tank II, so that the benzene series absorption equipment is regenerated through the cycle; the regeneration liquid of the benzene series absorption equipment can also be used for one time, namely, the regeneration liquid is pumped from an outlet of the regeneration unit II to a regeneration liquid inlet of the benzene series absorption equipment, a regeneration liquid outlet of the benzene series absorption equipment is connected to an inlet of a regeneration liquid collecting tank II of the regeneration unit II, and the benzene series absorption equipment always receives the fresh regeneration liquid provided from the outlet of the regeneration unit II;

when the benzene series removal unit I is extraction equipment, the extraction equipment comprises an extraction tank, the extraction tank of the extraction equipment is provided with an extraction liquid inlet, a water outlet and an extraction agent discharge liquid outlet, the mixed solution containing the benzene series and the bromine enters the water inlet of the extraction tank, extraction liquid is added into the extraction tank from the extraction liquid inlet of the extraction tank, and the water outlet of the extraction tank of the extraction equipment is connected to the water inlet of the bromine absorption equipment; an extractant discharging liquid (comprising the extractant and extracted benzene series) of an extraction tank of the extraction equipment is discharged from an outlet and then is subjected to subsequent treatment; or the extraction equipment comprises an extraction tank and a separation tank, the extraction tank of the extraction equipment is provided with an extraction liquid inlet, a water inlet and an outlet, the separation tank of the extraction equipment is provided with an inlet, a water outlet and an extraction agent discharge liquid outlet, the mixed solution containing the benzene series and the bromine enters the water inlet of the extraction tank, extraction liquid is added into the extraction tank from the extraction liquid inlet of the extraction tank, the outlet of the extraction tank is connected to the inlet of the separation tank of the extraction equipment, the water outlet of the separation tank of the extraction equipment is connected to the water inlet of the bromine absorption equipment, and the extraction agent discharge liquid (consisting of the extraction agent and the benzene series discharged out) outlet of the separation tank of the extraction equipment is discharged and then subjected to subsequent treatment;

when the benzene removal unit I is acidification equipment, the acidification equipment is provided with an acidification tank, the acidification tank is provided with a water inlet and a water outlet, the mixed solution containing the benzene and the bromine enters the water inlet of the acidification tank, acid is added into the acidification tank from an acid adding pump, and the water outlet of the acidification tank of the acidification equipment is connected to the water inlet of the bromine absorption equipment after solid-liquid separation to remove solids (solid-liquid separation means that a sedimentation tank I or a filtering device I is designed between the acidification tank of the acidification equipment and the bromine absorption equipment to filter out the solids).

Based on the above treatment system, preferably, the outlet of the alkali-producing tank of the bipolar membrane electrodialysis device is collected and recycled; or the outlet of the alkali production tank is connected to the inlet of the regeneration unit I and/or the inlet of the regeneration unit II; the sodium hydroxide solution is in an alkali production tank of the bipolar membrane electrodialysis equipment and can be used as the regeneration liquid of the regeneration unit I and/or the regeneration unit II.

Based on the above processing system, preferably, in the extraction tank, the mixed solution containing the benzene series and the bromine is fully mixed with the extractant provided by the extractant inlet of the extraction tank for extraction; the extraction tank is stopped from stirring and layering or the extraction tank is driven into a separation tank for layering, and generally, the residual aqueous solution after the mixed solution containing the benzene series and the bromine is extracted is discharged at the lower part, and the benzene series extracted from the extractant + is discharged at the upper part (discharged from the extractant discharging liquid outlet).

Based on the above treatment system, it is preferable that the acidification device includes an acidification tank, an acid addition pump, and the like, and in the acidification tank, the mixed solution containing benzene series and bromine is mixed with acid pumped from the acid addition pump, and the reduction of PH causes the benzene series to partially precipitate as insoluble substances.

Based on the above treatment system, preferably, the acid pumped by the acid pump is hydrobromic acid, acetic acid or the like.

Based on the above treatment system, preferably, the regeneration unit ii comprises at least one of a circulating regeneration tank ii, a fresh regeneration liquid pressurized replenishing pipeline, a regeneration unit ii buffer tank and a regeneration unit ii mixing tank, or the regeneration unit ii further comprises a regeneration liquid collection tank ii. When the regeneration unit II is the circulation regeneration tank II, the outlet of the regeneration unit II is the outlet of the circulation regeneration tank II (the regenerated liquid in the circulation regeneration tank II is conveyed by the regeneration pump II, the outlet of the regeneration pump II and the inlet of the regeneration unit II are inlets of the circulation regeneration tank II (the regenerated liquid is supplemented); or when the regeneration unit II is the fresh regeneration liquid pressurized supplement pipeline, the outlet of the regeneration unit II is the outlet of the fresh regeneration liquid pressurized supplement pipeline, and the inlet of the regeneration unit II is the inlet of the fresh regeneration liquid pressurized supplement pipeline; or when the regeneration unit II is a regeneration unit II buffer tank, the outlet of the regeneration unit II is the outlet of the regeneration unit II buffer tank (including the outlet of a pump for conveying the regeneration liquid in the regeneration unit II buffer tank), and the inlet of the regeneration unit II is the inlet of the regeneration unit II buffer tank (replenishing the regeneration liquid); or when regeneration unit II is regeneration unit II blending tank, regeneration unit II's export is the export of regeneration unit II blending tank (contain regeneration liquid in the regeneration unit II blending tank is carried with the pump, the export of this pump), regeneration unit II's import is the import of regeneration unit II blending tank (regeneration unit II blending tank import make-up water and the regeneration liquid of high concentration (or the solid form of the material that regeneration liquid contains), the required concentration's of mixture regeneration liquid).

Based on the above treatment system, preferably, the regeneration liquid of the regeneration unit II is selected as a solvent, and the solvent is a solvent capable of dissolving part or all of the benzene series into the solvent;

based on the above treatment system, the solvent of the regeneration liquid of the regeneration unit II preferably comprises organic acid, alcohol, ether, aromatic compound or ester.

Based on the above processing system, preferably, the solvent types of the regeneration liquid of the regeneration unit II comprise: hydrous small molecular carboxylic acid with the content of more than 40 percent, anhydrous small molecular carboxylic acid, hydrous methanol with the methanol content of more than 40 percent, anhydrous methanol, hydrous ethanol or anhydrous ethanol with the ethanol content of more than 40 percent, and the like.

Based on the above treatment system, it is preferable that the regeneration liquid of the regeneration unit ii is selected to be an alkaline substance, such as hydroxide, carbonate, bicarbonate, or the like.

Based on the above treatment system, it is preferable that the cation in the hydroxide, carbonate or bicarbonate is potassium ion, sodium ion, or the like.

Based on the above treatment system, it is preferable that the filtration device i or the filtration device ii is a filter, a microfiltration filter, an MBR filtration filter, an ultrafiltration filter, or the like.

Based on the above treatment system, preferably, a pickling unit I and/or a pickling unit II are/is also provided,

the outlet of the pickling unit I is connected to the pickling solution inlet of the bromine element absorption equipment, and the pickling solution outlet of the bromine element absorption equipment is connected to the circulating pickling tank I or the pickling collection tank I of the pickling unit I or is discharged out of the system through a pickling solution discharge port (the pickling unit I is provided with the circulating pickling tank I or the pickling collection tank I or the pickling solution discharge port);

or the outlet of the acid washing unit II is connected to the acid washing liquid inlet of the benzene series absorption equipment, and the acid washing liquid outlet of the benzene series absorption equipment is connected to the circulating acid washing tank II or the acid washing collecting tank II of the acid washing unit II or is discharged out of the system through the acid washing liquid discharge port (the acid washing unit II is provided with the circulating acid washing tank II or the acid washing collecting tank II or the acid washing liquid discharge port);

the pickling unit i and/or the pickling unit ii are provided for washing out divalent or more than divalent cations (the source of the divalent or more than divalent cations is the divalent or more than divalent cations in the mixed solution containing the benzene-based substance and the bromine element when passing through the bromine element absorption apparatus or the benzene-based substance absorption apparatus) adhered to the bromine element absorption apparatus or the benzene-based substance absorption apparatus with a pickling solution (i.e., an acid solution), for example, ions such as iron, chromium, nickel, cobalt, manganese, etc. in the aqueous solution i are dissolved in the pickling solution and washed away; or cobalt ions, manganese ions and the like in the water solution II are dissolved in the pickling solution to be washed away; the purpose of the acid washing unit I or the acid washing unit II is to wash divalent or more cations adhered to the bromine element absorption equipment or the benzene series absorption equipment into acid washing liquid, the acid washing unit I or the acid washing unit II is not to carry out acid washing in the acid washing unit I or the acid washing unit II, but the acid washing unit I or the acid washing unit II is to provide acid washing liquid for the bromine element absorption equipment or the benzene series absorption equipment, and the divalent or more cations adhered to the bromine element absorption equipment or the benzene series absorption equipment are washed into the acid washing liquid by the acid washing liquid provided by the acid washing unit I or the acid washing unit II in the bromine element absorption equipment or the benzene series absorption equipment;

for the acid washing unit I or the acid washing unit II, the acid washing process can be in a circulating acid washing mode or a one-off acid washing mode:

the cyclic pickling mode is that pickling liquid is sprayed to a pickling liquid inlet of the bromine element absorption equipment from a cyclic pickling tank I of the pickling unit I, a pickling liquid outlet of the bromine element absorption equipment is connected to an inlet of the cyclic pickling tank I of the pickling unit I, and the bromine element absorption equipment is pickled by the cycle; or for example, the acid washing liquid is sprayed from a circulating acid washing tank II of the acid washing unit II to an acid washing liquid inlet of the benzene series absorption equipment, and an acid washing liquid outlet of the benzene series absorption equipment is connected to an inlet of a circulating acid washing tank II of the acid washing unit II, so that the benzene series absorption equipment is subjected to acid washing through the circulation;

the disposable pickling form is that pickling liquid is pumped from an outlet of the pickling unit I to a pickling liquid inlet of the bromine element absorption equipment, a pickling liquid outlet of the bromine element absorption equipment is connected to an inlet of a pickling collection tank I of the pickling unit I, and the bromine element absorption equipment always receives fresh pickling liquid provided from an outlet of the pickling unit I; or for example, the acid washing liquid is pumped from the outlet of the acid washing unit II to the acid washing liquid inlet of the benzene series absorption equipment, the acid washing liquid outlet of the benzene series absorption equipment is connected to the inlet of the acid washing collecting tank II of the acid washing unit II, and the benzene series absorption equipment always receives the fresh acid washing liquid provided from the outlet of the acid washing unit II.

Based on the above treatment system, preferably, the acid used in the acid washing unit I and/or the acid washing unit II is acetic acid, hydrobromic acid or the like.

Based on the above treatment system, it is preferable that when the acid used in the acid washing unit I or the acid washing unit II is acetic acid, the acetic acid is an aqueous solution having an acetic acid concentration of 0.5% to 50%.

Based on the above treatment system, it is preferable that when the acid used in the acid washing unit i or the acid washing unit ii is hydrobromic acid, the hydrogen bromide is an aqueous hydrogen bromide solution having a hydrogen bromide concentration of 0.5% to 20%.

Based on the above treatment system, preferably, the acid washing unit i comprises at least one of a circulating acid washing tank i, a fresh acid washing liquid pressurized supplementing pipeline, a buffer tank of the acid washing unit i and a mixing tank of the acid washing unit i, or the acid washing unit i further comprises an acid washing collecting tank i; the acid washing unit II comprises at least one of a circulating acid washing tank II, a fresh acid washing liquid pressurized supplementing pipeline, an acid washing unit II buffer tank and an acid washing unit II mixing tank, or the acid washing unit II further comprises an acid washing collecting tank II. When the pickling unit I or the pickling unit II is the circulating pickling tank I or the circulating pickling tank II, the outlet of the pickling unit I or the pickling unit II is the outlet of the circulating pickling tank I or the circulating pickling tank II (the pickling solution in the circulating pickling tank I or the circulating pickling tank II is conveyed by the pickling pump I or the pickling pump II, the outlet of the pickling pump I or the pickling pump II), and the inlet of the pickling unit I or the pickling unit II is the inlet of the circulating pickling tank I or the circulating pickling tank II (the pickling solution is supplemented); or when the acid washing unit I or the acid washing unit II is the fresh acid washing liquid pressurized supplementing pipeline, the outlet of the acid washing unit I or the acid washing unit II is the outlet of the fresh acid washing liquid pressurized supplementing pipeline, and the inlet of the acid washing unit I or the acid washing unit II is the inlet of the fresh acid washing liquid pressurized supplementing pipeline; or when the acid washing unit I or the acid washing unit II is the buffer tank of the acid washing unit I or the buffer tank of the acid washing unit II, the outlet of the acid washing unit I or the outlet of the acid washing unit II is the outlet of the buffer tank of the acid washing unit I or the buffer tank of the acid washing unit II (comprising the delivery of the acid washing liquid in the buffer tank of the acid washing unit I or the buffer tank of the acid washing unit II by a pump, the outlet of the pump) and the inlet of the acid washing unit I or the inlet of the acid washing unit II are the inlet of the buffer tank of the acid washing unit I or the buffer tank of the acid washing unit II (the acid washing liquid is supplemented); or work as pickling unit I or pickling unit II does I blending tank of pickling unit or during the II blending tanks of pickling unit, pickling unit I or the export of pickling unit II does I blending tank of pickling unit or the export of the II blending tanks of pickling unit (contain I blending tank of pickling unit or the pump delivery is used to the pickler in the II blending tank of pickling unit, the export of this pump), pickling unit I or the import of pickling unit II does I blending tank of pickling unit or the import of the II blending tank of pickling unit (the pickler of the import make-up water and the high concentration of pickler of the I blending tank of pickling unit or pickling unit II blending tank mixes the pickler of required concentration).

Based on the treatment system, preferably, a water washing unit I and/or a water washing unit II are/is further arranged,

an outlet of the water washing unit I is connected to a water washing liquid inlet of the bromine element absorption equipment, and a water washing liquid outlet of the bromine element absorption equipment is connected to a circulating water washing tank I or a water washing collecting tank I of the water washing unit I or is discharged out of the system through a water washing liquid discharge port (the water washing unit I is provided with the circulating water washing tank I or the water washing collecting tank I or the water washing liquid discharge port);

or the outlet of the washing unit II is connected to the washing liquid inlet of the benzene series absorption equipment, and the washing liquid outlet of the benzene series absorption equipment is connected to the circulating water washing tank II or the washing collecting tank II of the washing unit II or is discharged out of the system through a washing liquid discharge port (the washing unit II is provided with the circulating water washing tank II or the washing collecting tank II or the washing liquid discharge port);

for the water washing unit I or the water washing unit II, the water washing process can be a circulating water washing mode or a disposable water washing mode:

the circulating water washing form is that for example, water washing liquid (namely water) is sprayed to a water washing liquid inlet of the bromine element absorption equipment from a circulating water washing tank I of the water washing unit I, a water washing liquid outlet of the bromine element absorption equipment is connected to an inlet of the circulating water washing tank I of the water washing unit I, and the bromine element absorption equipment is washed by the circulating water; or for example, a washing liquid (namely water) is sprayed to a washing liquid inlet of the benzene series absorption equipment from a circulating water washing tank II of the water washing unit II, and a washing liquid outlet of the benzene series absorption equipment is connected to an inlet of the circulating water washing tank II of the water washing unit II, so that the benzene series absorption equipment is washed in such a circulating manner;

the disposable water washing form is that for example, water washing liquid (i.e. water) is pumped from an outlet of the water washing unit i to a water washing liquid inlet of the bromine element absorption device, a water washing liquid outlet of the bromine element absorption device is connected to an inlet of a water washing collection tank i of the water washing unit i, and the bromine element absorption device always receives fresh water washing liquid (i.e. water) provided from the outlet of the water washing unit i; or for example, the water washing liquid (i.e. water) is sprayed to the water washing liquid inlet of the benzene series absorption equipment from the outlet of the water washing unit II, the water washing liquid outlet of the benzene series absorption equipment is connected to the inlet of the water washing collecting tank II of the water washing unit II, and the benzene series absorption equipment always receives the fresh water washing liquid (i.e. water) provided from the outlet of the water washing unit II.

One of the purposes of providing the water washing unit I and/or the water washing unit II is to wash out cations adhered to the bromine element absorption equipment or the benzene series absorption equipment by using water (the adhered cations are from the source of the mixed solution containing the benzene series and the bromine element and adhered to resin when passing through the bromine element absorption equipment or the benzene series absorption equipment), for example, ions such as iron, chromium, nickel, cobalt, manganese, sodium and the like in the aqueous solution I are dissolved in the water and washed away; or cobalt, manganese, sodium and other ions in the water solution II are dissolved in water and washed away; the second purpose of the water washing unit I and/or the water washing unit II is to add a water washing step between the steps of acid washing and alkaline substance regeneration, which is favorable for avoiding the consumption of the alkaline substance regeneration liquid by acid adhered to the bromine element absorption equipment or the benzene series absorption equipment; the third purpose of arranging the water washing unit I and/or the water washing unit II is to add a water washing step between the regeneration of alkaline substances and the normal adsorption operation, which is favorable for avoiding that cations contained in the mixed solution containing the benzene series and the bromine element to be treated react with the bromine element absorption equipment or alkaline substances adhered on the benzene series absorption equipment to generate water-insoluble solid substances, for example, insoluble substances of cobalt hydroxide and manganese hydroxide are generated when cobalt ions and manganese ions meet alkali; iron, chromium and nickel ions also react to form respective insoluble solids when encountering alkali. The water washing unit I or the water washing unit II is not used for washing in the water washing unit I or the water washing unit II, but the water washing unit I or the water washing unit II is used for providing water washing liquid (namely water) for the bromine element absorption equipment or the benzene series absorption equipment, and the bromine element absorption equipment or the benzene series absorption equipment is washed by the water washing liquid (namely water) provided by the water washing unit I or the water washing unit II in the bromine element absorption equipment or the benzene series absorption equipment;

based on the above treatment system, preferably, the water washing unit i comprises at least one of a circulating water washing tank i, a fresh water washing liquid pressurized supplementing pipeline and a water washing unit i buffer tank, or the water washing unit i further comprises a water washing collection tank i; and the water washing unit II comprises at least one of a circulating water washing tank II, a fresh water washing liquid pressure supplementing pipeline and a water washing unit II buffer tank, or the water washing unit II further comprises a water washing collecting tank II. When the water washing unit I or the water washing unit II is the circulating water washing tank I or the circulating water washing tank II, the outlet of the water washing unit I or the outlet of the water washing unit II is the outlet of the circulating water washing tank I or the circulating water washing tank II (water washing liquid in the circulating water washing tank I or the circulating water washing tank II is conveyed by the water washing pump I or the water washing pump II, the outlet of the water washing pump I or the water washing pump II), and the inlet of the water washing unit I or the water washing unit II is the inlet of the circulating water washing tank I or the circulating water washing tank II (water is supplemented by the water washing liquid, namely water); or when the water washing unit I or the water washing unit II is the fresh water washing liquid (namely water) pressurized supplementing pipeline, the outlet of the water washing unit I or the water washing unit II is the outlet of the fresh water washing liquid pressurized supplementing pipeline, and the inlet of the water washing unit I or the water washing unit II is the inlet of the fresh water washing liquid pressurized supplementing pipeline; or work as washing unit I or washing unit II does wash I buffer tank of unit or during washing II buffer tank of unit, washing unit I or the export of washing unit II does wash I buffer tank of unit or the export of washing II buffer tank of unit (contain wash I buffer tank of unit or the washing liquid in the washing II buffer tank of unit is carried with the pump, the export of this pump), washing unit I or the import of washing unit II does wash I buffer tank of unit or the import of washing II buffer tank of unit (supplementary washing liquid, promptly water).

Based on the above treatment system, preferably, a gas inlet is further provided above the bromine element absorption equipment or the benzene series absorption equipment, and the gas inlet is vented or connected with compressed gas for exhausting gas (to avoid negative pressure in the bromine element absorption equipment or the benzene series absorption equipment when the bromine element absorption equipment or the benzene series absorption equipment is exhausted), so as to exhaust liquid in the bromine element absorption equipment or the benzene series absorption equipment (for example, to open a valve of the gas inlet).

Based on the above treatment system, preferably, a drain is further provided below the bromine element absorption equipment or the benzene series absorption equipment, and is configured to drain the liquid in the bromine element absorption equipment or the benzene series absorption equipment (for example, open a valve of the drain).

Based on the treatment system, preferably, a recovery unit is further provided, wherein the recovery unit comprises at least one of a recovery unit I, a recovery unit II, a recovery unit III and a recovery unit IV,

a discharge port of a circulating solvent tank or a solvent recovery tank of the benzene removal unit II is connected to an inlet of the recovery unit I, and a recovered solvent outlet of the recovery unit I is collected or recycled to an inlet of the benzene removal unit II; the recovery unit I comprises an evaporation tower, an evaporation reboiler (used for heating, and the evaporation reboiler can be replaced by other heating equipment) and an overhead condenser of the recovery unit I, wherein a recovered solvent outlet of the recovery unit I is an outlet of the overhead condenser after a gas phase of the evaporation tower of the recovery unit I is condensed by the overhead condenser; heating and evaporating the solvent with the benzene series dissolved into steam of the solvent in a heating mode, and condensing the steam by using the overhead condenser to obtain a pure solvent for recycling; a discharge port at the bottom of the evaporation tower of the recovery unit I discharges the system;

the discharge port of the circulation pickling tank I or the pickling collection tank I of the pickling unit I is connected to the inlet of the recovery unit II, and the acid outlet of the recovery unit II is connected to the inlet of the pickling unit I or the inlet of the pickling unit II; the recovery unit II comprises an evaporation tower and an evaporation reboiler of the recovery unit II (used for heating, and the evaporation reboiler can be replaced by other heating equipment), the recovery unit II is used for concentrating acid in a heating mode (part of water is brought back in the acid washing process, and is evaporated by heating, and an acid outlet of the recovery unit II is a discharge outlet after concentration of the evaporation tower) so as to be used as acid of the acid washing unit I or the acid washing unit II again;

the discharge port of a circulating pickling tank II or a pickling collection tank II of the pickling unit II is connected to the inlet of the recovery unit III, and the acid outlet of the recovery unit III is connected to the inlet of the pickling unit I or the inlet of the pickling unit II; the recovery unit III comprises an evaporation tower and an evaporation reboiler of the recovery unit III (used for heating, and the evaporation reboiler can be replaced by other heating equipment), the recovery unit III is used for concentrating acid in a heating mode (part of water is brought back in the acid washing process, and is evaporated by heating, and an acid outlet of the recovery unit III is a discharge outlet after concentration of the evaporation tower) so as to be used as acid of the acid washing unit I or the acid washing unit II again;

an extractant discharge liquid outlet of an extraction tank or a separation tank of the extraction equipment is connected to an inlet of the recovery unit IV, and an extractant outlet of the recovery unit IV is collected or reused to an extraction liquid inlet of the extraction tank of the extraction equipment; the recovery unit IV comprises an evaporation tower, an evaporation reboiler (for heating, the evaporation reboiler can be replaced by heating equipment in other forms) and an overhead condenser of the recovery unit IV, and an extractant outlet of the recovery unit IV is an outlet of the overhead condenser after a gas phase of the evaporation tower of the recovery unit IV is condensed by the overhead condenser; heating and evaporating the extractant dissolved with the benzene series into steam of the extractant in a heating mode, and condensing the steam by using the overhead condenser to obtain a pure extractant for recycling; and a discharge port at the bottom of the evaporation tower of the recovery unit IV discharges the system.

Based on above processing system, preferentially, bromine element absorption equipment is equipped with regeneration liquid import, washing liquid import, pickling liquid import, air inlet, water inlet, delivery port, washing liquid export, pickling liquid export, regeneration liquid export, or still is equipped with evacuation mouth, solvent import, solvent export bromine element absorption equipment's top or below design collector (or call to female pipe, house steward), will bromine element absorption equipment's regeneration liquid import, washing liquid import, pickling liquid import, solvent import, air inlet, evacuation mouth, solvent export, water inlet, delivery port, washing liquid export, pickling liquid export or regeneration liquid export are connected to as required on the collector (with collector junction design valve), realize the operation of system with opening, closing of valve according to system operation step governing valve with the valve.

Based on the above treatment system, it is preferred that the headers above or below the elemental bromine absorption apparatus be horizontal, vertical, inclined, and in any direction.

Based on above processing system, preferentially, benzene series absorption equipment is equipped with regeneration liquid import, washing liquid import, water inlet, regeneration liquid export, air inlet, washing liquid export, delivery port, or still is equipped with the evacuation mouth benzene series absorption equipment's top or below design collector (or call to mother pipe, house steward), will benzene series absorption equipment's regeneration liquid import, washing liquid import, water inlet, regeneration liquid export, air inlet, washing liquid export, delivery port or evacuation mouth are connected to as required on the collector (with collector junction design valve), realize the operation of system with opening, closing of valve is adjusted according to system operation step to the valve.

Based on the above treatment system, it is preferable that the header above or below the benzene-series absorption apparatus may be horizontal, vertical, or inclined, and may be in various directions.

Based on the above treatment system, preferably, the mixed solution containing benzene series and bromine is a mixed solution containing benzene series and bromine in a terephthalic acid production device (generally used as sewage at present), and comprises an aqueous solution (i.e. an aqueous solution i) obtained by adding water to the oxidation residue of the oxidation process of the terephthalic acid production device and filtering the oxidation residue, an aqueous solution (i.e. an aqueous solution ii) obtained by adding water to the oxidation residue of the oxidation process of the terephthalic acid production device and removing iron ions, cobalt ions and manganese ions, or an aqueous solution (i.e. an aqueous solution iii) obtained by adding water to the oxidation residue of the oxidation process of the terephthalic acid production device and removing iron ions, cobalt ions and manganese ions:

for example, an aqueous solution (mainly containing benzene series including phthalic acid and acid groups thereof, benzoic acid and acid groups thereof, p-toluic acid and acid groups thereof, p-carboxybenzaldehyde and acid groups thereof, and ions such as cobalt, manganese, bromine, sodium, iron, chromium, nickel, etc., namely, an aqueous solution i, sewage) obtained by filtering oxidation residues of an oxidation process of a terephthalic acid production apparatus with water and removing iron ions (namely, the aqueous solution ii, sewage), or an aqueous solution (namely, the aqueous solution iii, sewage) obtained by removing iron, cobalt, and manganese ions from oxidation residues of an oxidation process of a terephthalic acid production apparatus with water:

the aqueous solution (namely the aqueous solution II) obtained by adding water to the oxidation residue in the oxidation process of the terephthalic acid production device and removing iron ions is a residual aqueous solution (mainly containing benzene series including phthalic acid and acid radicals thereof, benzoic acid and acid radicals thereof, p-toluic acid and acid radicals thereof, p-carboxybenzaldehyde and acid radicals thereof, and ions such as cobalt, manganese, bromine, sodium and the like) obtained by filtering the aqueous solution (namely the aqueous solution II) obtained by adding water to the oxidation residue and adding alkaline substances (sodium hydroxide, sodium carbonate, sodium bicarbonate and the like) to raise the pH to 4-6.5;

the aqueous solution (namely the aqueous solution III) obtained by adding water to the oxidation residue in the oxidation process of the terephthalic acid production device and removing iron, cobalt and manganese ions is prepared by adding water to the oxidation residue and adding alkaline substances (sodium hydroxide, sodium carbonate, sodium bicarbonate and the like) to raise the pH to be more than 8.5, forming iron, chromium, nickel, cobalt, manganese and the like ions into solid insoluble substances, and filtering to obtain a residual aqueous solution (mainly containing benzene series including phthalic acid and acid radicals thereof, benzoic acid and acid radicals thereof, p-toluic acid and acid radicals thereof, p-carboxybenzaldehyde and acid radicals thereof, and bromine, sodium and the like), and is remarked: the iron, chromium, nickel, cobalt and manganese ions can also be removed step by step, the PH value is firstly raised to 4-6.5, the iron, chromium and nickel ions form solid insoluble substances, the solid insoluble substances are removed by filtration, the PH value of the aqueous solution is raised to more than 8.5, the cobalt, manganese and other ions form solid insoluble substances, and the solid insoluble substances are removed by filtration; or the water solution (namely the water solution III) obtained by adding water to the oxidation residue in the oxidation process of the terephthalic acid production device and removing iron, cobalt and manganese ions is the water solution left after the water solution obtained by adding water to the oxidation residue and filtering is subjected to cobalt-manganese adsorption resin to adsorb the cobalt, manganese and other cation ions in the water solution.

Based on the above treatment system, it is preferable that a plurality of buffer tanks and/or transfer pumps are provided for smooth operation of the treatment system.

Discharge and be the process the utility model discloses a follow after the processing the utility model discloses an emit away in the technology route, no matter take after discharging that what kind of method of specific processing does not all influence the utility model discloses the protection of content.

The utility model discloses the purpose difference and the mutual independence of different steps, unit etc. that design, each step, unit etc. can be used alone and also can select according to the actual demand and the combination of different orders, also can only select to use some step wherein, unit etc. all the utility model discloses the within range of patent protection.

Advantageous effects

The utility model discloses a to containing benzene series thing and bromine element's mixed solution's processing system, through this system benzene series thing and bromine element in to mixed solution draw out, reduced the concentration of benzene series thing and bromine element in mixed solution, just also reduced the adverse effect that benzene series thing and bromine element in this mixed solution caused sewage treatment, turn into hydrobromic acid material with bromine simultaneously and retrieve, kill two birds with one stone.

The system is simple to operate and simple in equipment, fully considers the recovery and reuse (the bromine in the bromine is recovered with the maximum capacity and almost has no waste) as much as possible, and greatly helps to reduce the operation cost of enterprises.

Drawings

Fig. 1 is a schematic diagram of a treatment system for a mixed solution containing a benzene-based substance and elemental bromine in the first embodiment, the second embodiment and the fourth embodiment.

Fig. 2 is a schematic flow diagram of an apparatus for electrodialysis concentration.

Fig. 3 is a schematic diagram of an electrodialysis concentration apparatus.

Fig. 4 is a schematic flow diagram of an apparatus of the bipolar membrane electrodialysis apparatus.

Fig. 5 is a schematic diagram of a bipolar membrane electrodialysis apparatus.

FIG. 6 is a schematic diagram of a partial replacement of part three A of the example for the processing system of FIG. 1 for a mixed solution containing benzene and elemental bromine.

FIG. 7 is a schematic view of a partial replacement of the treatment system of FIG. 1 for a mixed solution containing a benzene series and elemental bromine in section III of the example.

Legend:

Detailed Description

The mixed solution treated in all the following examples is a mixed solution containing benzene and bromine, and the source of the mixed solution is a mixed solution (sewage) containing benzene and bromine of a terephthalic acid production device, specifically an aqueous solution (sewage) obtained by adding water and filtering oxidation residue of an oxidation process of the terephthalic acid production device, namely the aqueous solution I (namely the mixed solution treated in all the following examples is the aqueous solution I), and the analysis result of the components of the aqueous solution I is as follows (unit ppm):

example one

A treatment system for a mixed solution containing benzene series and bromine mainly comprises bromine absorption equipment, a regeneration unit I and a debenzolization unit I (the debenzolization unit I in the embodiment is acidification equipment):

the mixed solution (i.e. the source of the mixed solution, which is the aqueous solution i in this embodiment) 01 containing the benzene series and the bromine is connected to the water inlet of the acidification tank 02 of the acidification device, and the other inlet of the acidification tank 02 of the acidification device is connected to the outlet of the acid adding pump 47. A water outlet at the bottom of an acidification tank 02 of the acidification device is connected with a water inlet of a filter device I03, a water outlet of the filter device I03 is connected with a water inlet 57 of a bromine element absorption device 04, and a water outlet 05 is formed in the bottom of the bromine element absorption device 04;

the acid washing unit I is a circulating acid washing tank I25, the bottom of the circulating acid washing tank I25 is connected to an inlet of an acid washing pump I27 of the acid washing unit I, an outlet of the acid washing pump I27 of the acid washing unit I is connected to an acid washing liquid inlet 53 of a bromine element absorption device 04, an acid washing liquid outlet 59 of the bromine element absorption device 04 is connected to an inlet of the circulating acid washing tank I25 of the acid washing unit I, a bottom discharge outlet of the circulating acid washing tank I25 of the acid washing unit I is connected to an inlet of an evaporation tower 28 of a recovery unit II, the recovery unit II comprises the evaporation tower 28 and an evaporation reboiler 29, the evaporation tower 28 of the recovery unit II is connected with the evaporation reboiler 29 of the recovery unit II (the evaporation reboiler 29 is connected to a steam pipeline 37 for heating), a steam discharge pipeline 49 of the recovery unit II is arranged at the top of the evaporation tower 28 of the recovery unit II, and a bottom acid outlet of the evaporation tower 28 of the recovery unit II is connected to an inlet of the circulating acid washing tank I25 of the acid washing unit I; the evaporation tower 28 of the recovery unit II is provided with a discharge port 61 of the recovery unit II;

the water washing unit I is a circulating water washing tank I18, the bottom of the circulating water washing tank I18 is connected to an inlet of a water washing pump I23 of the water washing unit I, an outlet of the water washing pump I23 of the water washing unit I is connected to a water washing liquid inlet 52 of the bromine element absorption equipment 04, and a water washing liquid outlet 58 of the bromine element absorption equipment 04 is connected to an inlet of the circulating water washing tank I18 of the water washing unit I;

an air inlet 55 is arranged above the bromine element absorption equipment 04, and a drain 50 is arranged below the bromine element absorption equipment 04;

the regeneration unit I is a circulation regeneration tank I06, the bottom of the circulation regeneration tank I06 is connected to the inlet of a regeneration pump I08 of the regeneration unit I, the outlet of the regeneration pump I08 of the regeneration unit I is connected to a regeneration liquid inlet 51 of the bromine element absorption equipment 04, and a regeneration liquid outlet 60 of the bromine element absorption equipment 04 is connected to the inlet of the circulation regeneration tank I06 of the regeneration unit I;

a liquid outlet at the bottom of a circulating regeneration tank I06 of the regeneration unit I is connected to a water inlet of an evaporation tower 41 of an evaporation concentration device, the evaporation concentration device comprises the evaporation tower 41 and an evaporation reboiler 42, the evaporation tower 41 of the evaporation concentration device is connected with the evaporation reboiler 42 of the evaporation concentration device (the evaporation reboiler 42 is connected to a steam pipeline 37 for heating), a steam discharge port 44 is arranged at the top of the evaporation tower 41 of the evaporation concentration device, a concentrated solution water outlet 43 at the bottom of the evaporation tower 41 of the evaporation concentration device is connected to a water inlet of a cooler 45, a water outlet of the cooler 45 is connected to a water inlet of a filtering device II 46, and a water outlet of the filtering device II 46 is connected to a water inlet of the bipolar membrane electrodialysis equipment 30 (namely, a water inlet 221 of the bipolar membrane electrodialysis equipment);

a heater and a blowing device are arranged on an acid production tank 31 of the bipolar membrane electrodialysis equipment 30, and the acid production tank 31 is collected and recycled into a barrel; an alkali production tank 32 of the bipolar membrane electrodialysis device is connected to an inlet of a circulating regeneration tank I06 of the regeneration unit I or collected and recycled into a barrel; a fresh-salt water tank 33 of the bipolar membrane electrodialysis apparatus is connected to a water inlet of a fresh-salt water pump 34 of the bipolar membrane electrodialysis apparatus, and a water outlet of the fresh-salt water pump 34 of the bipolar membrane electrodialysis apparatus is connected to a water inlet of an evaporation tower 41 of the evaporation concentration device.

The treatment system of the mixed solution containing the benzene series and the bromine element operates according to the following steps:

step 1: the water solution I enters an acidification tank 02 of acidification equipment, acid added through an acid adding pump 47 is added into the acidification tank 02 of the acidification equipment (acetic acid is selected in the embodiment, pH is adjusted to be 3), the water solution I is added with the acid and stirred, then is filtered through a filtering device I03, enters bromine element absorption equipment 04 after being filtered to absorb bromine element (part of residual benzene series in the water solution I can be absorbed in the absorption process, resin with adsorption capacity on bromine is filled in the bromine element absorption equipment 04 in the embodiment, the resin filling amount is 10L, and the flow rate in the resin is 10L/H), and then is discharged out of the system from a water outlet 05 of the bromine element absorption equipment 04;

step 2: after being treated by the bromine element absorption equipment 04 for 10 hours, stopping entering the bromine element absorption equipment, opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening a drain port 50 of the bromine element absorption equipment 04 or a water outlet 05 of the bromine element absorption equipment 04, and draining the bromine element absorption equipment 04;

and step 3: an inlet 36 of the acid washing unit I replenishes acid washing liquid to a circulating acid washing tank I25 (in the embodiment, 5% acetic acid is used as the acid washing liquid, and the acid replenishing volume is 40L), the circulating acid washing tank I25 pumps the acid washing liquid to a bromine element absorption device 04 for acid washing of the bromine element absorption device 04 by using an acid washing pump I27, the acid washing liquid after acid washing returns to the circulating acid washing tank I25, and circulation acid washing is carried out by establishing circulation; after pickling is finished for 2 hours, after the bromine element absorption equipment 04 finishes pickling, the pickling solution in the circulating pickling tank I25 is discharged to an evaporation tower 28 of a recovery unit II for evaporation and concentration (concentration is 1.5 times), after concentration, part of the concentrated pickling solution is discharged back to the circulating pickling tank I25 from the bottom of the evaporation tower 28 of the recovery unit II for next pickling, and the other part of the concentrated pickling solution is discharged out of the system from a discharge port 61 of the evaporation tower 28;

and 4, step 4: opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening a drain 50 of the bromine element absorption equipment 04 or a water outlet 05 of the bromine element absorption equipment 04, and draining the pickling solution in the bromine element absorption equipment 04; the discharged pickling solution can be collected back to the circulating pickling tank I25;

and 5: an inlet 48 of the washing unit I is used for replenishing water (the water replenishing amount is 40L) to the circulating water washing tank I18, the circulating water washing tank I18 is used for pumping washing liquid to the bromine element absorption equipment 04 by using a washing pump I23 for washing the bromine element absorption equipment 04 (the washing speed is 20L/H), the washing liquid after washing returns to the circulating water washing tank I18, and the circulation is established for circulating washing;

and 6: after the water washing is finished for 2 hours, opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening a drain 50 of the bromine element absorption equipment 04 or a water outlet 05 of the bromine element absorption equipment 04, and draining the water washing liquid in the bromine element absorption equipment 04; simultaneously, the circulating water washing tank I18 is emptied;

and 7: an inlet 09 of the regeneration unit I supplements regeneration liquid (the regeneration liquid in the embodiment is 8% sodium hydroxide aqueous solution, and is 20L) to a circulation regeneration tank I06, the circulation regeneration tank I06 pumps the regeneration liquid to bromine element absorption equipment 04 by a regeneration pump I08 to regenerate the bromine element absorption equipment 04 (the regeneration speed is 20L/H), the regenerated regeneration liquid returns to the circulation regeneration tank I06, and the circulation is established for circulation regeneration;

and 8: after the regeneration process is finished for 3 hours, opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening an evacuation port 50 of the bromine element absorption equipment 04 or a water outlet 05 of the bromine element absorption equipment 04, and evacuating the regeneration liquid in the bromine element absorption equipment 04; the discharged regeneration liquid can be collected back to the circulation regeneration tank I06;

and step 9: an inlet 48 of the washing unit I is used for replenishing water (the water replenishing amount is 40L) to the circulating water washing tank I18, the circulating water washing tank I18 is used for pumping washing liquid to the bromine element absorption equipment 04 by using a washing pump I23 for washing the bromine element absorption equipment 04 (the washing speed is 20L/H), the washing liquid after washing is delivered to the circulating water washing tank I18, and the circulation is established for circulating washing;

step 10: after the water washing is finished for 2 hours, opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening an emptying port 50 of the bromine element absorption equipment 04 or a water outlet 05 of the bromine element absorption equipment 04, emptying the water washing liquid in the bromine element absorption equipment 04, simultaneously emptying a circulating water washing tank I18, and then preparing the bromine element absorption equipment 04 to meet the next feeding treatment of the aqueous solution I;

step 11: the regenerated regeneration liquid stored in the circulation regeneration tank I06 enters an evaporation tower 41 of an evaporation concentration device for evaporation concentration (concentration is 4 times), the concentrated liquid obtained after concentration is cooled by a cooler 45 and then enters a filtering device II 46 for filtering (sodium terephthalate in the regenerated liquid after concentration exceeds the saturation solubility thereof and is separated into solid which is removed by filtering), the filtering device II 46 then enters a bipolar membrane electrodialysis device 30 for treatment, the hydrobromic acid obtained by treatment is collected as a product of the system (namely an acid production tank 31, meanwhile, the acid production tank 31 is heated to 50 ℃ and is blown with a small amount of air to float a plurality of bubbles), the sodium hydroxide obtained by treatment is collected as a product of the system (namely an alkali production tank 32), or the sodium hydroxide obtained by treatment can return to the circulation regeneration tank I06 to be used as the regeneration liquid again, the light salt water obtained by treatment (namely, the light salt water tank 33 enters the evaporation tower 41 of the evaporation concentration device through a light salt water pump 34) for evaporation concentration again, and returned again to the bipolar membrane electrodialysis device 30 for treatment.

Remarks 1: the emptying port 50, the regeneration liquid inlet 51, the water washing liquid inlet 52, the pickling liquid inlet 53, the air inlet 55, the water inlet 57, the water washing liquid outlet 58, the pickling liquid outlet 59, the regeneration liquid outlet 60 and the water outlet 05 which are connected to the bromine element absorption equipment 04 are all connected with the bromine element absorption equipment 04 through valves, and the corresponding valves are opened and closed according to the sequence of the operation steps.

Remarks 2: the internal construction and operation principle of the bipolar membrane electrodialysis apparatus (note: the internal construction flow of the bipolar membrane electrodialysis in all the examples is the same, the bipolar membrane electrodialysis apparatus has two kinds of two compartments and three compartments, the two compartments are the combination of the bipolar membrane + the positive membrane or the negative membrane, the three compartments are the combination of the bipolar membrane + the positive membrane + the negative membrane (the transfer efficiency is high), and the three-compartment bipolar membrane electrodialysis apparatus is introduced as follows:

the bipolar membrane electrodialysis device 30 mainly comprises an electrode plate anode 201, an electrode plate cathode 202, a bipolar membrane 203, a cathode membrane 204, an anode membrane 205, an acid chamber 206, a salt dropping chamber 207, a base chamber 208, a polar water chamber 225, a polar water tank 209, a circulating polar water pump 210, a lost salt water tank 211, a circulating lost salt water pump 212, a circulating base tank 213, a circulating base pump 214, a circulating acid tank 215, a circulating acid pump 216, an acid production tank 31, an alkali production tank 32 and a dilute salt water tank 33. The outlet of the polar water tank 209 is connected to the inlet of the circulating polar water pump 210, the outlet of the circulating polar water pump 210 is connected to the inlet of the polar water chamber 225, and the outlet of the polar water chamber 225 is connected to the inlet of the polar water tank 209 to form a circulation; the outlet of the brine loss tank 211 is connected to the inlet of the brine circulation loss pump 212, the outlet of the brine circulation loss pump 212 is connected to the inlet of the brine loss chamber 207, and the outlet of the brine loss chamber 207 is connected to the inlet of the brine loss tank 211 to form a circulation; the outlet of the circulating alkali tank 213 is connected to the inlet of a circulating alkali pump 214, the outlet of the circulating alkali pump 214 is connected to the inlet of the alkali chamber 208, and the outlet of the alkali chamber 208 is connected to the inlet of the circulating alkali tank 213 to form a circulation; an outlet of the circulating acid tank 215 is connected to an inlet of a circulating acid pump 216, an outlet of the circulating acid pump 216 is connected to an inlet of the acid chamber 206, and an outlet of the acid chamber 206 is connected to an inlet of the circulating acid tank 215 to constitute a circulation. The pure water pipe 217 is connected to an inlet of the circulating alkali tank 213 (make-up pure water), and the circulating alkali tank 213 overflows to the alkali producing tank 32; the pure water pipe 217 is connected to the inlet of the circulating acid tank 215 (make-up pure water), and the circulating acid tank 215 overflows to the acid production tank 31; the water inlet 221 (i.e., the aqueous solution entering the bipolar membrane electrodialysis device 30 to be treated) is connected to the inlet make-up aqueous solution (i.e., replenished with ions) of the brine waste tank 211, and the brine waste tank 211 overflows to the brine fresh tank 33.

Firstly, the bipolar membrane 203 can electrolyze water into hydrogen ions 223 and hydroxide ions 224, the bipolar membrane 203, the cathode membrane 204 and the anode membrane 205 are arranged in sequence to form a plurality of alternate membrane stacks, and under the action of a direct current electric field, for all ions, cations 116 (cations contained in the treated salt, namely cations in the salt supplemented from the supplemented water 221) and the hydrogen ions 223 migrate towards the negative electrode 202 of the electrode plate, and anions 117 (anions contained in the treated salt, namely anions in the salt supplemented from the supplemented water 221) and the hydroxide ions 224 migrate towards the positive electrode 201 of the electrode plate.

The cations 116 and hydrogen ions 223 can pass through the positive membrane 205 and cannot pass through the negative membrane 204; the anion 117 and hydroxide ion 224 can pass through the negative membrane 204 and not the positive membrane 205.

Cations 116 in the salt losing chamber 207 move in the direction of the electrode plate negative electrode 202, pass through the positive membrane 205, enter the alkali chamber 208, anions 117 in the salt losing chamber 207 move in the direction of the electrode plate positive electrode 201, pass through the negative membrane 204, enter the acid chamber 206, and ions in the salt losing chamber 207 are lost. The hydroxide ions 224 generated by the water electrolysis of the bipolar membrane 203 move to the positive electrode 201 of the electrode plate and enter the alkali chamber 208 (form alkali with the cations 116 from the salt losing chamber 207), and the hydrogen ions 223 generated by the water electrolysis of the bipolar membrane 203 move to the negative electrode 202 of the electrode plate and enter the acid chamber 206 (form acid with the anions 117 from the salt losing chamber 207), so that the acid concentration in the acid chamber 206 is gradually increased and the alkali concentration in the alkali chamber 208 is also gradually increased because the direct current electric field is always present.

The salt losing chamber 207 continuously maintains the flow of water in the salt losing chamber 207 through the salt losing tank 211 and the salt losing circulating pump 212, in order to replenish ions in the salt losing chamber, water containing ions needs to be continuously replenished from the water inlet 221, and water with low ion concentration is discharged to the fresh salt water tank 33, in order to avoid the direct mixing of the water inlet 221 with relatively high concentration and the backwater of the salt losing circulating pump 212 (with relatively low concentration), a partition plate is arranged in the salt losing chamber 211, and the fresh salt water tank 33 is also led out and discharged from the backwater side of the salt losing circulating pump 212 (with relatively low concentration);

the acid chamber 206 is continuously maintained to flow the water in the acid chamber 206 through the circulating acid tank 215 and the circulating acid pump 216, and as the acid concentration in the circulating acid tank 215 is continuously increased, in order to keep the acid concentration in the circulating acid tank 215 stable, the flow of the supplementary pure water 217 is controlled in the circulating acid tank 215, and the supplementary pure water is continuously overflowed to the acid production tank 31 when the volume of the supplementary pure water is increased;

the acid chamber 208 continuously maintains the flow of the water in the alkali chamber 208 through the circulating alkali tank 213 and the circulating alkali pump 214, because the alkali concentration in the circulating alkali tank 213 is continuously increased, in order to keep the alkali concentration in the circulating alkali tank 213 stable, the flow of the supplemented pure water 217 is controlled in the circulating alkali tank 213, and the supplemented pure water is increased in volume and can continuously overflow to the alkali production tank 32;

in order to ensure conductivity, polar water, which is generally an aqueous sodium hydroxide solution, is present between the positive electrode plate 201 and the adjacent one of the bipolar membranes 203, and between the negative electrode plate 202 and the adjacent one of the bipolar membranes 203, and is also circulated by the polar water tank 209 and the polar water circulation pump 210.

Note: the utility model discloses the electrodialysis that all embodiments used is EX-4S-ED that Hangzhou blue nature technology share limited company provided, bipolar membrane electrodialysis is EX-4S that Hangzhou blue nature technology share limited company provided, reverse osmosis membrane uses DuPont' S SW30HRLE-440i, the filter is the conventional 5um pp cotton filter of selling, benzene and acetic acid, sodium hydroxide are industrial grade product, the resin that has adsorption efficiency to bromine that packs in bromine element absorption equipment 04 is the A62-MP resin that kohaisi (Beijing) science and technology limited company provided, benzene series thing absorption equipment 301 packs the resin that has adsorption efficiency to benzene series thing is the benzene series thing adsorption resin-600 of American Dusheng brand ADSTulsu.

The experiment was run using the system described above:

the system samples and analyzes values at each point (the following concentration units are ppm if not specified):

the analysis results of the components of the aqueous solution I are as follows:

PH	TA	BA	4-CBA	PT acid	Cobalt ion	Manganese ion	Bromine ion	Sodium ion
									4.68	7347	1625	183	452	1296	878	2213	1290

After acetic acid is added into an acidification tank 02 of the acidification device to adjust the pH value to 3, a water sample passes through a filtering device I03 and is as follows:

the bromine element absorption equipment 04 samples and analyzes the results of water outlet from the water outlet 05 at different times:

the discharge liquid of a circulating pickling tank I25 of the pickling unit I is as follows:

the discharge from the circulating water wash tank I18 of the washing unit I was as follows (washing step after pickling):

the discharge liquid from the liquid outlet of the circulation regeneration tank I06 of the regeneration unit I is as follows (hereinafter referred to as regeneration liquid a):

sampling point	pH	TA	BA	4-CBA	PT acid	Bromine ion
							Discharge liquid of circulation regeneration tank I06	12.87	3005	332	88	188	8097

The discharge liquid from the circulating water washing tank I18 of the water washing unit I is as follows (step of water washing after regeneration):

the effluent from filtration unit ii 46 was analyzed as follows:

sampling point	pH	TA	BA	4-CBA	PT acid	Bromine ion
							Discharge from filtration apparatus II 46	13.61	122	989	287	577	31512

The acid forming tank 31 was analyzed as follows:

sampling point	Bromine ion	Sodium ion	Acidity hydrogen ion meter
				Acid generating tank 31	118622	512	1.5mol/L

The soda pot 32 was analyzed as follows:

the weak brine tank 33 was analyzed as follows:

sampling point	Bromide ion	Sodium ion
			Fresh brine tank 33	21025	5814

And (4) conclusion: the concentration of bromine and benzene series in the water (water outlet 05 of the bromine absorption equipment 04) finally discharged from the system after the water solution I is treated is reduced, and the method is favorable for the treatment of the sewage at the later stage; meanwhile, hydrobromic acid with acidity of 1.5mol/L and bromide ion of 118622ppm can be reused to generate economic value.

Example two

Part A:

in contrast to the first embodiment, in the first embodiment, the liquid outlet at the bottom of the circulating regeneration tank i 06 of the regeneration unit i is connected to the water inlet of the evaporation tower 41 of the evaporation concentration device, the evaporation concentration device includes the evaporation tower 41 and an evaporation reboiler 42, the evaporation tower 41 of the evaporation concentration device is connected to the evaporation reboiler 42 of the evaporation concentration device (the reboiler 42 is connected to the steam pipeline 37 for heating), the top of the evaporation tower 41 of the evaporation concentration device is provided with a steam discharge port 44, the water outlet 43 of the concentrated solution at the bottom of the evaporation tower 41 of the evaporation concentration device is connected to the water inlet of the cooler 45, the water outlet of the cooler 45 is connected to the water inlet of the filtering device ii 46, and the water outlet of the filtering device ii 46 is connected to the water inlet of the membrane electrodialysis apparatus 30 (i.e. the water inlet 221 of the bipolar membrane electrodialysis apparatus); a heater and a blowing device are arranged on an acid production tank 31 of the bipolar membrane electrodialysis equipment 30, and the acid production tank 31 is collected and recycled into a barrel; an alkali-producing tank 32 of the bipolar membrane electrodialysis equipment is connected to an inlet of a circulating regeneration tank I06 of the regeneration unit I or collected and recycled into a barrel; the dilute brine tank 33 of the bipolar membrane electrodialysis apparatus is connected to the water inlet of the dilute brine pump 34 of the bipolar membrane electrodialysis apparatus, and the water outlet of the dilute brine pump 34 of the bipolar membrane electrodialysis apparatus is connected to the water inlet of the evaporation tower 41 of the evaporation concentration device. The liquid outlet at the bottom of the circulating regeneration tank I06 of the 'replacement' regeneration unit I is connected to the water inlet of the reverse osmosis concentration device 38, the fresh water outlet 39 of the reverse osmosis concentration device 38 is discharged, the concentrated solution (concentrated water) outlet 40 of the reverse osmosis concentration device 38 is connected to the water inlet of the filtering device II 46, and the water outlet of the filtering device II 46 is connected to the water inlet of the bipolar membrane electrodialysis device 30 (i.e. the water inlet 221 of the bipolar membrane electrodialysis device). A heater and a blowing device are arranged on an acid production tank 31 of the bipolar membrane electrodialysis equipment 30, and the acid production tank 31 is collected and recycled into a barrel; an alkali production tank 32 of the bipolar membrane electrodialysis device is connected to an inlet of a circulating regeneration tank I06 of the regeneration unit I or collected and recycled into a barrel; a dilute brine tank 33 of the bipolar membrane electrodialysis apparatus is connected to a water inlet of a dilute brine pump 34 of the bipolar membrane electrodialysis apparatus, and a water outlet of the dilute brine pump 34 of the bipolar membrane electrodialysis apparatus is connected to a water inlet of the reverse osmosis concentration device 38. ", the rest is identical to the first embodiment.

The treatment system for the mixed solution containing the benzene series and the bromine element operates according to the following steps:

compared with the first embodiment, the step 11 is replaced as follows, the rest steps are completely the same as the first embodiment, and the replaced step 11 is as follows:

step 11: the regenerated regeneration liquid stored in the circulation regeneration tank I06 enters a reverse osmosis concentration device 38 for concentration (concentration by 4 times), the concentrated liquid (concentrated water) obtained after concentration enters a filtering device II 46 for filtration, the concentrated liquid (concentrated water) obtained after concentration enters a bipolar membrane electrodialysis device 30 for treatment after the filtering device II 46, the hydrobromic acid obtained after treatment is collected as a product of the system (namely an acid production tank 31, meanwhile, the acid production tank 31 is heated to 50 ℃, a small amount of air is blown in to enable a plurality of bubbles to float upwards), the sodium hydroxide obtained after treatment is collected as a product of the system (namely an alkali production tank 32), or the hydrobromic acid can return to the circulation regeneration tank I06 to be used as the regeneration liquid again, the light salt water obtained after treatment (namely the light salt water tank 33 passes through a light salt water pump 34) and is concentrated again through the reverse osmosis concentration device 38, and the light salt water returns to the bipolar membrane electrodialysis device 30 for treatment again.

Remarks 1: the emptying port 50, the regeneration liquid inlet 51, the washing liquid inlet 52, the pickling liquid inlet 53, the air inlet 55, the water inlet 57, the washing liquid outlet 58, the pickling liquid outlet 59, the regeneration liquid outlet 60 and the water outlet 05 which are connected to the bromine element absorption equipment 04 are all connected with the bromine element absorption equipment 04 through valves, and the corresponding valves are opened and closed according to the sequence of the steps of the operation.

The experiment was run using the system described above:

the source water of this experiment was the regeneration liquid a in example one, and the regeneration liquid a was treated by different subsequent methods, and the data of the regeneration liquid a is as follows:

regeneration liquid a (i.e., discharge liquid from the liquid discharge port of the recycling regeneration tank I06 of the regeneration unit I):

sampling point	pH	TA	BA	4-CBA	PT acids	Bromine ion
							Circulating regeneration tank I06 effluent	12.87	3005	332	88	188	8097

The regenerated liquid a is obtained after being concentrated by the reverse osmosis concentration device 38, then passing through the filtering device II 46 and being treated by the bipolar membrane electrodialysis equipment 30:

the acid forming tank 31 was analyzed as follows:

sampling point	Bromine ion	Sodium ion	Acidity hydrogen ion meter
				Acid producing tank 31	124324	601	1.6mol/L

The soda pot 32 was analyzed as follows:

sampling point	Bromine ion	Sodium ion	Alkalinity hydroxyl meter
				Acid producing tank 32	698	27793	1.3mol/L

The weak brine tank 33 was analyzed as follows:

and (4) conclusion: the concentration of bromine and benzene in the water (water outlet 05 of the bromine absorption equipment 04) finally discharged from the system after the water solution I is treated is reduced, and the method is favorable for the treatment of the sewage at the later stage; meanwhile, hydrobromic acid with acidity of 1.6mol/L and bromide ion of 124324ppm can be reused to generate economic value. This experiment also demonstrates that the effect of replacing the evaporative concentration unit (main unit, evaporative column 41, reboiler 42) with the reverse osmosis concentration unit 38 is the same.

And part B:

in contrast to the first embodiment, in the first embodiment, the liquid outlet at the bottom of the circulating regeneration tank i 06 of the regeneration unit i is connected to the water inlet of the evaporation tower 41 of the evaporation concentration device, the evaporation concentration device includes the evaporation tower 41 and an evaporation reboiler 42, the evaporation tower 41 of the evaporation concentration device is connected to the evaporation reboiler 42 of the evaporation concentration device (the reboiler 42 is connected to the steam pipeline 37 for heating), the top of the evaporation tower 41 of the evaporation concentration device is provided with a steam discharge port 44, the water outlet 43 of the concentrated solution at the bottom of the evaporation tower 41 of the evaporation concentration device is connected to the water inlet of the cooler 45, the water outlet of the cooler 45 is connected to the water inlet of the filtering device ii 46, and the water outlet of the filtering device ii 46 is connected to the water inlet of the membrane electrodialysis apparatus 30 (i.e. the water inlet 221 of the bipolar membrane electrodialysis apparatus); a heater and a blowing device are arranged on an acid-producing tank 31 of the bipolar membrane electrodialysis equipment 30, and the acid-producing tank 31 is collected and recycled into the barrel; an alkali production tank 32 of the bipolar membrane electrodialysis device is connected to an inlet of a circulating regeneration tank I06 of the regeneration unit I or collected and recycled into a barrel; the dilute brine tank 33 of the bipolar membrane electrodialysis apparatus is connected to the water inlet of the dilute brine pump 34 of the bipolar membrane electrodialysis apparatus, and the water outlet of the dilute brine pump 34 of the bipolar membrane electrodialysis apparatus is connected to the water inlet of the evaporation tower 41 of the evaporation concentration device. A liquid outlet at the bottom of a circulating regeneration tank I06 of the 'replacement' regeneration unit I is connected to a water inlet 113 of the electrodialysis concentration device 20, and a fresh water outlet 21 of the electrodialysis concentration device 20 discharges; a concentrated solution (concentrated water) outlet 22 of the electrodialysis concentration device 20 is connected to a water inlet of the filtering device II 46, and a water outlet of the filtering device II 46 is connected to a water inlet of the bipolar membrane electrodialysis equipment 30 (namely, a water inlet 221 of the bipolar membrane electrodialysis equipment). A heater and a blowing device are arranged on an acid production tank 31 of the bipolar membrane electrodialysis equipment 30, and the acid production tank 31 is collected and recycled into a barrel; an alkali-producing tank 32 of the bipolar membrane electrodialysis equipment is connected to an inlet of a circulating regeneration tank I06 of the regeneration unit I or collected and recycled into a barrel; a fresh-salt water tank 33 of the bipolar membrane electrodialysis apparatus is connected to a water inlet of a fresh-salt water pump 34 of the bipolar membrane electrodialysis apparatus, and a water outlet of the fresh-salt water pump 34 of the bipolar membrane electrodialysis apparatus is connected to a water inlet 113 of the electrodialysis concentration device 20. ", the rest is exactly the same as the first embodiment.

compared with the first embodiment, the step 11 is replaced as follows, the rest steps are completely the same as the first embodiment, and the step 11 for replacement is as follows:

step 11: the regenerated regeneration liquid stored in the circulation regeneration tank I06 enters the electrodialysis concentration device 20 for concentration (concentration by 4 times), the concentrated liquid (concentrated water) obtained after concentration enters the filtering device II 46 for filtration, the filtering device II 46 then enters the bipolar membrane electrodialysis device 30 for treatment, the treated hydrobromic acid is collected as a product of the system (namely, the acid production tank 31, meanwhile, the acid production tank 31 is heated to 50 ℃, a small amount of air is blown in to enable a plurality of bubbles to float upwards), the treated sodium hydroxide is collected as a product of the system (namely, the alkali production tank 32), or the treated weak brine can return to the circulation regeneration tank I06 to be used as the regeneration liquid again, the treated weak brine (namely, the weak brine tank 33 passes through the electrodialysis concentration device 20 again for concentration, and returns to the bipolar membrane electrodialysis device 30 again for treatment.

Remarking: internal construction and operation principle of electrodialysis concentration device (note: the internal construction flow of electrodialysis concentration device in all embodiments is the same):

the electrodialysis concentration device mainly comprises an electrode plate anode 101, an electrode plate cathode 102, a cathode membrane 103, an anode membrane 104, a salt losing chamber 111, a concentration chamber 112, an electrode water chamber 118, an electrode water tank 105, an electrode water circulating pump 106, a salt losing tank 107, a salt losing circulating pump 108, a concentration tank 109 and a circulating concentration pump 110. The outlet of the polar water tank 105 is connected to the inlet of the polar water circulating pump 106, the outlet of the polar water circulating pump 106 is connected to the inlet of the polar water chamber 118, and the outlet of the polar water chamber 118 is connected to the inlet of the polar water tank 105 to form a cycle; the outlet of the salt losing tank 107 is connected to the inlet of a salt losing circulating pump 108, the outlet of the salt losing circulating pump 108 is connected to the inlet of a salt losing chamber 111, and the outlet of the salt losing chamber 111 is connected to the inlet of the salt losing tank 107 to form a circulation; the outlet of the concentration tank 109 is connected to the inlet of the circulation concentration pump 110, the outlet of the circulation concentration pump 110 is connected to the inlet of the concentration chamber 112, and the outlet of the concentration chamber 112 is connected to the inlet of the concentration tank 109 to constitute a circulation. The water inlet 113 (i.e., the aqueous solution entering the electrodialysis concentration apparatus 20 to be treated) is connected to the inlet make-up aqueous solution (i.e., ions are made up) of the salt rejection tank 107, and the salt rejection tank 107 overflows from the fresh water outlet 21; a water inlet 113 (i.e., an aqueous solution to be treated entering the electrodialysis concentration apparatus 20) is connected to an inlet of the concentration tank 109, and the concentration tank 109 overflows through a concentrate (concentrate) outlet 22.

The negative films 103 and the positive films 104 are alternately stacked (with a separator between them) to form a plurality of film stacks in which the negative films 103 and the positive films 104 are alternately stacked, electrodes (an electrode plate positive electrode 101 and an electrode plate negative electrode 102) are arranged at two ends of the film stack, directional migration of ions is generated under the action of a direct current electric field, anions 117 migrate towards the direction of the electrode plate positive electrode 101, cations 116 migrate towards the direction of the electrode plate negative electrode 102, the anions 117 can penetrate through the negative films 103 and cannot penetrate through the positive films 104, and similarly, the cations 116 can penetrate through the positive films 104 and cannot penetrate through the negative films 103.

Such a combination will form salt losing chambers 111 (the cations 116 of the salt losing chambers 111 permeate the positive membrane 104 and lose the anions 117 permeate the negative membrane 103, so the salt content is continuously reduced) and concentrating chambers 112 (the concentrating chambers 112 obtain the cations 116 and the anions 117, so the salt content is continuously increased) in the membrane stack, so as to ensure the water flow and fresh ion supply and replacement of the salt losing chambers 111 and the concentrating chambers 112:

the salt losing chamber 111 continuously maintains the flow of water in the salt losing chamber 111 through the salt losing tank 107 and the salt losing circulating pump 108, in order to supplement ions in the salt losing chamber, water containing ions needs to be continuously supplemented from the water inlet 113, water with low ion concentration is discharged from the fresh water outlet 21, in order to avoid direct mixing of the water inlet 113 with relatively high concentration and the backwater of the salt losing circulating pump 108 (with relatively low concentration), a partition plate is arranged in the salt losing chamber 107, and the fresh water outlet 21 is also led out and discharged from the backwater side of the salt losing circulating pump 108 (with relatively low concentration);

the concentrating chamber 112 continuously maintains the flow of water in the concentrating chamber 112 through the concentrating tank 109 and the concentrating circulation pump 110, and the concentrated solution (concentrated water) 22 is continuously discharged because the ion rise of the concentrating chamber is accompanied by volume expansion in general; or the water solution is continuously supplemented to the concentration chamber 112 from the water inlet 113, that is, the volume is supplemented, so that the concentration chamber 112 overflows from the concentrated solution (concentrated water) outlet 22, and the concentration of the concentration chamber 112 is controlled by controlling the amount of the water solution supplemented to the concentration chamber 112 from the water inlet 113 (that is, a part of the water solution supplemented from the water inlet 113 is directly mixed with the concentrated water solution in the concentration chamber 112 without treatment, so that the final concentrated solution is prepared to overflow from the concentrated solution (concentrated water) outlet 22).

In order to ensure conductivity, polar water is present between the electrode plate positive electrode 101 and the adjacent one of the negative films 103, and between the electrode plate negative electrode 102 and the adjacent one of the positive films 104, and the polar water is generally an aqueous sodium hydroxide solution, and is circulated by the polar water tank 105 and the polar water circulation pump 106.

The experiment was run using the system described above:

The regeneration liquid a is concentrated by the electrodialysis concentration device 20, then passes through the filtering device II 46 and is treated by the bipolar membrane electrodialysis equipment 30 to obtain:

the acid forming tank 31 was analyzed as follows:

sampling point	Bromine ion	Sodium ion	Acidity hydrogen ion meter
				Acid producing tank 31	120876	753	1.6mol/L

The alkali production tank 32 was analyzed as follows:

sampling point	Bromine ion	Sodium ion	Alkalinity hydroxyl meter
				Acid producing tank 32	842	27123	1.2mol/L

The weak brine tank 33 was analyzed as follows:

sampling point	Bromine ion	Sodium ion
			Fresh brine tank 33	19986	5773

And (4) conclusion: the concentration of bromine and benzene in the water (water outlet 05 of the bromine absorption equipment 04) finally discharged from the system after the water solution I is treated is reduced, and the method is favorable for the treatment of the sewage at the later stage; meanwhile, hydrobromic acid with acidity of 1.6mol/L and bromide ion of 120876ppm can be reused to generate economic value. This experiment also demonstrates that the effect of replacing the evaporative concentration unit (main unit, evaporation column 41, reboiler 42) with the electrodialysis concentration unit 20 is the same.

Overall conclusion: for the concentration device, the evaporation concentration device (mainly comprising the evaporation tower 41 and the reboiler 42), the electrodialysis concentration device 20 or the reverse osmosis concentration device 38 is used for concentration, and the analysis results of the acid production tank 31, the alkali production tank 32 and the dilute brine tank 33 of the bipolar membrane electrodialysis equipment 30 are basically the same, and have the same functions and the concentration functions, so that the bipolar membrane electrodialysis equipment 30 can be provided with relatively concentrated inlet water, and therefore, the three concentration modes are feasible and completely interchangeable.

That is, similarly, by using the evaporation concentration device (mainly comprising the evaporation tower 41 and the reboiler 42), the electrodialysis concentration device 20 or the reverse osmosis concentration device 38, the concentration of bromine and benzene in the water (the water outlet 05 of the bromine absorption device 04) finally discharged from the system after the aqueous solution i is treated is reduced, which is beneficial to the subsequent sewage treatment; meanwhile, the obtained hydrobromic acid can be reused to generate economic value.

It is thus proved that the evaporation and concentration device (mainly comprising the evaporation tower 41 and the reboiler 42), the electrodialysis concentration device 20 or the reverse osmosis concentration device 38 are all the same in function but only in function of concentration, and the three devices can be replaced by each other. The regenerated liquid containing, for example, the regeneration unit i is concentrated 38 by a reverse osmosis concentration device, and the outlet of the brine pump 34 of the bipolar membrane electrodialysis apparatus 30 is concentrated by an electrodialysis concentration device 20 or an evaporation concentration device in a similar combination, that is, the concentration of the regenerated liquid of the regeneration unit i or the concentration of the outlet of the brine pump 34 of the bipolar membrane electrodialysis apparatus may be combined by one or more of an optional evaporation concentration device (mainly comprising an evaporation column 41, a reboiler 42), an electrodialysis concentration device 20, or a reverse osmosis concentration device 38.

EXAMPLE III

Part A:

a treatment system for a mixed solution containing benzene series and bromine mainly comprises bromine absorption equipment, a regeneration unit I and a debenzolization unit I (the debenzolization unit I in the embodiment is benzene series absorption equipment):

in contrast to the first and second embodiments, in this embodiment, the "mixed solution containing benzene series and bromine" (i.e., the source of the mixed solution, which is the aqueous solution i in this embodiment) 01 in the first and second embodiments is connected to the water inlet of the acidification tank 02 of the acidification device, and the other inlet of the acidification tank 02 of the acidification device is connected to the outlet of the acid adding pump 47. A water outlet at the bottom of an acidification tank 02 of the acidification device is connected with a water inlet of a filtering device I03, a water outlet of the filtering device I03 is connected with a water inlet 57 of a bromine element absorption device 04, a water outlet 05 at the bottom of the bromine element absorption device 04 is replaced by a mixed solution (namely, the source of the mixed solution, in the embodiment, an aqueous solution I) containing benzene series and bromine 01 which is connected with a water inlet 324 of a benzene series absorption device 301, a water outlet 329 at the bottom of the benzene series absorption device 301 is connected with the water inlet 57 of the bromine element absorption device 04, and a water outlet 05 at the bottom of the bromine element absorption device 04; the acid washing unit II is a circulating acid washing tank II 308, the bottom of the circulating acid washing tank II 308 is connected to the inlet of an acid washing pump II 310 of the acid washing unit II, the outlet of the acid washing pump II 310 of the acid washing unit II is connected to an acid washing liquid inlet 323 of the benzene system absorption equipment 301, an acid washing liquid outlet 327 of the benzene system absorption equipment 301 is connected to the inlet of the circulating acid washing tank II 308 of the acid washing unit II, the bottom discharge port of the circulating acid washing tank II 308 of the acid washing unit II is connected to the inlet of an evaporation tower 312 of the recovery unit III, the recovery unit III comprises the evaporation tower 312 and an evaporation reboiler 313, the evaporation tower 312 of the recovery unit III is connected with the evaporation reboiler 313 of the recovery unit III (the evaporation reboiler 313 is connected to a steam pipeline 37 for heating), the top of the evaporation tower 312 of the recovery unit III is provided with a steam discharge pipeline 314, and the bottom acid outlet of the evaporation tower 312 of the recovery unit III is connected to the inlet of the circulating acid washing tank II of the acid washing unit II; the evaporation tower 312 of the recovery unit III is provided with a discharge port 331 of the recovery unit III; the water washing unit II is a circulating water washing tank II 316, the bottom of the circulating water washing tank II 316 is connected to the inlet of a water washing pump II 318 of the water washing unit II, the outlet of the water washing pump II 318 of the water washing unit II is connected to a water washing liquid inlet 322 of the benzene series absorption equipment 301, and a water washing liquid outlet 328 of the benzene series absorption equipment 301 is connected to the inlet of the circulating water washing tank II 316 of the water washing unit II; an air inlet 326 is arranged above the benzene series absorption equipment 301, and a drain port 330 is arranged below the benzene series absorption equipment; the regeneration unit II is a circulation regeneration tank II 302, the bottom of the circulation regeneration tank II 302 is connected to the inlet of a regeneration pump II 304 of the regeneration unit II, the outlet of the regeneration pump II 304 of the regeneration unit II is connected to the regeneration liquid inlet 321 of the benzene series absorption equipment 301, the regeneration liquid outlet 325 of the benzene series absorption equipment 301 is connected to the inlet of the circulation regeneration tank II 302 of the regeneration unit II, and the rest parts are completely the same as the first embodiment and the second embodiment.

compared with the first embodiment and the second embodiment, the steps 1-2 are replaced as follows, the rest steps are completely the same as the first embodiment and the second embodiment, and the steps 1-2 for replacement are as follows:

step 1:

(1) the aqueous solution i enters the benzene series absorption equipment 301 (in this embodiment, the benzene series absorption equipment 301 is filled with resin having an adsorption capacity to benzene series, the resin loading amount is 10L, and the flow rate of the aqueous solution i in the resin is 10L/H), the benzene series in the aqueous solution i is adsorbed by the benzene series absorption equipment 301, and then enters the bromine element absorption equipment 04 to adsorb bromine element (in the adsorption process, a part of the remaining benzene series in the aqueous solution i is also absorbed, in this embodiment, the bromine element absorption equipment is filled with resin having an adsorption capacity to bromine, the resin loading amount is 10L, and the flow rate in the resin is 10L/H), and then the aqueous solution i is discharged from the water outlet 05 to the system;

(2) after the benzene series absorption equipment 301 is treated for 10 hours, the benzene series absorption equipment 301 stops entering the equipment, an air inlet 326 of the benzene series absorption equipment 301 is opened, an emptying port 330 of the benzene series absorption equipment 301 is opened at the same time, and the benzene series absorption equipment 301 is emptied;

(3) an inlet 311 of the acid washing unit II is used for supplementing acid to a circulating acid washing tank II 308 (in the embodiment, 5% acetic acid is used, and the acid supplementing volume is 40L), the circulating acid washing tank II 308 is used for pumping acid washing liquid to the benzene series absorption equipment 301 by using an acid washing pump II 310 to carry out acid washing on the benzene series absorption equipment 301 (the acid washing speed is 20L/H), the acid washing liquid after acid washing is returned to the circulating acid washing tank II 308, and the circulation is established for carrying out circulating acid washing; after pickling is finished for 2 hours, after the pickling of the benzene series absorption equipment 301 is finished, the pickling solution in the circulating pickling tank II 308 is discharged to an evaporation tower 312 of a recovery unit III for evaporation and concentration (concentration by 1.5 times), after concentration, the bottom of the evaporation tower 312 of the recovery unit III is discharged part of the concentrated pickling solution to the circulating pickling tank II 308 for next pickling, and the other part of the concentrated pickling solution is discharged out of the system from a discharge port 331 of the evaporation tower 312;

(4) opening an air inlet 326 of the benzene series absorption equipment 301, simultaneously opening an emptying port 330 of the benzene series absorption equipment 301, and emptying the pickling solution in the benzene series absorption equipment 301; the discharged pickling solution can be collected back to the circulating pickling tank II 308;

(5) an inlet 319 of the water washing unit II is used for replenishing water (the water replenishing amount is 40L) to a circulating water washing tank II 316, the circulating water washing tank II 316 is used for washing the benzene series absorption equipment 301 with water by using a water washing pump II 318, the washing liquid after washing returns to the circulating water washing tank II 316, and the circulation is established for circulating water washing;

(6) after the washing for 2 hours, opening the air inlet 326 of the benzene series absorption equipment 301, simultaneously opening the emptying port 330 of the benzene series absorption equipment 301, and emptying the washing liquid of the benzene series absorption equipment 301; simultaneously emptying the circulating water washing tank II 316;

(7) an inlet 305 of the regeneration unit II supplements regeneration liquid (the regeneration liquid in the embodiment is 8% sodium hydroxide aqueous solution, and is 20L) to a circulation regeneration tank II 302, the circulation regeneration tank II 302 uses a regeneration pump II 304 to pump the regeneration liquid to a benzene series absorption device 301 for regeneration (the regeneration speed is 20L/H) of the benzene series absorption device 301, the regenerated regeneration liquid returns to the circulation regeneration tank II 302, and the circulation is established for circulation regeneration;

(8) after the regeneration process is finished for 3 hours, opening the air inlet 326 of the benzene series absorption equipment 301, simultaneously opening the emptying port 330 of the benzene series absorption equipment 301, and emptying the regeneration liquid in the benzene series absorption equipment 301; the discharged regeneration liquid can be collected back to the circulating regeneration tank II 302;

(9) an inlet 319 of the water washing unit II is used for replenishing water (the water replenishing amount is 40L) to a circulating water washing tank II 316, the circulating water washing tank II 316 is used for washing the benzene series absorption equipment 301 with water by using a washing pump II 318, the washing liquid after washing returns to the circulating water washing tank II 316, and the circulation is established for circulating washing;

(10) after the washing for 2 hours, opening an air inlet 326 of the benzene series absorption equipment 301, simultaneously opening an emptying port 330 of the benzene series absorption equipment 301, emptying the washing liquid in the benzene series absorption equipment 301, simultaneously emptying a circulating water washing tank II 316, and then preparing the benzene series absorption equipment 301 for the next feeding treatment of the aqueous solution I;

step 2: after the benzene series is adsorbed by the benzene series absorption equipment 301, the water solution I is treated by the bromine absorption equipment 04 for 10 hours and then stops entering, an air inlet 55 of the bromine absorption equipment 04 is opened, meanwhile, an emptying port 50 of the bromine absorption equipment 04 or an water outlet 05 of the bromine absorption equipment 04 is opened, and the bromine absorption equipment 04 is emptied;

Remarks 2: the regeneration liquid inlet 321, the water washing liquid inlet 322, the acid washing liquid inlet 323, the water inlet 324, the regeneration liquid outlet 325, the air inlet 326, the acid washing liquid outlet 327, the water washing liquid outlet 328, the water outlet 329 and the drain 330 which are connected to the benzene series absorption equipment 301 are all connected with the benzene series absorption equipment 301 through valves, and the corresponding valves are opened and closed according to the sequence of the steps of the operation to realize the operation.

The experiment was run using the system described above:

the system samples and analyzes values at each point (the following concentration units are ppm if no special designation is given):

the source water of the experiment is an aqueous solution I, and the analysis result of the components of the aqueous solution I is as follows:

pH	TA	BA	4-CBA	PT acid	Cobalt ion	Manganese ion	Bromide ion	Sodium ion
									4.68	7347	1625	183	452	1296	878	2213	1290

The effluent from the water outlet 329 is sampled and analyzed at different time through the benzene series absorption equipment 301 to obtain the result:

the discharge liquid of the circulating pickling tank II 308 of the pickling unit II is as follows:

the discharge from the circulating water wash tank ii 316 of the water wash unit ii is as follows (step of water washing after pickling):

the discharge liquid from the liquid outlet of the circulating regeneration tank II 302 of the regeneration unit II is as follows:

sampling point	pH	TA	BA	4-CBA	PT acid	Bromine ion
							Recycle regeneration tank II 302 effluent	12.95	31231	7912	893	2003	11.2

The discharge liquid of the circulating water washing tank II 316 of the water washing unit II is as follows (step of water washing after regeneration):

and (4) conclusion: after the aqueous solution i was subjected to the experiment, "the benzene-based material absorption apparatus 301 in the experiment discharged from the water outlet 329" and "the aqueous solution i was subjected to the acidification tank 02 of the acidification apparatus in the first and second examples and acetic acid was added to adjust PH to 3, water samples are similar after passing through the filter device I03, the concentrations of benzene series (TA, BA, 4-CBA and PT acid) in the aqueous solution I are all reduced, the same concentrations of other cobalt ions, manganese ions, bromide ions and sodium ions do not affect the concentration and do not change, so it can be inferred that the same results as those in the first and second embodiments can be obtained by carrying out the subsequent route (step) of the water sample at the water outlet of the filtering device i 03 after acidification in the first and second embodiments on the water discharged from the water outlet 329 of the benzene-based absorption device 301 in the present experiment (i.e., the benzene-based absorption device 301 is used to replace the acidification device).

The concentrations of bromine and benzene in the water (the water outlet 05 of the bromine absorption equipment 04) finally discharged from the system after the water solution I is treated are reduced, and the method is favorable for the treatment of the sewage at the later stage; meanwhile, the obtained hydrobromic acid can be reused to generate economic value.

And part B:

a treatment system for a mixed solution containing benzene series and bromine mainly comprises bromine absorption equipment, a regeneration unit I and a benzene series removal unit I (the benzene series removal unit I in the embodiment is extraction equipment):

in contrast to the first and second embodiments, in this embodiment, the "mixed solution containing benzene series and bromine" (i.e., the source of the mixed solution, which is the aqueous solution i in this embodiment) 01 in the first and second embodiments is connected to the water inlet of the acidification tank 02 of the acidification device, and the other inlet of the acidification tank 02 of the acidification device is connected to the outlet of the acid adding pump 47. A water outlet at the bottom of an acidification tank 02 of the acidification device is connected with a water inlet of a filtering device I03, a water outlet of the filtering device I03 is connected with a water inlet 57 of a bromine element absorption device 04, a water outlet 05' at the bottom of the bromine element absorption device 04 is replaced by a mixed solution (namely the source of the mixed solution) 01 containing benzene series and bromine element and is connected with an inlet of an extraction tank 401 of the extraction device, the other inlet of the extraction tank 401 is a fresh extractant supplement pipeline 409, an outlet of the extraction tank 401 is connected with an inlet of a separation tank 402 of the extraction device, an outlet of an aqueous solution delivery pump 403 of the separation tank 402 of the extraction device is connected with the water inlet 57 of the bromine element absorption device 04, and a water outlet 05 at the bottom of the bromine element absorption device 04; an extractant discharge liquid outlet 404 of a separation tank 402 of the extraction device is connected to an inlet of an evaporation tower 405 of a recovery unit IV, the recovery unit IV comprises the evaporation tower 405, an evaporation reboiler 406 and a top condenser 408 of the evaporation tower, the evaporation tower 405 of the recovery unit IV is connected with the evaporation reboiler 406 of the recovery unit IV (the evaporation reboiler 406 is connected to a steam pipeline 37 for heating), the steam pipeline above the evaporation tower 405 of the recovery unit IV is connected to an inlet of the top condenser 408 of the evaporation tower, an outlet of the top condenser 408 is connected to an inlet of an extraction tank 401', and the rest parts are completely the same as the first embodiment and the second embodiment.

compared with the first embodiment and the second embodiment, the steps 1 to 2 are replaced as follows, the rest of the steps are completely the same as the first embodiment and the second embodiment, and the steps 1 to 2 are replaced as follows:

step 1:

(1) the aqueous solution i enters an extraction tank 401 of the extraction equipment, and meanwhile, a fresh extraction agent (benzene in this embodiment) is added to the extraction tank 401 of the extraction equipment, and is stirred, mixed and extracted, and is layered in a separation tank 402 after passing through the extraction tank 401, most of the benzene series is dissolved in the extraction agent benzene, the upper layer of the separation tank 402 is the extraction agent benzene + the dissolved benzene series, and the lower layer is a mixed solution (aqueous solution);

(2) the lower layer of the separation tank 402 is pumped to a bromine absorption device 04 by an aqueous solution delivery pump 403 to absorb bromine (part of the residual benzene series in the aqueous solution I is absorbed in the absorption process, the bromine absorption device in this embodiment is filled with resin having bromine absorption capacity, the resin filling amount is 10L, and the flow rate in the resin is 10L/H), and then the bromine is discharged out of the system from a water outlet 05;

(3) the upper layer of the separation tank 402 enters an evaporation tower 405 of a recovery unit IV to evaporate benzene into benzene vapor, and the benzene vapor returns to the extraction tank 401 to be reused after being condensed by a condenser 408 at the top of the evaporation tower.

Step 2: after benzene series are extracted from the aqueous solution I by extraction equipment (main equipment, namely an extraction tank 401 and a separation tank 402), treating the aqueous solution I by bromine element absorption equipment 04 for 10 hours, stopping the aqueous solution I, opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening an evacuation port 50 of the bromine element absorption equipment 04 or a water outlet 05 of the bromine element absorption equipment 04, and evacuating the bromine element absorption equipment 04;

The experiment was run using the system described above:

Extracted by an extraction tank 401 of the extraction device, then layered in a separation tank 402, and sampled and analyzed at the outlet of an aqueous solution delivery pump 403 as follows:

and (4) conclusion: in the experiment, the concentration of benzene compounds (TA, BA, 4-CBA, PT acid) in the aqueous solution i is reduced, and the concentration of other cobalt ions, manganese ions, bromide ions, and sodium ions is the same, and the concentration is not changed, so it can be inferred that the water discharged from the outlet of the aqueous solution delivery pump 403 in the experiment is implemented according to the following route (step) of the water outlet of the filter device i 03 after the acidification in the first and second embodiments (i.e. the acidification device is replaced by an extraction device), and the same result as the results in the first and second embodiments can be obtained.

Namely, the concentration of bromine and benzene series in the water (water outlet 05 of the bromine absorption equipment 04) finally discharged from the system after the water solution I is treated is reduced, which is beneficial to the treatment of the sewage at the later stage; meanwhile, the obtained hydrobromic acid can be reused to generate economic value.

Overall conclusion: for the benzene removal unit I, the effects of reducing the benzene concentration in the mixed solution (i.e. the aqueous solution I) containing the benzene and the bromine by using the acidification device (mainly comprising the acidification tank 02 and the acid addition pump 47), the benzene absorption device 301 or the extraction device (mainly comprising the extraction tank 401 and the separation tank 402) are the same, and the benzene concentration in the aqueous solution I can be reduced to different degrees, so that the three benzene removal units I can be realized in a feasible and completely interchangeable manner. No matter what kind of concrete mode of removing benzene series unit I passes, the same result can be obtained by following the subsequent route (step) of the water sample at the water outlet of the filtering device I03 of the first embodiment and the second embodiment.

Meanwhile, the concentration device in the subsequent step can be combined by one or more of an optional evaporation concentration device (mainly comprising an evaporation tower 41 and a reboiler 42), an electrodialysis concentration device 20 or a reverse osmosis concentration device 38.

In other words, the concentrations of bromine and benzene in the water (the water outlet 05 of the bromine absorption equipment 04) finally discharged from the system after the water solution I is treated are reduced, which is beneficial to the treatment of the sewage at the later stage; meanwhile, the obtained hydrobromic acid can be reused to generate economic value.

Example four

A treatment system for a mixed solution containing benzene series and bromine mainly comprises bromine absorption equipment, a regeneration unit I and a benzene series removal unit II:

in contrast to the first and second embodiments, this embodiment connects the "mixed solution containing benzene series and bromine" (i.e. the source of the mixed solution, in this embodiment, the aqueous solution i) 01 of the first and second embodiments to the water inlet of the acidification tank 02 of the acidification device, and the other inlet of the acidification tank 02 of the acidification device is connected to the outlet of the acid adding pump 47. A water outlet at the bottom of an acidification tank 02 of the acidification device is connected with a water inlet of a filtering device I03, a water outlet of the filtering device I03 is connected with a water inlet 57 of a bromine element absorption device 04, and a water outlet 05 is arranged at the bottom of the bromine element absorption device 04; the acid washing unit I is a circulating acid washing tank I25, the bottom of the circulating acid washing tank I25 is connected to an inlet of an acid washing pump I27 of the acid washing unit I, an outlet of the acid washing pump I27 of the acid washing unit I is connected to an acid washing liquid inlet 53 of a bromine element absorption device 04, an acid washing liquid outlet 59 of the bromine element absorption device 04 is connected to an inlet of the circulating acid washing tank I25 of the acid washing unit I, a bottom discharge outlet of the circulating acid washing tank I25 of the acid washing unit I is connected to an inlet of an evaporation tower 28 of a recovery unit II, the recovery unit II comprises the evaporation tower 28 and an evaporation reboiler 29, the evaporation tower 28 of the recovery unit II is connected with the evaporation reboiler 29 of the recovery unit II (the evaporation reboiler 29 is connected to a steam pipeline 37 for heating), a steam discharge pipeline 49 of the recovery unit II is arranged at the top of the evaporation tower 28 of the recovery unit II, and a bottom acid outlet of the evaporation tower 28 of the recovery unit II is connected to an inlet of the circulating acid washing tank I25 of the acid washing unit I; the evaporation tower 28 of the recovery unit II is provided with a discharge port 61 of the recovery unit II; the 'replacement' is that a mixed solution (namely, a source of the mixed solution, in this embodiment, an aqueous solution i) 01 containing the benzene series and the bromine is connected to a water inlet 57 of the bromine absorption equipment 04, and a water outlet 05 is arranged at the bottom of the bromine absorption equipment 04; the debenzolization unit II is a circulating solvent tank 10, the bottom of the circulating solvent tank 10 is connected to the inlet of a solvent pump 12 of the debenzolization unit II, the outlet of the solvent pump 12 of the debenzolization unit II is connected to a solvent inlet 54 of a bromine absorption device 04, a solvent outlet 56 of the bromine absorption device 04 is connected to the inlet of the circulating solvent tank 10 of the debenzolization unit II, the bottom discharge port of the circulating solvent tank 10 of the debenzolization unit II is connected to the inlet of an evaporation tower 14 of the recovery unit I, the recovery unit I comprises the evaporation tower 14, an evaporation reboiler 15 and an overhead condenser 16 of the evaporation tower 14, the evaporation tower 14 of the recovery unit I is connected with the evaporation reboiler 15 of the recovery unit I (the evaporation reboiler 15 is connected to a steam pipeline 37 for heating), the top of the evaporation tower 14 of the recovery unit I is provided with a steam pipeline of the recovery unit I, and is connected to the inlet of the overhead condenser 16 of the evaporation tower 14, the outlet of the overhead condenser 16 is connected to the circulating solvent tank 10; the evaporation column 14 of the recovery unit I is provided with a bottom discharge port 17' and the rest is completely the same as in the first and second embodiments.

compared with the first embodiment and the second embodiment, the steps 1 to 4 are replaced as follows, the rest steps are completely the same as the first embodiment and the second embodiment, and the steps 1 to 4 are replaced as follows:

step 1: the aqueous solution I enters bromine element absorption equipment 04 to absorb bromine elements (the absorption process can absorb part of the residual benzene series in the aqueous solution I, the bromine element absorption equipment 04 in the embodiment is filled with resin with bromine absorption capacity, the resin filling amount is 10L, and the flow rate in the resin is 10L/H), and then the bromine element is discharged out of the system from a water outlet 05;

and step 3: an inlet 13 of the benzene removal unit II is used for replenishing a solvent (the solvent in the embodiment is 92% acetic acid, and the volume is 40L) to a circulating solvent tank 10 of the benzene removal unit II, the circulating solvent tank 10 pumps the solvent to the bromine element absorption equipment 04 by using a solvent pump 12 to dissolve the benzene in the solvent to the bromine element absorption equipment 04, the solvent returns to the circulating solvent tank 10 after dissolving the benzene, and the circulation is established to circularly dissolve the benzene in the bromine element absorption equipment 04; after the cyclic dissolution is finished for 2 hours, after the bromine element absorption equipment 04 finishes the cyclic dissolution of the benzene series, the solvent in the cyclic solvent tank 10 is discharged to an evaporation tower 14 of a recovery unit I for evaporation, and the evaporated solvent acetic acid vapor is condensed by a condenser 16 and then returns to the cyclic solvent tank 10; the bottom discharge port 17 of the evaporation tower 14 of the recovery unit I discharges;

and 4, step 4: opening an air inlet 55 of the bromine element absorption equipment 04, simultaneously opening an emptying port 50 of the bromine element absorption equipment 04, and emptying the solvent in the bromine element absorption equipment 04; the discharged solvent can be collected back to the circulating solvent tank 10;

remarks 1: the emptying port 50, the regeneration liquid inlet 51, the washing liquid inlet 52, the pickling liquid inlet 53, the air inlet 55, the water inlet 57, the washing liquid outlet 58, the pickling liquid outlet 59, the regeneration liquid outlet 60, the water outlet 05, the solvent inlet 54 and the solvent outlet 56 which are connected to the bromine element absorption equipment 04 are all connected with the bromine element absorption equipment 04 by valves, and the corresponding valves are opened and closed according to the sequence of the steps of the operation.

The experiment was run using the system described above:

pH	TA	BA	4-CBA	PT acids	Cobalt ion	Manganese ion	Bromine ion	Sodium ion
									4.68	7347	1625	183	452	1296	878	2213	1290

the discharge liquid of the circulating solvent tank 10 of the debenzolization series unit II is as follows:

the discharge liquid of the circulating water washing tank I18 of the washing unit I is as follows (washing step after acid washing):

the liquid discharged from the liquid outlet of the recycling regeneration tank I06 of the regeneration unit I is as follows:

sampling point	pH	TA	BA	4-CBA	PT acid	Bromine ion
							Discharge liquid of circulation regeneration tank I06	12.53	5312	187	66	107	7569

The discharge liquid of the circulating water washing tank I18 of the water washing unit I is as follows (the step of water washing after regeneration):

the effluent from filtration unit ii 46 was analyzed as follows:

sampling point	pH	TA	BA	4-CBA	PT acids	Bromine ion
							Discharge from filtration apparatus II 46	13.88	137	687	247	413	30098

And (4) conclusion: the mixed solution water solution I containing the benzene series and the bromine can absorb the bromine when passing through the bromine absorption equipment 04, meanwhile, benzene series can be adsorbed, after the benzene series on the resin of the bromine element absorption equipment 04 is dissolved in the solvent (92% acetic acid is used in this embodiment), the solvent of the bromine element absorption equipment 04 is discharged, and then the bromine element absorption equipment 04 is washed by water and then the bromine element absorption equipment 04 is regenerated, the benzene-based compound concentration in the regenerated liquid obtained at this time was low (since the benzene-based compound in the bromine element absorption device 04 was dissolved in the solvent in the previous process and discharged from the bromine element absorption device 04), and the composition of the discharged liquid of the filter unit ii 46 was almost the same as that of the discharged liquid of the filter unit ii 46 in the first and second examples, so it was inferred that the same results were obtained in the subsequent steps of the discharged liquid of the filter unit ii 46 in the first and second examples.

Meanwhile, the concentration device in the subsequent step can be combined by one or more of an optional evaporation concentration device (mainly comprising an evaporation tower 41, a reboiler 42), an electrodialysis concentration device 20 or a reverse osmosis concentration device 38.

In other words, after the aqueous solution i is treated, the concentrations of bromine and benzene in the water (the water outlet 05 of the bromine absorption equipment 04) finally discharged from the system are reduced, which is beneficial to the subsequent sewage treatment; meanwhile, the obtained hydrobromic acid can be reused to generate economic value.

Claims

1. The treatment system for the mixed solution containing the benzene series and the bromine is characterized by comprising bromine absorption equipment, a regeneration unit I, a benzene removal unit I or a benzene removal unit II:

the benzene removal unit I is provided with a water inlet and a water outlet, the water outlet of the benzene removal unit I is connected to the water inlet of the bromine element absorption equipment, and the water outlet of the bromine element absorption equipment is discharged out of the system; an outlet of the regeneration unit I is connected to a regeneration liquid inlet of the bromine element absorption equipment, and a regeneration liquid outlet of the bromine element absorption equipment is connected to a circulation regeneration tank I or a regeneration liquid collection tank I of the regeneration unit I;

or the bromine absorption equipment is provided with a water inlet and a water outlet, and the water outlet of the bromine absorption equipment is discharged out of the system; an outlet of the debenzolization unit II is connected to a solvent inlet of the bromine element absorption equipment, and a solvent outlet of the bromine element absorption equipment is connected to a circulating solvent tank or a solvent recovery tank of the debenzolization unit II; the outlet of the regeneration unit I is connected to the regeneration liquid inlet of the bromine element absorption equipment, and the regeneration liquid outlet of the bromine element absorption equipment is connected to the circulation regeneration tank I or the regeneration liquid collection tank I of the regeneration unit I.

2. The treatment system of claim 1, wherein the debenzolization unit i is: benzene series absorption equipment, extraction equipment or acidification equipment.

3. A treatment system according to claim 1 or 2, characterized in that a bipolar membrane electrodialysis device is further provided,

and a liquid outlet of the circulation regeneration tank I or the regeneration liquid collecting tank I is connected to a water inlet of the bipolar membrane electrodialysis equipment.

4. A treatment system according to claim 3, further provided with a concentration device,

5. The treatment system according to claim 3, wherein a filtering device II or a sedimentation tank II is further arranged in front of the water inlet of the bipolar membrane electrodialysis device.

6. The treatment system according to claim 4, wherein a dilute brine outlet of the bipolar membrane electrodialysis device is connected to a water inlet of the concentration device.

7. The treatment system of claim 4 or 6, wherein the concentration device is a reverse osmosis concentration device, an electrodialysis concentration apparatus, or an evaporative concentration device.

8. The processing system of claim 7, further comprising a cooling device:

or a concentrated solution outlet of the evaporation concentration device is connected to a water inlet of the cooling device, a water outlet of the cooling device is connected to a water inlet of a filtering device II or a sedimentation tank II, and a water outlet of the filtering device II or the sedimentation tank II is connected to a water inlet of the bipolar membrane electrodialysis equipment;

or a concentrated solution outlet of the evaporation concentration device is connected to a water inlet of a filtering device II or a sedimentation tank II, a water outlet of the filtering device II or the sedimentation tank II is connected to a water inlet of the cooling device, and a water outlet of the cooling device is connected to a water inlet of the bipolar membrane electrodialysis equipment.

9. The processing system of claim 2,

when the benzene series removing unit I is benzene series absorption equipment, a regeneration unit II is further arranged, an outlet of the regeneration unit II is connected to a regeneration liquid inlet of the benzene series absorption equipment, and a regeneration liquid outlet of the benzene series absorption equipment is connected to a circulating regeneration tank II or a regeneration liquid collecting tank II of the regeneration unit II or is discharged out of the system;

when the benzene series removal unit I is extraction equipment, the extraction equipment comprises an extraction tank, the extraction tank is provided with an extraction liquid inlet, a water outlet and an extraction agent discharge liquid outlet, and the water outlet of the extraction tank is connected to the water inlet of the bromine element absorption equipment; the extractant discharge liquid outlet of the extraction tank is discharged and then is subjected to subsequent treatment; or the extraction equipment comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extraction liquid 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, the outlet of the extraction tank is connected to the inlet of the separation tank, the water outlet of the separation tank is connected to the water inlet of the bromine element absorption equipment, and the extractant discharge liquid outlet of the separation tank of the extraction equipment is discharged for subsequent treatment;

when removing benzene series unit I for acidizing equipment, acidizing equipment contains the acidizing jar, the acidizing jar is equipped with water inlet, delivery port, the delivery port of acidizing jar of acidizing equipment is connected to the water inlet of sedimentation tank I or filter equipment I, the delivery port of sedimentation tank I or filter equipment I is connected to bromine element absorption equipment's water inlet.

10. The treatment system according to claim 1, further comprising a pickling unit I,

the exit linkage of pickling unit I is in the pickle liquor import of bromine element absorption equipment, bromine element absorption equipment's pickle liquor exit linkage is in the circulation pickling jar I or the pickling holding vessel I of pickling unit I or discharge this system.

11. The treatment system according to claim 2, further comprising a pickling unit II,

the outlet of the acid washing unit II is connected to the acid washing liquid inlet of the benzene series absorption equipment, and the acid washing liquid outlet of the benzene series absorption equipment is connected to the circulating acid washing tank II or the acid washing collecting tank II of the acid washing unit II or the system is discharged.

12. The treatment system according to claim 1, wherein a water washing unit I is further provided,

the exit linkage of washing unit I is in the washing liquid import of bromine element absorption equipment, bromine element absorption equipment's washing liquid exit linkage in washing unit I's circulating water washing jar I or washing collecting vessel I or discharge out this system.

13. The treatment system according to claim 2, wherein a water washing unit II is further provided,

or the outlet of the washing unit II is connected to the washing liquid inlet of the benzene series absorption equipment, and the washing liquid outlet of the benzene series absorption equipment is connected to the circulating water washing tank II of the washing unit II or the washing collecting tank II or the system is discharged.

14. The treatment system according to claim 1, 2, 4, 5, 6, 8, 9, 10, 11, 12 or 13, wherein a gas inlet is further provided above the bromine absorption device or the benzene-based material absorption device.

15. The treatment system according to claim 1, 2, 4, 5, 6, 8, 9, 10, 11, 12 or 13, wherein a drain is further provided below the bromine absorption equipment or the benzene-series absorption equipment.

16. The treatment system according to claim 1, further comprising a recovery unit I,

and a discharge port of a circulating solvent tank or a solvent recovery tank of the benzene-series removing unit II is connected to an inlet of the recovery unit I, and a recovered solvent outlet of the recovery unit I is collected or connected to an inlet of the benzene-series removing unit II.

17. The treatment system according to claim 10, wherein a recovery unit II is further provided, a discharge port of the recycle pickling tank I or the pickling collection tank I of the pickling unit I is connected to an inlet of the recovery unit II, and an acid outlet of the recovery unit II is connected to an inlet of the pickling unit I.

18. The treatment system according to claim 11, further comprising a recovery unit III, wherein the discharge port of the recycle pickling tank II or the pickling collection tank II of the pickling unit II is connected to the inlet of the recovery unit III, and the acid outlet of the recovery unit III is connected to the inlet of the pickling unit II.

19. The treatment system according to claim 9, wherein a recovery unit iv is further provided, and an extractant discharge liquid outlet of the extraction tank or the separation tank of the extraction device is connected to an inlet of the recovery unit iv, and an extractant outlet of the recovery unit iv collects or is connected to an extraction liquid inlet of the extraction tank of the extraction device.