A system for treating pta oxidation residue

Abstract

The utility model discloses a kind of processing systems of PTA oxidation residue, the system includes: heating crystallizer I, phthalic acid extraction device, organic matter elimination equipment, still set collection tank, heating crystallizer II, bipolar membrane electrodialysis equipment or evaporation tank.PTA oxidation residue is treated using the system, the value of phthalic acid, benzoic acid, bromine in it is recycled, waste is changed into treasure, simultaneously also avoided the difficulty of sewage treatment brought by the PTA oxidation residue of existing this into sewage system processing, it is favorable to sewage device better operation and environmental protection.

Description

Technical Field

[0001] This utility model belongs to the field of chemical production technology, specifically relating to a PTA oxidation residue treatment system. Background Technology

[0002] The main process of a PTA (purified terephthalic acid) plant is divided into two systems: an oxidation system and a refining system. The oxidation system is used first, followed by the refining system.

[0003] The oxidation system refers to the oxidation reaction in which PX (paraxylene) reacts with oxygen in the air to produce terephthalic acid in an oxidation reactor, with acetic acid as the solvent and a ternary catalyst containing cobalt, manganese, and bromine (hereinafter referred to as the cobalt-manganese-bromine ternary catalyst).

[0004] The refining system refers to the process of hydrogenating the terephthalic acid obtained from the oxidation system to reduce impurities in the terephthalic acid product from the oxidation process and improve the quality of the terephthalic acid product.

[0005] In the oxidation system, a portion is extracted from the oxidation cycle mother liquor (acetic acid as solvent). The main purpose is to remove some impurities from the oxidation cycle mother liquor to prevent the concentration of impurities from accumulating and increasing. Inevitably, the extraction of the oxidation cycle mother liquor also extracts the solvent acetic acid, cobalt-manganese catalyst, and bromine catalyst (which also contain benzene compounds, mainly phthalic acid and benzoic acid). This extracted liquid is first evaporated to recover most of the solvent acetic acid. During the process, the amount of solvent acetic acid decreases and the solute concentration increases. Then, it is further evaporated again in a heated crystallizer (usually a thin-film evaporator) to obtain the oxidation residue. In current technology, sodium carbonate aqueous solution is added to the oxidation residue to dissolve phthalic acid and benzoic acid in the residue, while simultaneously forming cobalt and manganese ions into carbonate insoluble substances for cobalt and manganese recovery, which are then discharged into wastewater. However, this operation has several drawbacks. First, dissolving benzoic acid and phthalic acid with sodium carbonate and having them enter the wastewater is a waste of benzoic acid and phthalic acid, as these substances are valuable. Second, the oxidation residue contains bromide ions, which also end up in the wastewater, wasting the value of the bromide ions. Furthermore, benzoic acid, phthalic acid, and bromide are all detrimental to wastewater treatment plants, making wastewater treatment difficult. Utility Model Content

[0006] The purpose of this invention is to provide a PTA oxidation residue treatment system for deep treatment of the oxidation residue, namely, processing the solid output of the heated crystallizer (i.e., the heated crystallizer I described in this invention, commonly a thin-film evaporator) to recover the material value, mainly referring to the separation and recovery of the phthalic acid, benzoic acid, and bromine value. At the same time, due to the extraction of benzoic acid, phthalic acid, and bromine, the concentration of benzoic acid, phthalic acid, and bromine in the wastewater treatment plant is reduced, which is beneficial to the operation of the wastewater treatment plant.

[0007] A PTA oxidation residue treatment system, the system comprising a heated crystallizer I, a phthalic acid extraction device, an organic matter removal device, and also including a collection tank, a heated crystallizer II, a bipolar membrane electrodialysis device or an evaporator;

[0008] The PTA oxidation residue originates from the heated crystallizer I. The subsequent process involves the PTA oxidation reaction and the extraction of the oxidation mother liquor. Specifically, the PTA oxidation reaction generates an oxidation circulating mother liquor, a solution primarily composed of acetic acid. A small portion of this oxidation circulating mother liquor needs to be discharged outside the system to prevent the accumulation of impurities (which are detrimental to the PTA oxidation reaction) within it. This small discharge stabilizes the concentration of impurities in the oxidation circulating mother liquor. This discharged oxidation circulating mother liquor is called the extracted oxidation mother liquor. Its main component is acetic acid, so it needs to be evaporated and recovered first through an evaporation system. At this point, the solvent in the extracted liquid... The acetic acid content is significantly reduced, thus increasing the proportion of solutes (mainly phthalic acid, benzoic acid, and cobalt, manganese, and bromide ions, which are catalysts for the PTA oxidation reaction). The remaining acetic acid is then evaporated and recovered again in the heated crystallizer I, yielding a solid product known as the PTA oxidation residue. This solid product is the solid substance remaining after the removal of the solvent acetic acid. Generally, the heated crystallizer I is a thin-film evaporator. The main components of the PTA oxidation residue are TA (phthalic acid), BA (benzoic acid), other benzene compounds, a small amount of incompletely evaporated acetic acid, and cobalt, manganese, and bromide ions originally present in the mother liquor (cobalt, manganese, and bromide ions are catalysts for the PTA oxidation reaction).

[0009] The solid outlet of the heated crystallizer I is connected to the inlet of the phthalic acid extraction device, the liquid outlet of the phthalic acid extraction device is connected to the inlet of the mixer I, the mixer I is also provided with a dosing port, the outlet of the mixer I is connected to the inlet of the solid-liquid separator I, and the liquid outlet of the solid-liquid separator I is connected to the inlet of the collection tank, the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, or the inlet of the evaporator.

[0010] Alternatively, the solid outlet of the heated crystallizer I can be connected to the inlet of the phthalic acid extraction device, the liquid outlet of the phthalic acid extraction device can be connected to the inlet of the cobalt-manganese adsorption device, and the outlet of the cobalt-manganese adsorption device can be connected to the inlet of the collection tank, the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, or the inlet of the evaporator.

[0011] The organic matter removal device is located between the liquid outlet of the phthalic acid extraction device and the inlet of the mixer I; or the organic matter removal device is located between the liquid outlet of the phthalic acid extraction device and the inlet of the cobalt-manganese adsorption device; or the organic matter removal device is located between the liquid outlet of the solid-liquid separator I and the inlet of the heated crystallizer II; or the organic matter removal device is located between the liquid outlet of the solid-liquid separator I and the inlet of the bipolar membrane electrodialysis device; or the organic matter removal device is located between the liquid outlet of the solid-liquid separator I and the inlet of the collector. The organic matter removal device is located between the inlet of the collecting tank; or between the liquid outlet of the solid-liquid separator I and the inlet of the evaporator; or between the outlet of the cobalt-manganese adsorption device and the inlet of the heated crystallizer II; or between the outlet of the cobalt-manganese adsorption device and the inlet of the bipolar membrane electrodialysis device; or between the outlet of the cobalt-manganese adsorption device and the inlet of the collecting tank; or between the outlet of the cobalt-manganese adsorption device and the inlet of the evaporator.

[0012] First, the PTA oxidation residue (i.e., the solid outlet of the heated crystallizer I) is mixed with liquid in the mixer I, then filtered to reduce the benzene content in the liquid from the original oxidation residue, while obtaining phthalic acid. The filtrate is then treated with an alkaline substance through the dosing port of the mixer I to remove cobalt and manganese ions as precipitates; or the filtrate is treated with a cobalt and manganese adsorption device to remove cobalt and manganese ions, and the liquid after removing cobalt and manganese ions is directly collected as a sodium bromide aqueous solution; or the liquid after removing cobalt and manganese ions is treated with the heated crystallizer II to crystallize a solid containing sodium bromide as a product for recovery; or the liquid after removing cobalt and manganese ions is treated with a bipolar membrane electrodialysis device to obtain sodium bromide and sodium hydroxide products for recovery; or the liquid after removing cobalt and manganese ions is further treated with the evaporator to obtain hydrobromic acid.

[0013] Meanwhile, in order to further reduce the benzene series compound content in the final collection tank's sodium bromide aqueous solution product, the liquid entering the heated crystallizer II, the liquid entering the evaporator, or the liquid entering the bipolar membrane electrodialysis device, there are two methods:

[0014] Firstly, the filtrate obtained after mixing and solid-liquid separation in mixer I is further treated by the organic matter removal device to remove benzene compounds. The liquid after removing benzene compounds is then passed through mixer I (where alkaline substances are added at the dosing port to precipitate cobalt and manganese ions) or the cobalt and manganese adsorption device to adsorb the cobalt and manganese ions. Both of these methods help reduce the benzene content in the liquid that finally enters the heated crystallizer II, the bipolar membrane electrodialysis device, the collection tank, or the evaporator.

[0015] Secondly, the filtrate obtained after mixing and solid-liquid separation in mixer I (i.e., precipitation of cobalt and manganese ions) is further treated by the organic matter removal device to remove benzene compounds. The liquid after removing the benzene compounds is then processed by the heated crystallizer II, the bipolar membrane electrodialysis device, the evaporator, or collected in a collection tank. Alternatively, the solution after the cobalt and manganese ions have been adsorbed by the cobalt and manganese adsorption device is further treated by the organic matter removal device to remove benzene compounds. The liquid after removing the benzene compounds is then processed by the heated crystallizer II, the bipolar membrane electrodialysis device, the evaporator, or collected in a collection tank.

[0016] Based on the above system, preferably, the dosing port of the mixer I is used to add a solid or aqueous solution of an alkaline substance, which is mainly sodium hydroxide, sodium bicarbonate, sodium carbonate, potassium hydroxide, potassium bicarbonate, potassium carbonate, etc.

[0017] Based on the above system, preferably, the dosing port of the mixer I is used to add a solid or aqueous solution of an alkaline substance. The alkaline substance is mainly sodium hydroxide, sodium bicarbonate, sodium carbonate, potassium hydroxide, potassium bicarbonate, potassium carbonate, etc. After adding the alkaline substance, the insoluble salts of cobalt and manganese ions are filtered out in the solid-liquid separator I, and then dissolved by adding acid. The acid is preferably acetic acid and / or hydrobromic acid.

[0018] Based on the above system, preferably, the dosing port of the mixer I is used to add a solid or aqueous solution of an alkaline substance. The alkaline substance is mainly sodium hydroxide, sodium bicarbonate, sodium carbonate, potassium hydroxide, potassium bicarbonate, potassium carbonate, etc. After adding the alkaline substance, the insoluble salts of cobalt and manganese ions are filtered out in the solid-liquid separator I, and then dissolved by adding acid. The acid is preferably acetic acid and / or hydrobromic acid. After the cobalt and manganese ions are dissolved by acid, they are connected to the oxidation reaction of PTA, which is equivalent to the recovery of cobalt and manganese ions.

[0019] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with filler material that has an adsorption effect on cobalt-manganese ions.

[0020] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with a packing material that adsorbs cobalt-manganese ions, and after the packing material is saturated with cobalt-manganese ions, it is regenerated with acid.

[0021] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with a packing material that adsorbs cobalt-manganese ions. After the packing material is saturated with adsorbed cobalt-manganese ions, it is regenerated with an acid solution, preferably acetic acid and / or hydrobromic acid.

[0022] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with a packing material that adsorbs cobalt-manganese ions. After the packing material is saturated with adsorbed cobalt-manganese ions, it is regenerated with acid. Before and / or after acid regeneration, the packing material needs to be washed with water and / or acid washed.

[0023] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with packing material that adsorbs cobalt-manganese ions. After the packing material is saturated with adsorbed cobalt-manganese ions, it is regenerated with acid solution. The acid is preferably acetic acid and / or hydrobromic acid. The acid regeneration solution is connected to the oxidation reaction of PTA, which is equivalent to the recovery of cobalt-manganese ions.

[0024] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with a filler that adsorbs cobalt-manganese ions, and the filler is preferably a resin that adsorbs cobalt-manganese.

[0025] Based on the above system, preferably, the cobalt-manganese adsorption device is filled with a filler that has an adsorption effect on cobalt-manganese ions. The filler is a resin that has an adsorption effect on cobalt-manganese, preferably a chelating resin.

[0026] Based on the above system, preferably, the organic matter elimination equipment refers to a benzene series adsorption equipment or an incineration equipment.

[0027] Based on the above system, preferably, the benzene series adsorption device is filled with packing material that has an adsorption effect on benzene series compounds.

[0028] Based on the above system, preferably, the benzene series adsorption device is filled with packing material that has an adsorption effect on benzene series compounds, and after the packing material is saturated with benzene series compounds, it is regenerated with an alkaline solution.

[0029] Based on the above system, preferably, the benzene series adsorption device is filled with packing material that has an adsorption effect on benzene series compounds. After the packing material is saturated with benzene series compounds, it is regenerated with an alkaline solution, and the regenerated liquid is discharged to a wastewater treatment device for treatment.

[0030] Based on the above system, preferably, the benzene series adsorption device is filled with packing material that has an adsorption effect on benzene series compounds. After the packing material is saturated with benzene series compounds, it is regenerated with an alkaline solution, preferably a sodium hydroxide solution.

[0031] Based on the above system, preferably, the benzene series adsorption equipment is filled with packing material that has an adsorption effect on benzene series compounds. After the packing material is saturated with benzene series compounds, it is regenerated with an alkaline solution. Before and / or after the alkaline solution regeneration, the packing material needs to be washed with water and / or acid washed.

[0032] Based on the above system, preferably, the benzene series adsorption device is filled with a filler that has an adsorption effect on benzene series compounds, and the filler is preferably a resin that has an adsorption effect on benzene series compounds.

[0033] Based on the above system, preferably, the benzene series adsorption device is filled with a packing material that has an adsorption effect on benzene series compounds. The packing material is a resin that has an adsorption effect on benzene series compounds, preferably a macroporous adsorption resin.

[0034] Based on the above system, preferably, the incineration equipment refers to equipment that uses incineration to burn off organic matter completely. After the organic matter reaches a certain temperature, the organic matter will be completely burned off.

[0035] Based on the above system, preferably, the incineration equipment also requires external fuel, such as methanol, natural gas, etc.

[0036] Based on the above system, preferably, the heating crystallizer II refers to a device that can evaporate liquid to obtain crystalline solid.

[0037] Based on the above system, preferably, the heating crystallizer II refers to a device that can evaporate liquid to obtain crystalline solid, and its main heat source is steam and / or electricity.

[0038] Based on the above system, preferably, the heating crystallizer II refers to a device that can evaporate liquid to obtain crystalline solid, preferably a multi-effect evaporator, MVR or other similar device, and is also equipped with a centrifuge.

[0039] Based on the above system, preferably, the heating crystallizer II refers to a device that can evaporate liquid to obtain crystalline solid, preferably a multi-effect evaporator, MVR or other similar device, and also includes necessary conventional components such as heaters, instruments, and control valves attached to conventional multi-effect evaporators and MVR devices; at the same time, MVR also includes a steam compressor.

[0040] Based on the above system, preferably, the bipolar membrane electrodialysis equipment is a device that can convert salt into corresponding acid and alkali under the action of an electric field. For example, in this case, the influent is a sodium bromide aqueous solution. After being treated by the bipolar membrane electrodialysis equipment, it will produce two products: acid (hydrobromic acid) and alkali (sodium hydroxide), and at the same time, a low-concentration brine (i.e., sodium bromide dilute brine) will be generated.

[0041] Based on the above system, preferably, the benzene series compounds refer to benzene and benzene derivatives and organic compounds containing benzene rings contained in the system, such as TA (phthalic acid), BA (benzoic acid), etc.

[0042] Based on the above system, preferably, the phthalic acid extraction device includes a mixer II and a solid-liquid separator II;

[0043] The inlet of the mixer II is the inlet of the phthalic acid extraction device. The mixer II is also provided with a liquid inlet. The outlet of the mixer II is connected to the inlet of the solid-liquid separator II. The liquid outlet of the solid-liquid separator II is the liquid outlet of the phthalic acid extraction device.

[0044] The main purpose of the phthalic acid extraction device is to separate phthalic acid and benzoic acid in the PTA oxidation residue. A solvent is added to the inlet of the mixer II to dissolve most of the benzoic acid, while most of the phthalic acid remains undissolved. Therefore, after separation by the solid-liquid separator II, the solid obtained is mainly composed of phthalic acid, and the liquid obtained is a filtrate of the solvent that has dissolved the benzoic acid, thus achieving the separation of phthalic acid and benzoic acid.

[0045] Based on the above system, preferably, a solvent is added to the inlet of the mixer II. The solvent is preferably hot water at 50-120°C, and more preferably hot water at 90-100°C. Benzoic acid has a certain solubility in hot water, while phthalic acid has extremely low solubility, thus achieving the separation of phthalic acid and benzoic acid.

[0046] Based on the above system, preferably, an organic solvent is added to the inlet of the mixer II. The solvent is preferably a solvent that is insoluble in terephthalic acid but soluble in terebenzoic acid.

[0047] Based on the above system, preferably, an organic solvent is added to the inlet of the mixer II. The solvent is preferably methanol, ethanol, benzene, toluene, xylene, acetic acid, etc.

[0048] Based on the above system, preferably, a benzoic acid extraction device is also provided; the liquid outlet of the benzoic acid extraction device is connected to the inlet of the benzoic acid extraction device, and the liquid outlet of the benzoic acid extraction device is connected to the inlet of the mixer I, the inlet of the cobalt-manganese adsorption device, or the inlet of the organic matter elimination device.

[0049] Based on the above system, preferably, the benzoic acid extraction device includes: a cooling device and a filtration device I; a concentration device and a filtration device I; a concentration device, a cooling device, and a filtration device I; an integrated cooling and filtration machine; or an integrated concentration device and a cooling and filtration machine, specifically:

[0050] The inlet of the cooling equipment is the same as the inlet of the benzoic acid extraction device, and the outlet of the cooling equipment is connected to the inlet of the filtration device I. The liquid outlet of the filtration device I is the same as the liquid outlet of the benzoic acid extraction device.

[0051] The inlet of the concentration device is the same as the inlet of the benzoic acid extraction device, the outlet of the concentration device is connected to the inlet of the filtration device I, and the liquid outlet of the filtration device I is the same as the liquid outlet of the benzoic acid extraction device;

[0052] The inlet of the concentration equipment is the same as the inlet of the benzoic acid extraction device. The outlet of the concentration equipment is connected to the inlet of the cooling equipment. The outlet of the cooling equipment is connected to the inlet of the filtration device I. The liquid outlet of the filtration device I is the same as the liquid outlet of the benzoic acid extraction device.

[0053] The inlet of the cooling equipment is the same as the inlet of the benzoic acid extraction device, the outlet of the cooling equipment is connected to the inlet of the concentration equipment, the outlet of the concentration equipment is connected to the inlet of the filtration device I, and the liquid outlet of the filtration device I is the same as the liquid outlet of the benzoic acid extraction device.

[0054] The inlet of the integrated cooling and filtration unit is the same as the inlet of the benzoic acid extraction device, and the liquid outlet of the integrated cooling and filtration unit is the same as the liquid outlet of the benzoic acid extraction device.

[0055] The inlet of the concentration equipment is the same as the inlet of the benzoic acid extraction device, the outlet of the concentration equipment is connected to the inlet of the integrated cooling and filtration machine, and the liquid outlet of the integrated cooling and filtration machine is the same as the liquid outlet of the benzoic acid extraction device.

[0056] When hot water is used as the solvent for benzoic acid (i.e., hot water is added as the solvent to the inlet of the mixer II; hot water dissolves benzoic acid but not phthalic acid, and is used to separate benzoic acid and phthalic acid), the main solute in the filtrate of the solid-liquid separator II is benzoic acid. Cooling can reduce the solubility of benzoic acid in water. The solubility of benzoic acid in water decreases as the temperature decreases, so lowering the water temperature can precipitate benzoic acid into a solid, which is then used as the benzoic acid product. At the same time, the purpose of concentration is to reduce the amount of solvent (water) and increase the amount of benzoic acid precipitated.

[0057] Based on the above system, preferably, the benzoic acid extraction device includes: a mixer III and a filtration device II, specifically:

[0058] The inlet of the mixer III is the inlet of the benzoic acid extraction device. The mixer III is also provided with a liquid inlet. The outlet of the mixer III is connected to the inlet of the filter device II. The liquid outlet of the filter device II is the liquid outlet of the benzoic acid extraction device.

[0059] An organic solvent is added to the inlet of the mixer II. The solvent is preferably an organic solvent that is insoluble in terephthalic acid but soluble in benzoic acid. At this time, benzoic acid dissolves in the organic solvent, while terephthalic acid does not dissolve. After the terephthalic acid is separated and removed by the solid-liquid separator II, the remaining filtrate of the solid-liquid separator II is a mixed solution of organic solvent and benzoic acid. By adding another liquid (such as water), the concentration of the organic solvent can be reduced. After the concentration of the organic solvent is reduced, the solubility of benzoic acid in it decreases, and the benzoic acid can be filtered out as a product by the filtration device II.

[0060] Based on the above system, preferably, the benzoic acid extraction device includes: a heating crystallizer III, specifically:

[0061] The inlet of the heating crystallizer III is the inlet of the benzoic acid extraction device. The solid outlet of the heating crystallizer III is connected to the inlet of the washing tank I. The washing tank I is also provided with a washing liquid inlet. The outlet of the washing tank I is connected to the inlet of the filtration device III. The liquid outlet of the filtration device III is the liquid outlet of the benzoic acid extraction device.

[0062] Alternatively, the inlet of the heating crystallizer III may be the inlet of the benzoic acid extraction device, the solid outlet of the heating crystallizer III may be connected to the inlet of the washing and filtering integrated machine I, the washing and filtering integrated machine I may also be provided with a washing liquid inlet, and the liquid outlet of the washing and filtering integrated machine I may be the liquid outlet of the benzoic acid extraction device.

[0063] Alternatively, the inlet of the heating crystallizer III may be the inlet of the benzoic acid extraction device. The heating crystallizer III may also be provided with a washing liquid inlet. The outlet of the heating crystallizer III may be connected to the inlet of the filtration device III. The liquid outlet of the filtration device III may be the liquid outlet of the benzoic acid extraction device.

[0064] The process involves adding a liquid (such as water) to benzoic acid for washing. After washing and filtering, the resulting solid is the benzoic acid solid product, while the liquid is a solution containing ions (such as cobalt, manganese, and bromide ions) from the washed-off benzoic acid solid.

[0065] Based on the above system, preferably, the benzoic acid extraction device includes: a heating crystallizer III and a washing tank II, specifically:

[0066] The inlet of the washing tank II is the inlet of the benzoic acid extraction device. The washing tank II is also provided with a washing liquid inlet. The aqueous phase outlet of the washing tank II is the liquid outlet of the benzoic acid extraction device. The oil phase outlet of the washing tank II is connected to the inlet of the heating crystallizer III. The solid outlet of the heating crystallizer III collects benzoic acid product.

[0067] Before passing through the heating crystallizer III, the solution is first washed in the washing tank II (e.g., using water as the washing solution) to remove ions (such as cobalt, manganese, and bromine ions) from the solution. The solution is then separated into layers through the aqueous phase outlet of the washing tank II (the aqueous solution contains cobalt, manganese, and bromine ions). The oil phase outlet is heated in the heating crystallizer III to remove the organic solvent, resulting in a solid benzoic acid product.

[0068] Based on the above system, preferably, the organic solvent heated in the gas phase of the heating crystallizer III is cooled and then turned into a liquid for reuse (the solvent added to the inlet of the mixer II is reused as a solvent).

[0069] Based on the above system, preferably, the gas phase heating outlet of the heating crystallizer III is connected to the inlet of the cooler. After the benzoic acid vapor passes through the cooler and its temperature is reduced, solid benzoic acid product is precipitated.

[0070] Based on the above system, preferably, the solid outlet of the filter device I, the solid outlet of the cooling filter integrated machine, the solid outlet of the filter II, the solid outlet of the filter III, or the solid outlet of the washing filter integrated machine I mainly contains benzoic acid, requiring an additional washing process to regenerate and deeply wash the benzoic acid.

[0071] Based on the above system, preferably, the solid outlet of the filter device I, the solid outlet of the integrated cooling filter, the solid outlet of the filter II, the solid outlet of the filter III, or the solid outlet of the integrated washing filter I mainly contains benzoic acid, requiring an additional washing process to regenerate and deeply wash the benzoic acid. Generally, washing with water is sufficient.

[0072] Based on the above system, preferably, the main purpose of washing benzoic acid is to remove cobalt, manganese, and bromide ions, thereby improving the purity of benzoic acid. At the same time, the cobalt, manganese, and bromide ions are washed off to facilitate their subsequent recovery and prevent their loss. In addition, the above washing includes at least one washing operation, and in actual operation, multiple washing operations are generally performed.

[0073] Based on the above system, preferably, the main purpose of washing benzoic acid is to remove cobalt, manganese, and bromide ions, thereby improving the purity of benzoic acid. At the same time, the cobalt, manganese, and bromide ions are also washed off to facilitate their subsequent recovery and prevent their loss. In addition, the above washing includes at least one washing operation, but in actual operation, multiple washing operations are generally performed. The water used in the later washing can be reused in the previous washing, which can save water consumption and minimize the amount of washing wastewater generated.

[0074] Based on the above system, preferably, the washing wastewater can be discharged to a sewage treatment plant, or it can be connected to the inlet of the mixer II, the inlet of the overnight separator II, the inlet of the cooling device I, the inlet of the mixer III, or the inlet of the heating crystallizer III for reuse, thereby increasing the recovery rate of benzoic acid.

[0075] Based on the above system, preferably, the benzoic acid product is packaged in the form of slices or other methods as the final benzoic acid product and sold to the factory.

[0076] Based on the above system, preferably, a nanofiltration system I is also provided;

[0077] The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the nanofiltration system I. The freshwater outlet of the nanofiltration system I is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporator.

[0078] Alternatively, the inlet of the organic matter removal device can be connected to the inlet of the nanofiltration system I, and the freshwater outlet of the nanofiltration system I can be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

[0079] The nanofiltration system I is mainly composed of a nanofiltration membrane, along with necessary components such as a membrane housing, a high-pressure pump, and control valves. The nanofiltration membrane is a membrane device that can separate monovalent and divalent ions. For example, in this case, carbonate ions (sodium carbonate) in the water are intercepted at the concentrate stage of the nanofiltration membrane, while bromide ions (sodium bromide) in the water are allowed to pass through the nanofiltration membrane at the freshwater stage, thus achieving the separation of sodium bromide and sodium carbonate.

[0080] If sodium bicarbonate is present in the water, it is also a monovalent anion and will pass through the nanofiltration membrane, just like sodium bromide, and will be measured in nanofiltration freshwater.

[0081] That is, after treatment by the nanofiltration system I, sodium carbonate is first removed (measured in the concentrate of the nanofiltration system I), and only the aqueous solution with sodium bromide as the main component (the desalinated water of the nanofiltration system I) is passed through. Finally, the solution is collected in the collection tank to form an aqueous solution of sodium bromide, crystallized in the heating crystallizer II to obtain a solid sodium bromide product, passed through the evaporator to obtain a hydrobromic acid product, or processed by the bipolar membrane electrodialysis equipment to obtain two products: hydrobromic acid and sodium hydroxide.

[0082] Based on the above system, preferably, the concentrate outlet of nanofiltration system I, i.e., the concentrate of nanofiltration system I, refers to the concentrate of the nanofiltration membrane of nanofiltration system I (which mainly contains ions intercepted by the nanofiltration membrane); the desalination outlet of nanofiltration system I, i.e., the desalination of nanofiltration system I, refers to the desalination of the nanofiltration membrane of nanofiltration system I (which mainly contains ions that permeate through the nanofiltration membrane).

[0083] Based on the above system, preferably, it also includes a heating evaporation device I and a solid-liquid separator VI.

[0084] The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporation tank.

[0085] Alternatively, the inlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank.

[0086] The purpose of using the heating evaporation equipment I and the solid-liquid separator VI is to first evaporate a portion of the water from the solution using the heating evaporation equipment I, thus concentrating the solute. At this point, the solubility of sodium carbonate decreases, while sodium bromide still has a relatively high solubility (the separation is mainly based on the difference in solubility between sodium carbonate and sodium bromide). Then, using the solid-liquid separator VI, a solid salt mainly containing sodium carbonate and an aqueous solution containing sodium bromide (the filtrate from the solid-liquid separator VI) can be obtained. That is, after the treatment by the heating evaporation equipment I and the solid-liquid separator VI, the sodium carbonate solid is removed first, and only the aqueous solution mainly containing sodium bromide is collected in the collection tank to form a sodium bromide aqueous solution. After crystallization by the heating crystallizer II, sodium bromide solid product is obtained. After treatment by the bipolar membrane electrodialysis equipment, hydrobromic acid and sodium hydroxide products are obtained, or hydrobromic acid product is obtained by the evaporation tank.

[0087] Based on the above system, preferably, an alkali addition pipeline I or a heating device I is also provided;

[0088] The alkali addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the nanofiltration system I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the nanofiltration system I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the organic matter removal device and the inlet of the nanofiltration system I, and the connection point is called connection point a.

[0089] Alternatively, the outlet of the organic matter removal device, the liquid outlet of the solid-liquid separator I, or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating device I, and the outlet of the heating device I may be connected to the inlet of the nanofiltration system I;

[0090] The function of the alkali addition line I is to provide alkali, namely sodium hydroxide, to convert sodium bicarbonate in the source water into sodium carbonate. This prevents sodium bicarbonate from passing through the nanofiltration membrane in nanofiltration system I into the fresh water of nanofiltration system I. The addition of sodium hydroxide converts sodium bicarbonate into sodium carbonate, which is then intercepted by the nanofiltration membrane in nanofiltration system I at the concentrate level. This results in a higher purity sodium bromide aqueous solution (nanofiltration fresh water) that no longer contains the originally high concentration of sodium bicarbonate.

[0091] The function of heating device I is to heat sodium bicarbonate into sodium carbonate and carbon dioxide. The carbon dioxide dissipates, achieving the same purpose as adding alkali, namely, converting sodium bicarbonate into sodium carbonate, which is beneficial for the subsequent separation by nanofiltration system I.

[0092] Based on the above system, preferably, an alkali addition pipeline I or a heating device I is also provided;

[0093] The alkali addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the heating evaporation device I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the heating evaporation device I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the organic matter removal device and the inlet of the heating evaporation device I, and the connection point is called connection point a.

[0094] Alternatively, the outlet of the organic matter removal device, the liquid outlet of the solid-liquid separator I, or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating device I, and the outlet of the heating device I may be connected to the inlet of the heating evaporation device I;

[0095] The function of the alkali addition pipeline I is to provide alkali, namely sodium hydroxide, to convert sodium bicarbonate in the source water into sodium carbonate by adding sodium hydroxide. The sodium carbonate is then separated by the solid-liquid separator VI to obtain solid sodium carbonate.

[0096] The function of heating device I is to heat sodium bicarbonate into sodium carbonate and carbon dioxide. The carbon dioxide dissipates, achieving the same purpose as adding alkali, namely, converting sodium bicarbonate into sodium carbonate.

[0097] Based on the above system, preferably, an acid addition pipeline I is also provided;

[0098] The acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the heated crystallizer II, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the bipolar membrane electrodialysis device, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the organic matter removal device, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the collection tank, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the evaporator, and the connection point is called connection point b.

[0099] Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the heated crystallizer II, with the acid addition line I connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the bipolar membrane electrodialysis device, with the acid addition line I connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the organic matter removal device. Between the inlets and outlets, the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is set between the freshwater outlet of the nanofiltration system I and the inlet of the collection tank, and the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is set between the freshwater outlet of the nanofiltration system I and the inlet of the evaporator, and the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b;

[0100] The purpose of the acid addition line I is to add acid. Acid addition can react with the small amount of sodium carbonate and / or sodium bicarbonate that still exist in the freshwater of the nanofiltration system I (i.e., permeate through the nanofiltration membrane) to generate carbon dioxide. The carbon dioxide will then dissipate, which helps to reduce the concentration of sodium carbonate and / or sodium bicarbonate in the freshwater of the nanofiltration system I and improve the purity of sodium bromide.

[0101] Based on the above system, preferably, the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separation device I and the inlet of the organic matter removal device, and the connection position is called connection point e; or the acid addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, and the connection position is called connection point e;

[0102] Alternatively, a decarbonization tower I may be installed, located between the liquid outlet of the solid-liquid separation device I and the inlet of the organic matter removal device, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separation device I and the inlet of the decarbonization tower I; the connection point is referred to as connection point e.

[0103] The purpose of the acid addition line I is to add acid. Adding acid can react sodium carbonate and sodium bicarbonate with the acid to generate carbon dioxide that escapes into the air, which is beneficial to improving the purity of sodium bromide. Furthermore, for the organic matter removal equipment (when selecting benzene series adsorption equipment), lowering the pH of the aqueous solution is beneficial for the organic matter removal equipment to adsorb organic matter (benzene series).

[0104] Based on the above system, preferably, the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the heated crystallizer II, and the connection position is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the bipolar membrane electrodialysis device, and the connection position is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the organic matter removal device, and the connection position is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the collection tank, and the connection position is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the evaporator, and the connection position is called connection point b.

[0105] Alternatively, a decarbonization tower I can be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the heated crystallizer II, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I can be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the bipolar membrane electrodialysis equipment, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I can be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the organic matter removal equipment. Between the inlets and outlets, the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is provided, which is located between the liquid outlet of the solid-liquid separator VI and the inlet of the collection tank, and the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is provided, which is located between the liquid outlet of the solid-liquid separator VI and the inlet of the evaporator, and the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I, and the connection point is called connection point b;

[0106] The purpose of the acid addition line I is to add acid. Acid addition can react the small amount of sodium carbonate and / or sodium bicarbonate still present in the liquid outlet of the solid-liquid separator VI to generate carbon dioxide. The carbon dioxide escapes, which helps to reduce the concentration of sodium carbonate and / or sodium bicarbonate in the fresh water of the nanofiltration system I and improve the purity of sodium bromide.

[0107] Based on the above system, preferably, the acid production pipeline of the bipolar membrane electrodialysis equipment is connected to the hydrobromic acid demand point of the PTA unit.

[0108] Based on the above system, preferably, the acid production pipeline of the bipolar membrane electrodialysis equipment is connected to the hydrobromic acid demand point user of the PTA unit, preferably the PTA oxidation batching tank or the PTA oxidation circulating mother liquor tank.

[0109] Based on the above system, preferably, the heating device I is a device for heating the aqueous solution, preferably a heat exchanger.

[0110] Based on the above system, preferably, the heating device I is a device for heating aqueous solution, preferably a heat exchanger, and the heat source is preferably steam or electricity.

[0111] Based on the above system, preferably, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporation tank. After being processed by the heating evaporation device I and the solid-liquid separator VI, the solubility of sodium carbonate and sodium bicarbonate is relatively low compared to that of sodium bromide. Therefore, evaporation is a process of concentration. After the amount of solvent water is greatly reduced, sodium carbonate and sodium bicarbonate are preferentially precipitated and can be removed by filtration. The filtrate is sodium bromide. That is to say, the separation of sodium carbonate, sodium bicarbonate, and sodium bromide is achieved by the heating evaporation device I and the solid-liquid separator VI.

[0112] Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. After processing by the heating evaporation device I and the solid-liquid separator VI, the solubility of sodium carbonate and sodium bicarbonate is relatively low compared to that of sodium bromide. Therefore, evaporation leads to concentration. After the amount of solvent water is greatly reduced, sodium carbonate and sodium bicarbonate are preferentially precipitated and can be removed by filtration. The filtrate is sodium bromide. That is to say, the separation of sodium carbonate, sodium bicarbonate, and sodium bromide is achieved by the heating evaporation device I and the solid-liquid separator VI.

[0113] The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the cooling device '. The outlet of the cooling device ' is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. After being processed by the heating evaporation device I and the solid-liquid separator VI, the solubility of sodium carbonate and sodium bicarbonate is much lower than that of sodium bromide. Therefore, after evaporation, the product is concentrated. After the amount of solvent water is greatly reduced, sodium carbonate and sodium bicarbonate are preferentially precipitated. After cooling, the solubility of sodium carbonate and sodium bicarbonate is further reduced significantly, while the solubility of sodium bromide does not change much with the decrease in temperature. It can be removed by filtration, and the filtrate is sodium bromide. That is to say, the separation of sodium carbonate, sodium bicarbonate, and sodium bromide is achieved by the heating evaporation device I, the cooling device ', and the solid-liquid separator VI.

[0114] Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. After being processed by the heating evaporation device I and the solid-liquid separator VI, the solubility of sodium carbonate and sodium bicarbonate is much lower than that of sodium bromide. Therefore, after evaporation, the solution is concentrated. After the amount of solvent water is greatly reduced, sodium carbonate and sodium bicarbonate are preferentially precipitated. After cooling, the solubility of sodium carbonate and sodium bicarbonate is further reduced significantly, while the solubility of sodium bromide does not change much with the decrease in temperature. It can be removed by filtration, and the filtrate is sodium bromide. That is to say, the separation of sodium carbonate, sodium bicarbonate, and sodium bromide is achieved by the heating evaporation device I, the cooling device ', and the solid-liquid separator VI.

[0115] Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device can be connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I can be connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II. The freshwater outlet of the nanofiltration system II can be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. That is, the sodium carbonate in the sodium bromide aqueous solution is intercepted again by the nanofiltration system II at the concentrate of the nanofiltration system II, which is equivalent to removing the sodium carbonate in the sodium bromide aqueous solution again.

[0116] Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; that is, the sodium carbonate in the sodium bromide aqueous solution is intercepted again by the nanofiltration system II in the concentrate of the nanofiltration system II, which is equivalent to removing the sodium carbonate in the sodium bromide aqueous solution again.

[0117] Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device can be connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I can be connected to the inlet of the cooling device '. The outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II. The freshwater outlet of the nanofiltration system II can be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. That is, the sodium carbonate in the sodium bromide aqueous solution is intercepted again by the nanofiltration system II at the concentrate of the nanofiltration system II, which is equivalent to removing the sodium carbonate in the sodium bromide aqueous solution again.

[0118] Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; that is, the sodium carbonate in the sodium bromide aqueous solution is intercepted again by the nanofiltration system II in the concentrated water of the nanofiltration system II, which is equivalent to removing the sodium carbonate in the sodium bromide aqueous solution again.

[0119] Based on the above system, preferably, it is also equipped with an alkali addition pipeline II and a heating device II or an acid addition pipeline II;

[0120] The alkali addition pipeline II is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the nanofiltration system II, and the connection point is called connection point c;

[0121] Alternatively, the heating device II may be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the nanofiltration system II;

[0122] Alternatively, the acid addition line II can be connected between the liquid outlet of the solid-liquid separator VI and the inlet of the nanofiltration system II, and the connection point is called connection point d;

[0123] The purpose of the alkali addition line II is to convert the sodium bicarbonate in the liquid outlet of the solid-liquid separator VI back into sodium carbonate, which is then used for further separation by the nanofiltration system II. This is because the nanofiltration membrane can intercept divalent ions (carbonate ions), and if monovalent sodium bicarbonate cannot be intercepted, it needs to be converted into sodium carbonate.

[0124] The purpose of acid addition line II is to neutralize free hydroxide ions in the solution with acid.

[0125] Based on the above system, preferably, the nanofiltration system I or the nanofiltration system II includes a single-stage nanofiltration system, a single-stage multi-stage nanofiltration system, a multi-stage single-stage nanofiltration system, or a multi-stage multi-stage nanofiltration system;

[0126] For example, if the fresh water from the first nanofiltration stage is then treated by a second nanofiltration stage, the purpose is to further reduce the sodium carbonate content still present in the first nanofiltration fresh water (an aqueous solution of sodium bromide). This is called the second nanofiltration stage.

[0127] For example, if the concentrate from the first-stage nanofiltration is then treated by a second nanofiltration process, the purpose is to further compress and concentrate the sodium carbonate in the first-stage nanofiltration concentrate, thereby increasing the concentration of sodium carbonate. This is called two-stage nanofiltration.

[0128] Based on the above system, preferably, the alkali addition pipeline I or the alkali addition pipeline II is connected to the alkali pipeline for providing sodium hydroxide.

[0129] Based on the above system, preferably, the alkali supply line I or the alkali supply line II is connected to the alkali supply line to provide sodium hydroxide. This alkali supply line is preferably the alkali production line of the bipolar membrane electrodialysis equipment, that is, the sodium hydroxide produced by the bipolar membrane electrodialysis equipment is recycled back to the alkali supply line I or the alkali supply line II; if the sodium hydroxide produced by the bipolar membrane electrodialysis equipment is insufficient, more fresh external alkali is supplied.

[0130] Based on the above system, preferably, the acid addition line I or the acid addition line II is connected to the acid supply line to provide hydrobromic acid and / or acetic acid.

[0131] Based on the above system, preferably, the acid addition line I or the acid addition line II is connected to the acid production line for providing hydrobromic acid and / or acetic acid. This acid line is preferably the acid production line of the bipolar membrane electrodialysis equipment, that is, a portion of the hydrobromic acid produced by the bipolar membrane electrodialysis equipment is recycled back to the acid addition line I or the acid addition line II; the other portion of the hydrobromic acid is used as the target product of this device.

[0132] Based on the above system, preferably, a concentration system II and / or a concentration system III are also provided;

[0133] The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the nanofiltration system I, the inlet of the heating device I, the inlet of the organic matter removal device, the inlet of the heating evaporation device I, connection point a, connection point b, or connection point e.

[0134] Alternatively, the outlet of the cobalt-manganese adsorption device can be connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II can be connected to the inlet of the nanofiltration system I, the inlet of the heating device I, the inlet of the organic matter removal device, the inlet of the heating evaporation device I, connection point a, connection point b, or connection point e.

[0135] Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II can be connected to the inlet of the nanofiltration system I, the inlet of the heating device I, the inlet of the organic matter removal device, the inlet of the heating evaporation device I, connection point a or connection point b;

[0136] Alternatively, connection point a can be connected to the inlet of the concentration system II, and the concentrate outlet of the concentration system II can be connected to the inlet of the nanofiltration system I or the inlet of the heating evaporation device I;

[0137] Alternatively, the outlet of heating device I can be connected to the inlet of concentration system II, and the concentrate outlet of concentration system II can be connected to the inlet of nanofiltration system I or the inlet of heating evaporation device I;

[0138] Alternatively, the freshwater outlet of nanofiltration system I can be connected to the inlet of concentration system III, and the concentrate outlet of concentration system III can be connected to the inlet of heated crystallizer II, the inlet of bipolar membrane electrodialysis equipment, the inlet of collection tank, the inlet of evaporator, connection point b, or the inlet of organic matter removal equipment;

[0139] Alternatively, the freshwater outlet of nanofiltration system II can be connected to the inlet of concentration system III, and the concentrate outlet of concentration system III can be connected to the inlet of heated crystallizer II, the inlet of bipolar membrane electrodialysis equipment, the inlet of collection tank, the inlet of evaporator, connection point b, or the inlet of organic matter removal equipment.

[0140] Alternatively, the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III may be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, the connection point b, or the inlet of the organic matter removal device.

[0141] Alternatively, the outlet of the decarbonization tower I can be connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III can be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, the connection point b, or the inlet of the organic matter removal device;

[0142] Alternatively, the outlet of connection point b can be connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III can be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

[0143] Alternatively, the outlet of the organic matter removal device may be connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III may be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

[0144] Based on the above system, preferably, the evaporator is further equipped with a heater and a dosing port; the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator; the dosing port of the evaporator allows for the addition of two types of chemical agents:

[0145] One method involves adding a non-volatile acid. This method utilizes the principle of converting non-volatile acids into volatile acids. A non-volatile acid (such as sulfuric acid or phosphoric acid) is added to the dosing port of the evaporator and heated to convert sodium bromide + sulfuric acid (or phosphoric acid, etc.) into hydrobromic acid, which is then heated and evaporated into a gaseous phase. The hydrobromic acid is then collected in the collection tank or absorbed by the water absorption acid generator to form an aqueous solution.

[0146] Another method involves adding an oxidizing agent (such as chlorine, or sodium hypochlorite + hydrochloric acid, hydrogen peroxide, etc.) to oxidize the sodium bromide into bromine, which is then heated and evaporated to obtain bromine vapor, and collected in the collection tank (the vapor phase of bromine must first be liquefied by cooling).

[0147] Based on the above system, preferably, the liquid outlet of the water absorption acid generator is further provided with a heater, or the liquid outlet of the water absorption acid generator is connected to the inlet of the evaporator, the evaporator is provided with a heater, and the gas phase outlet of the evaporator is connected to the collection tank or the water absorption acid generator; or the liquid outlet of the water absorption acid generator is connected to the inlet of the evaporator, the evaporator is provided with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to the collection tank or the water absorption acid generator.

[0148] When a non-volatile acid is added to the evaporator, the evaporated hydrobromic acid vapor may still contain a small amount of non-volatile acid droplets (such as sulfuric acid) carried by the steam. After being reheated and evaporated in the evaporator and absorbed by the water absorption acid generator, the content of non-volatile acid droplets in the hydrobromic acid vapor is reduced, and there are fewer impurities in the hydrobromic acid.

[0149] When adding a non-volatile acid to the evaporator, the evaporated hydrobromic acid vapor may still contain a small amount of non-volatile acid droplets (e.g., sulfuric acid) carried by the steam. After adding chemicals (e.g., barium hydroxide) to the evaporator and reheating it for evaporation, the content of non-volatile acid droplets in the hydrobromic acid vapor is reduced, resulting in fewer impurities in the hydrobromic acid. Note: Sulfuric acid in the hydrobromic acid solution reacts with barium hydroxide to form barium sulfate, which has extremely low solubility. Reheating the evaporator to evaporate the hydrobromic acid vapor and then absorbing it through the water absorption acid generator helps to significantly reduce the sulfuric acid content in the hydrobromic acid.

[0150] Based on the above system, preferably, it also includes dryer I or dryer II.

[0151] The solid outlet of the solid-liquid separator II is connected to the inlet of the dryer I;

[0152] Alternatively, the solid outlet of the filter device I, the solid outlet of the integrated cooling and filtration machine I, the solid outlet of the filter device II, the solid outlet of the filter device III, or the solid outlet of the integrated washing and filtration machine I can be connected to the inlet of the dryer II.

[0153] Based on the above system, preferably, the solid outlet of the solid-liquid separator II or the solid outlet of the dryer I is collected as phthalic acid product or connected to the oxidation system of the PTA plant; or the solid outlet of the solid-liquid separator II or the solid outlet of the dryer I is connected to a pulping tank, the pulping tank also having a liquid inlet, and the outlet of the pulping tank being connected to the oxidation system of the PTA plant; or the solid outlet of the solid-liquid separator II or the solid outlet of the dryer I is mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA plant.

[0154] Alternatively, the solid outlet of the solid-liquid separator II or the solid outlet of the dryer I can be connected to the inlet of the washing tank IV, which also has a washing liquid inlet. The outlet of the washing tank IV is connected to the inlet of the solid-liquid separator IV, and the solid outlet of the solid-liquid separator IV is collected as phthalic acid product or connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator IV or the solid outlet of the dryer I can be connected to a pulping tank, which also has a liquid inlet. The outlet of the pulping tank is connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator IV can be mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA unit; the liquid outlet of the solid-liquid separator IV can be connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter removal device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device.

[0155] Alternatively, the solid outlet of the solid-liquid separator II or the solid outlet of the dryer I can be connected to the inlet of the washing and filtering integrated machine II, which also has a washing liquid inlet. The solid outlet of the washing and filtering integrated machine II can be collected as phthalic acid product or connected to the oxidation system of the PTA unit; or the solid outlet of the washing and filtering integrated machine II can be connected to a pulping tank, which also has a liquid inlet. The outlet of the pulping tank can be connected to the oxidation system of the PTA unit; or the solid outlet of the washing and filtering integrated machine II can be mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA unit; the liquid outlet of the washing and filtering integrated machine II can be connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter removal device, the inlet of the mixer I or the inlet of the cobalt-manganese adsorption device, connection point a, connection point b, connection point c or connection point d.

[0156] Alternatively, the solid outlet of the filtration device I, the solid outlet of the integrated cooling and filtration machine I, the solid outlet of the filtration device II, the solid outlet of the filtration device III, the solid outlet of the integrated washing and filtration machine I, or the solid outlet of the dryer II can be first connected to the inlet of the washing tank V. The washing tank V is also provided with a washing liquid inlet. The outlet of the washing tank V is connected to the inlet of the solid-liquid separator V. The solid outlet of the solid-liquid separator V collects benzoic acid product. The liquid outlet of the solid-liquid separator V is connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter elimination device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device, the connection point a, the connection point b, or the connection point e.

[0157] Based on the above system, preferably, the liquid outlet of the phthalic acid extraction device is connected to the benzoic acid extraction device, the liquid outlet of the benzoic acid extraction device is connected to the organic matter removal device, the liquid outlet of the benzoic acid extraction device is connected to the inlet of the mixer I, the liquid outlet of the benzoic acid extraction device is connected to the inlet of the cobalt-manganese adsorption device, the outlet of the organic matter removal device is connected to the inlet of the mixer I, the outlet of the organic matter removal device is connected to the inlet of the cobalt-manganese adsorption device, the outlet of the cobalt-manganese adsorption device is connected to the organic matter removal device, the liquid outlet of the solid-liquid separation device I is connected to the organic matter removal device, the outlet of the organic matter removal device is connected to the inlet of the nanofiltration system I, and the outlet of the cobalt-manganese adsorption device is connected to the nanofiltration system I. Oxidizing agents are installed between the liquid outlet of solid-liquid separation device I and the inlet of nanofiltration system I; between the outlet of organic matter removal device and the inlet of heating evaporation device I; between the outlet of cobalt-manganese adsorption device and the heating evaporation device I; between the liquid outlet of solid-liquid separation device I and the heating evaporation device I; between the outlet of cobalt-manganese adsorption device and the connection point a; between the liquid outlet of solid-liquid separation device I and the inlet of connection point a; between the outlet of organic matter removal device and the inlet of connection point a; between connection point a and the inlet of nanofiltration system I; between connection point e and the inlet of organic matter removal device; between connection point e and the inlet of decarbonization tower I; and between the outlet of decarbonization tower I and the inlet of organic matter removal device.

[0158] The oxidizing agent removal device removes oxidizing agents from the aqueous solution to prevent them from harming subsequent systems or causing impurities in sodium bromide (e.g., oxidizing agents exist in the form of bromine or sodium bromate).

[0159] Based on the above system, preferably, the oxidizing agent equipment adds reducing chemicals to reduce the oxidizing properties.

[0160] Based on the above system, preferably, the oxidizing agent removal device adds reducing chemical substances to reduce the oxidizing properties, including organic or inorganic reducing agents.

[0161] Based on the above system, preferably, the oxidizing agent removal device adds reducing chemical substances to reduce the oxidizing properties, including organic reducing agents, preferably formic acid, sodium formate, formaldehyde, acetaldehyde, etc.

[0162] Based on the above system, preferably, the oxidizing agent removal device adds reducing chemical substances to reduce the oxidizing properties, including inorganic reducing agents, preferably sodium sulfite, sodium bisulfite, sodium thiosulfate, etc.

[0163] Based on the above system, preferably, the oxidizing device is a solid bed that eliminates and / or adsorbs oxidants for removing oxidants from water.

[0164] Based on the above system, preferably, the heating crystallizer I is a thin-film evaporator;

[0165] Alternatively, the concentrate outlet of nanofiltration system I may be connected to the dosing port of mixer I;

[0166] Alternatively, the concentrate outlet of the nanofiltration system II may be connected to the dosing port of the mixer I, the connection point c, the inlet of the heating device I, or the inlet of the heating evaporation device I;

[0167] Alternatively, the solid outlet of the solid-liquid separator VI may be connected to the dosing port of the mixer I;

[0168] Alternatively, the bipolar membrane electrodialysis equipment may be equipped with an acid production tank, an alkali production tank, and / or a brine tank. The outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the mixer I, the inlet of the heating evaporation equipment I, the inlet of the organic matter removal equipment, connection point a, connection point b, connection point e, the inlet of nanofiltration system I, the inlet of concentration system II, or the inlet of concentration system III.

[0169] Based on the above system, preferably, if there are other bromine-containing aqueous solutions, they can also be incorporated into this system for processing, and the incorporation point can be any location in this system.

[0170] Beneficial effects

[0171] This invention provides a PTA oxidation residue treatment system that performs deep treatment on the oxidation residue. Specifically, it processes the solid output from the heated crystallizer (i.e., the heated crystallizer I described in this invention, commonly a thin-film evaporator) to recover the material value, mainly referring to the separation and recovery of phthalic acid, benzoic acid, and bromine. Simultaneously, due to the extraction of benzoic acid, phthalic acid, and bromine, the concentrations of these substances in the wastewater treatment system are reduced. This also avoids the difficulties in wastewater treatment caused by the existing PTA oxidation residue entering the wastewater system, thus promoting better operation of the wastewater treatment system and environmental protection. Attached Figure Description

[0172] Figure 1 This is a schematic diagram of Example 1.

[0173] Figure 2 This is a schematic diagram of Example 2.

[0174] Figure 3 This is a schematic diagram of Example 3.

[0175] Figure 4 This is a schematic diagram of Example 4.

[0176] Figure 5 This is a schematic diagram of Example 5.

[0177] Figure 6 This is a schematic diagram of Example 6.

[0178] Figure 7 This is a schematic diagram of Example 7.

[0179] Figure 8 This is a schematic diagram of Example 8.

[0180] legend:

[0181]

[0182] Detailed Implementation

[0183] The following non-limiting embodiments are intended to enable those skilled in the art to more fully understand the present invention, but do not limit the present invention in any way.

[0184] Example 1

[0185] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using concentration equipment 007 (using evaporation and concentration equipment as an example), cooling equipment 012, and filtration equipment I009 as examples), an organic matter removal device (benzene series adsorption equipment, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, an oxidizing agent removal device 057, a nanofiltration membrane 022 of nanofiltration system I, a concentration system III (using reverse osmosis membrane 027 as an example), a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporator 037, or a heated crystallizer II051.

[0186] The solid outlet of the heated crystallizer I001 is connected to the inlet of the mixer II002. The mixer II002 is also provided with a liquid inlet 003. The outlet of the mixer II002 is connected to the inlet of the solid-liquid separator II004. The liquid outlet 006 of the solid-liquid separator II004 is connected to the inlet of the concentration device 007 (using an evaporation and concentration device as an example). The concentration device 007 (using an evaporation and concentration device as an example) is also provided with a heater 008. The outlet of the concentration device 007 (using an evaporation and concentration device as an example) is connected to the inlet of the cooling device 012. The outlet of the cooling device 012 is connected to the inlet of the filter device I009. The liquid outlet 011 of the filter device I009 is connected to the inlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013. The outlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 is connected to the inlet of the mixer I014. The mixer I014 is also provided with a dosing port 015. The outlet of the mixer I014 is connected to the inlet of the solid-liquid separator I016. The liquid outlet 018 of the solid-liquid separator I016 is connected to the alkali addition stirring tank 019. The alkali addition stirring tank 019 is also provided with an alkali addition pipeline I020.

[0187] The solid outlet 005 of the solid-liquid separator II004 is connected to the inlet of the washing tank IV058. The washing tank IV058 is also provided with a washing liquid inlet 059. The outlet of the washing tank IV058 is connected to the inlet of the solid-liquid separator IV060. The liquid outlet 062 of the solid-liquid separator IV060 is connected to the liquid inlet 003 of the mixer II002. The solid outlet 061 of the solid-liquid separator IV060 collects the solids.

[0188] The solid outlet 010 of the filter device I009 is connected to the inlet of the washing tank V063. The washing tank V063 is also provided with a washing liquid inlet 064. The outlet of the washing tank V063 is connected to the inlet of the solid-liquid separator V065. The liquid outlet 067 of the solid-liquid separator V065 is connected to the liquid inlet 003 of the mixer II002. The solid outlet 066 of the solid-liquid separator V065 collects the solids.

[0189] Solids are collected at the solid outlet 017 of the solid-liquid separator I016;

[0190] The outlet of the alkali addition stirring tank 019 is connected to the inlet of the oxidizing agent 057. The outlet of the oxidizing agent 057 is connected to the inlet of the nanofiltration membrane 022 of the nanofiltration system I via the high-pressure pump 021 of the nanofiltration system I. The concentrate outlet 023 of the nanofiltration membrane 022 of the nanofiltration system I is connected to the dosing port 015 of the mixer I 014. The desalination outlet 024 of the nanofiltration membrane 022 of the nanofiltration system I is connected to the inlet of the buffer tank 025. The buffer tank 025 is connected to the reverse osmosis membrane 027 via the high-pressure pump 026 of the reverse osmosis membrane. The concentrate outlet 028 of the reverse osmosis membrane 027 is connected to the inlet of the acid addition stirring tank 029. The acid addition stirring tank 029 is also equipped with an acid addition pipeline I 056.

[0191] There are then four connection methods:

[0192] (1) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the collecting tank 030;

[0193] (2) The outlet of the acid mixing tank 029 is connected to the inlet of the bipolar membrane electrodialysis equipment 031. The bipolar membrane electrodialysis equipment 031 is also equipped with an alkali production tank 032, an acid production tank 034, and a brine tank 033. The outlet of the alkali production tank 032 is connected to the alkali addition pipeline I020 of the alkali mixing tank 019. The outlet of the brine tank 033 is connected to the inlet of the buffer tank 025. The outlet I035 of the acid production tank 034 is connected to the acid addition pipeline I056 of the acid mixing tank 029. The outlet II036 of the acid production tank 034 is connected to the oxidation system of the PTA unit.

[0194] (3) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the evaporator 037. The evaporator 037 is also equipped with a heater 038 and a dosing port 039. The gas phase outlet 040 of the evaporator 037 is connected to the inlet of the water absorption acid generator 041. The water absorption acid generator 041 is also equipped with a water dosing point 042. The liquid outlet of the water absorption acid generator 041 is connected to the inlet of the evaporator '043. The evaporator '043 is also equipped with a heater '044 and a dosing port '045. The gas phase outlet 046 of the evaporator '043 is connected to the inlet of the water absorption acid generator '047. The water absorption acid generator '047 is also equipped with a water dosing point '048. The outlet I 049 of the water absorption acid generator '047 is connected to the acid-adding pipeline I 056 of the acid-adding stirring tank 029. The outlet II 050 of the water absorption acid generator '047 is connected to the oxidation system of the PTA unit.

[0195] (4) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the heating crystallizer II 051. The heating crystallizer II 051 is also equipped with a heater 052. The outlet of the heating crystallizer II 051 is connected to the inlet of the centrifuge 053. The solid outlet of the centrifuge 053 is collected, and the liquid outlet of the centrifuge 053 is connected to the inlet of the heating crystallizer II 051.

[0196] The above system operates as follows:

[0197] The target material processed in this embodiment is the oxidation residue of PTA. In all embodiments of this utility model, the target material processed is the oxidation residue of PTA, and the source of the oxidation residue of PTA is the heated crystallizer I001 equipment.

[0198] The PTA oxidation residue originates from the heated crystallizer I001. The solid outlet of the heated crystallizer I001 contains the PTA oxidation residue, which enters the mixer II002 where 90°C hot water (approximately ten times the volume of the liquid inlet 003) is added and stirred. After solid-liquid separation in the solid-liquid separator II004, the liquid outlet 006 of the solid-liquid separator II004 mainly contains a solution of benzoic acid dissolved in hot water. This solution is then concentrated in the concentration unit 007 (using an evaporation and concentration unit as an example), cooled by the cooling unit 012, and then separated by the filtration unit I009. The liquid outlet 011 of the filtration unit I009 contains a solution that has reduced the benzene content. The formic acid solution is first processed by an organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 to adsorb benzene series compounds. Then it enters a mixer I 014, and sodium carbonate aqueous solution is added to the mixer I 014 (from the dosing port 015). Then it is separated into solid and liquid by a solid-liquid separator I 016. The filtrate from the solid-liquid separator I 016 is adjusted for pH by adding sodium hydroxide (sodium hydroxide aqueous solution is added through an alkali addition stirring tank 019 and an alkali addition pipeline I 020). Then it first passes through an oxidizing agent removal device 057 (filled with adsorption packing material: activated carbon) to remove oxidants, and then it is treated by the nanofiltration membrane 022 of the nanofiltration system I.

[0199] The solids from solid-liquid separator II004 are washed in washing tank IV058. Water (approximately ten times the volume) is added to the washing liquid inlet 059 of washing tank IV058 for washing. Afterwards, solids and liquids are separated in solid-liquid separator IV060. The resulting liquid is recycled back to mixer II002, and the resulting solids are collected.

[0200] The solids in the filter equipment I009 are washed in the washing tank V063. Water (about twenty times the volume) is added to the washing liquid inlet 064 of the washing tank V063 for washing. Then, solid-liquid separation is performed in the solid-liquid separator V065. The resulting liquid is recycled back to the mixer II002, and the resulting solids are collected.

[0201] Solid collection in solid-liquid separator I016;

[0202] The concentrate outlet 023 of nanofiltration membrane 022 in nanofiltration system I is returned to the dosing port 015 of mixer I 014 to provide sodium carbonate. The desalinated water outlet 024 of nanofiltration membrane 022 in nanofiltration system I (mainly sodium bromide) is concentrated by concentration system III (using reverse osmosis membrane 027 as an example), and then acid is added to neutralize sodium carbonate with hydrobromic acid (via acid addition stirring tank 029 and acid addition line I 056, which is used to provide hydrobromic acid). After that, there are four treatment methods:

[0203] (1) Collect using collection container 030;

[0204] (2) The alkali obtained by the bipolar membrane electrodialysis equipment 031 is recycled back to the alkali addition pipeline I020 of the alkali addition stirring tank 019 to provide sodium hydroxide; part of the hydrobromic acid obtained is recycled back to the acid addition pipeline I056 of the acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate therein, and the other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of the PTA unit; the sodium bromide liquid in the brine tank 033 is recycled back to the buffer tank 025, and after being concentrated again by the reverse osmosis membrane, it is recycled back to the bipolar membrane electrodialysis equipment 031 for further treatment;

[0205] (3) The process is carried out using evaporator 037. Sulfuric acid is added from the chemical inlet 039 of evaporator 037 and heated by heater 038 to generate hydrogen bromide gas. Water is added to the acid generator 041 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. The hydrobromic acid aqueous solution then enters evaporator 043. Barium hydroxide is added from the chemical inlet 045 of evaporator 043 and heated by heater 044 to generate hydrogen bromide gas. Water is added to the acid generator 047 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. Part of the hydrobromic acid aqueous solution is recycled back to the acid addition pipeline I056 of acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate in it. The other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of PTA unit.

[0206] (4) Evaporate and concentrate using heating crystallizer II051, and produce sodium bromide solid product using centrifuge 053. The filtrate from centrifuge 053 is then returned to heating crystallizer II051 for reheating. This continuous cycle produces sodium bromide solid product.

[0207] Note: All embodiments of this utility model use DuPont FilmTec nanofiltration membranes. TM The NF270-400 / 34i bipolar membrane electrodialysis unit uses the EX-4S provided by Hangzhou Lanran Technology Co., Ltd., while the reverse osmosis membrane uses DuPont's SW30HRLE-440i. The filter is a commercially available 5µm pore size PP cotton filter element, and all solid-liquid separators are centrifuges.

[0208] Run the experiment using the above system:

[0209] Hot water at 95°C was added to the inlet 003 of mixer II002 and stirred. A sample was taken from the solid outlet 005 of solid separator II004 for analysis: phthalic acid (TA) = 45.18%, benzoic acid (BA) = 0.25%, cobalt ions = 3206 ppm, manganese ions = 1881 ppm, bromide ions = 1991 ppm, and water content was approximately 50%.

[0210] Analysis of samples taken from the solid outlet 061 of the solid-liquid separator Ⅳ060: phthalic acid (TA) = 47.21%, benzoic acid (BA) = 0.13%, cobalt ions = 235 ppm, manganese ions = 199 ppm, bromide ions = 178 ppm, and water content is approximately 50%.

[0211] Analysis of samples taken from the solid outlet 010 of filter equipment I009 showed the following: benzoic acid (BA) = 27.73%, cobalt ions = 15531 ppm, manganese ions = 9891 ppm, bromide ions = 10919 ppm, and water content was approximately 72%.

[0212] Analysis of samples taken from the solid outlet 066 of solid separator V065 showed the following: benzoic acid (BA) = 31.12%, cobalt ions = 771 ppm, manganese ions = 561 ppm, bromide ions = 605 ppm, and water content was approximately 65%.

[0213] Analysis of samples taken from liquid outlet 011 of filter equipment I009: phthalic acid (TA) = 2451 ppm, benzoic acid (BA) = 6911 ppm; analysis of samples taken from outlet of organic matter removal equipment (benzene series adsorption equipment) 013: phthalic acid (TA) = 2 ppm, benzoic acid (BA) = 1 ppm.

[0214] A sample was taken from the solid outlet 017 of the solid-liquid separator I016: cobalt carbonate 31.1%, manganese carbonate 25.12%, and water content approximately 43%.

[0215] The pH of the effluent from the alkali addition mixing tank 019 was controlled at 11.5. The oxidizing power was tested at 18 ppm using the starch-potassium iodide method. The oxidizing power at the outlet of the oxidizing equipment was not detectable.

[0216] Analysis of the concentrate outlet 023 of nanofiltration membrane 022 of nanofiltration system I020: carbonate 48013 ppm, bromide 1038 ppm; analysis of the desalination outlet 024 of nanofiltration membrane 022 of nanofiltration system I020: carbonate 3210 ppm, bromide 9817 ppm.

[0217] The pH of the acid-adding stirring tank 029 was controlled at 3.5; sodium bromide was controlled at 111013 ppm.

[0218] There are four possible processing methods:

[0219] (1) Collected as sodium bromide aqueous solution product;

[0220] (2) The following is the analysis of the acid production tank 034 of the bipolar membrane electrodialysis equipment 031: hydrogen ions 1.26mol / L, bromide ions 9.91%, sodium ions 45ppm, proving that the product is hydrobromic acid;

[0221] (3) The liquid outlet sample analysis of water absorption acid generator 041 is as follows: hydrobromic acid content 31.1%, sulfate 215ppm; the liquid outlet sample analysis of water absorption acid generator '047 is as follows: hydrobromic acid content 38.7%, sulfate undetectable.

[0222] (4) The solid outlet 054 of the centrifuge 053 of the heated crystallizer II 051 was sampled and analyzed as follows: sodium bromide content 98.7%.

[0223] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate a product mainly containing phthalic acid (TA). Simultaneously, after washing, the cobalt, manganese, and bromide ion content in the phthalic acid (TA) product obtained from the solid outlet 061 of solid-liquid separator IV060 is reduced, meaning the overall system's loss of cobalt, manganese, and bromide ions from the phthalic acid (TA) product is reduced. Similarly, the solid outlet 010 of filter I009 can separate a product mainly containing benzoic acid (BA). Furthermore, after washing, the cobalt, manganese, and bromide ion content in the benzoic acid (BA) product obtained from the solid outlet 066 of solid-liquid separator V065 is reduced, meaning the overall system's loss of cobalt, manganese, and bromide ions from the benzoic acid (BA) product is reduced. The loss of cobalt, manganese, and bromide ions is reduced; phthalic acid (TA) and benzoic acid (BA) in the liquid outlet 011 of filter I009 can be removed by the organic matter removal device (benzene series adsorption device) 013; the solid in solid-liquid separator I016 is cobalt carbonate and manganese carbonate precipitated with sodium carbonate; the filtrate from solid-liquid separator I016 is separated by nanofiltration membrane 022 of nanofiltration system I into an aqueous solution mainly composed of sodium carbonate (concentrated water of nanofiltration membrane 022) and an aqueous solution mainly composed of sodium bromide (dehydrated water of nanofiltration membrane 022). The dehydrated water of nanofiltration membrane 022 (mainly composed of sodium bromide) is concentrated by reverse osmosis, and then treated by adding acid to remove residual sodium carbonate. It can be processed in four ways:

[0224] (1) A sodium bromide aqueous solution can be collected;

[0225] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0226] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0227] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0228] Example 2

[0229] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using concentration equipment 007 (using evaporation and concentration equipment as an example), cooling equipment 012, and filtration equipment I009 as examples), an organic matter removal device (benzene series adsorption equipment, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, a heated evaporation device I068, a solid-liquid separator VI070, a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporation tank 037, or a heated crystallizer II051.

[0230] The solid outlet of the heated crystallizer I001 is connected to the inlet of the mixer II002. The mixer II002 is also provided with a liquid inlet 003. The outlet of the mixer II002 is connected to the inlet of the solid-liquid separator II004. The liquid outlet 006 of the solid-liquid separator II004 is connected to the inlet of the concentration device 007 (using an evaporation and concentration device as an example). The concentration device 007 (using an evaporation and concentration device as an example) is also provided with a heater 008. The outlet of the concentration device 007 (using an evaporation and concentration device as an example) is connected to the inlet of the cooling device 012. The outlet of the cooling device 012 is connected to the inlet of the filter device I009. The liquid outlet 011 of the filter device I009 is connected to the inlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013. The outlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 is connected to the inlet of the mixer I014. The mixer I014 is also provided with a dosing port 015. The outlet of the mixer I014 is connected to the inlet of the solid-liquid separator I016. The liquid outlet 018 of the solid-liquid separator I016 is connected to the alkali addition stirring tank 019. The alkali addition stirring tank 019 is also provided with an alkali addition pipeline I020.

[0231] The solid outlet 005 of the solid-liquid separator II004 is connected to the inlet of the washing tank IV058. The washing tank IV058 is also provided with a washing liquid inlet 059. The outlet of the washing tank IV058 is connected to the inlet of the solid-liquid separator IV060. The liquid outlet 062 of the solid-liquid separator IV060 is connected to the liquid inlet 003 of the mixer II002. The solid outlet 061 of the solid-liquid separator IV060 collects the solids.

[0232] The solid outlet 010 of the filter device I009 is connected to the inlet of the washing tank V063. The washing tank V063 is also provided with a washing liquid inlet 064. The outlet of the washing tank V063 is connected to the inlet of the solid-liquid separator V065. The liquid outlet 067 of the solid-liquid separator V065 is connected to the liquid inlet 003 of the mixer II002. The solid outlet 066 of the solid-liquid separator V065 collects the solids.

[0233] Solids are collected at the solid outlet 017 of the solid-liquid separator I016;

[0234] The outlet of the alkali addition stirring tank 019 is connected to the inlet of the heating evaporation equipment I068. The heating evaporation equipment I068 is also equipped with a heater 069. The outlet of the heating evaporation equipment I068 is connected to the inlet of the solid-liquid separator VI070. The solid outlet 071 of the solid-liquid separator VI070 is connected to the dosing port 015 of the mixer I014. The liquid outlet 072 of the solid-liquid separator VI070 is connected to the inlet of the acid addition stirring tank 029. The acid addition stirring tank 029 is also equipped with an acid addition pipeline I056.

[0235] There are then four connection methods:

[0236] (1) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the collecting tank 030;

[0237] (2) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the bipolar membrane electrodialysis equipment 031. The bipolar membrane electrodialysis equipment 031 is also equipped with an alkali-producing tank 032, an acid-producing tank 034, and a brine tank 033. The outlet of the alkali-producing tank 032 is connected to the alkali-adding pipeline I020 of the alkali-adding stirring tank 019. The outlet of the brine tank 033 is connected to the inlet of the heating evaporation equipment I068. The outlet I035 of the acid-producing tank 034 is connected to the acid-adding pipeline I056 of the acid-adding stirring tank 029. The outlet II036 of the acid-producing tank 034 is connected to the oxidation system of the PTA unit.

[0238] (3) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the evaporator 037. The evaporator 037 is also equipped with a heater 038 and a dosing port 039. The gas phase outlet 040 of the evaporator 037 is connected to the inlet of the water absorption acid generator 041. The water absorption acid generator 041 is also equipped with a water dosing point 042. The liquid outlet of the water absorption acid generator 041 is connected to the inlet of the evaporator '043. The evaporator '043 is also equipped with a heater '044 and a dosing port '045. The gas phase outlet 046 of the evaporator '043 is connected to the inlet of the water absorption acid generator '047. The water absorption acid generator '047 is also equipped with a water dosing point '048. The outlet I 049 of the water absorption acid generator '047 is connected to the acid-adding pipeline I 056 of the acid-adding stirring tank 029. The outlet II 050 of the water absorption acid generator '047 is connected to the oxidation system of the PTA unit.

[0239] (4) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the heating crystallizer II 051. The heating crystallizer II 051 is also equipped with a heater 052. The outlet of the heating crystallizer II 051 is connected to the inlet of the centrifuge 053. The solid outlet of the centrifuge 053 is collected, and the liquid outlet of the centrifuge 053 is connected to the inlet of the heating crystallizer II 051.

[0240] The above system operates as follows:

[0241] The target material processed in this embodiment is the oxidation residue of PTA. In all embodiments of this utility model, the target material processed is the oxidation residue of PTA, and the source of the oxidation residue of PTA is the heated crystallizer I001 equipment.

[0242] The PTA oxidation residue originates from the heated crystallizer I001. The solid outlet of the heated crystallizer I001 contains the PTA oxidation residue, which enters the mixer II002 where 90°C hot water (from the inlet 003, approximately ten times the volume) is added and stirred. After solid-liquid separation in the solid-liquid separator II004, the liquid outlet 006 of the solid-liquid separator II004 mainly contains a solution of benzoic acid dissolved in hot water. This solution is then concentrated in the concentration unit 007 (using an evaporation and concentration unit as an example), cooled by the cooling unit 012, and then separated into solid and liquid components by the filtration unit I009. The filtration unit I009... The liquid outlet 011 is a solution with reduced benzoic acid content. After passing through the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 to adsorb benzene series compounds, it enters the mixer I014. Sodium carbonate aqueous solution is added to the mixer I014 (from the dosing port 015). Then, solid-liquid separation is performed by the solid-liquid separator I016. The filtrate of the solid-liquid separator I016 is adjusted for pH by adding sodium hydroxide (sodium hydroxide aqueous solution is added through the alkali addition stirring tank 019 and the alkali addition pipeline I020). Then, it is treated by the heating evaporation device I068 and the solid-liquid separator VI070.

[0243] The solids from solid-liquid separator II004 are washed in washing tank IV058. Water (approximately ten times the volume) is added to the washing liquid inlet 059 of washing tank IV058 for washing. Afterwards, solids and liquids are separated in solid-liquid separator IV060. The resulting liquid is recycled back to mixer II002, and the resulting solids are collected.

[0244] The solids in the filter equipment I009 are washed in the washing tank V063. Water (about twenty times the volume) is added to the washing liquid inlet 064 of the washing tank V063 for washing. Then, solid-liquid separation is performed in the solid-liquid separator V065. The resulting liquid is recycled back to the mixer II002, and the resulting solids are collected.

[0245] Solid collection in solid-liquid separator I016;

[0246] The solid outlet 071 of solid-liquid separator VI070 is connected to the dosing port 015 of mixer I014 to supply sodium carbonate. The liquid outlet 072 of solid-liquid separator VI070 (mainly sodium bromide) is neutralized with hydrobromic acid by adding acid (via acid addition stirring tank 029 and acid addition line I056, which is used to supply hydrobromic acid). After that, there are four processing methods:

[0247] (1) Collect using collection container 030;

[0248] (2) The alkali obtained by the bipolar membrane electrodialysis equipment 031 is recycled back to the alkali addition pipeline I020 of the alkali addition stirring tank 019 to provide sodium hydroxide; part of the hydrobromic acid obtained is recycled back to the acid addition pipeline I056 of the acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate therein, and the other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of the PTA unit; the sodium bromide liquid in the brine tank 033 is recycled back to the heating evaporation equipment I068 for further treatment;

[0249] (3) The process is carried out using evaporator 037. Sulfuric acid is added from the chemical inlet 039 of evaporator 037 and heated by heater 038 to generate hydrogen bromide gas. Water is added to the acid generator 041 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. The hydrobromic acid aqueous solution then enters evaporator 043. Barium hydroxide is added from the chemical inlet 045 of evaporator 043 and heated by heater 044 to generate hydrogen bromide gas. Water is added to the acid generator 047 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. Part of the hydrobromic acid aqueous solution is recycled back to the acid addition pipeline I056 of acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate in it. The other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of PTA unit.

[0250] (4) Evaporate and concentrate using heating crystallizer II051, and produce sodium bromide solid product using centrifuge 053. The filtrate from centrifuge 053 is then returned to heating crystallizer II051 for reheating. This continuous cycle produces sodium bromide solid product.

[0251] Run the experiment using the above system:

[0252] Hot water at 95°C was added to the inlet 003 of mixer II002 and stirred. A sample was taken from the solid outlet 005 of solid separator II004 for analysis: phthalic acid (TA) = 45.18%, benzoic acid (BA) = 0.25%, cobalt ions = 3206 ppm, manganese ions = 1881 ppm, bromide ions = 1991 ppm, and water content was approximately 50%.

[0253] Analysis of samples taken from the solid outlet 061 of the solid-liquid separator Ⅳ060: phthalic acid (TA) = 47.21%, benzoic acid (BA) = 0.13%, cobalt ions = 235 ppm, manganese ions = 199 ppm, bromide ions = 178 ppm, and water content is approximately 50%.

[0254] Analysis of samples taken from the solid outlet 010 of filter equipment I009 showed the following: benzoic acid (BA) = 27.73%, cobalt ions = 15531 ppm, manganese ions = 9891 ppm, bromide ions = 10919 ppm, and water content was approximately 72%.

[0255] Analysis of samples taken from the solid outlet 066 of solid separator V065 showed the following: benzoic acid (BA) = 31.12%, cobalt ions = 771 ppm, manganese ions = 561 ppm, bromide ions = 605 ppm, and water content was approximately 65%.

[0256] Analysis of samples taken from liquid outlet 011 of filter equipment I009: phthalic acid (TA) = 2451 ppm, benzoic acid (BA) = 6911 ppm; analysis of samples taken from outlet of organic matter removal equipment (benzene series adsorption equipment) 013: phthalic acid (TA) = 2 ppm, benzoic acid (BA) = 1 ppm.

[0257] A sample was taken from the solid outlet 017 of the solid-liquid separator I016: cobalt carbonate 31.1%, manganese carbonate 25.12%, and water content approximately 43%.

[0258] The pH of the effluent from the alkali addition stirring tank 019 was controlled at 11.5. Analysis of the solid outlet 071 of the solid separator VI070 showed 98.17% carbonate and 6015 ppm bromide. Analysis of the liquid outlet 072 of the solid separator VI070 showed 61717 ppm carbonate and 201918 ppm bromide.

[0259] The pH of the acid-adding stirring tank 029 was controlled at 3.5; sodium bromide concentration was 381317 ppm.

[0260] There are four possible processing methods:

[0261] (1) Collected as sodium bromide aqueous solution product;

[0262] (2) The following is the analysis of the acid production tank 034 of the bipolar membrane electrodialysis equipment 031: hydrogen ions 1.12 mol / L, bromide ions 9.02%, sodium ions 63 ppm, proving that the product is hydrobromic acid;

[0263] (3) The liquid outlet sample analysis of water absorption acid generator 041 is as follows: hydrobromic acid content 29.9%, sulfate 198ppm; the liquid outlet sample analysis of water absorption acid generator '047 is as follows: hydrobromic acid content 26.5%, sulfate undetectable.

[0264] (4) The solid outlet 054 of the centrifuge 053 of the heated crystallizer Ⅱ051 was sampled and analyzed as follows: sodium bromide content 97.3%.

[0265] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate a product mainly containing phthalic acid (TA). Simultaneously, after washing, the cobalt, manganese, and bromide ion content in the phthalic acid (TA) product obtained from the solid outlet 061 of solid-liquid separator IV060 is reduced, meaning the overall system's loss of cobalt, manganese, and bromide ions from the phthalic acid (TA) product is reduced. The solid outlet 010 of filter I009 can separate a product mainly containing benzoic acid (BA). Furthermore, after washing, the benzoic acid (BA) content in the solid outlet 066 of solid-liquid separator V065 is reduced. A) The content of cobalt, manganese, and bromide ions in the product is reduced, meaning the overall system loses less cobalt, manganese, and bromide ions from the benzoic acid (BA) product; phthalic acid (TA) and benzoic acid (BA) in the liquid outlet 011 of filter I009 can be removed by the organic matter removal device (benzene series adsorption device) 013; the solid outlet of solid-liquid separator I016 is cobalt carbonate and manganese carbonate precipitated with sodium carbonate; after the filtrate from solid-liquid separator I016 is treated by heating evaporation device I068 and solid-liquid separator VI070, and the filtrate is acidified to remove residual sodium carbonate, it can be treated in four ways:

[0266] (1) A sodium bromide aqueous solution can be collected;

[0267] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0268] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0269] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0270] Furthermore, it has been proven that the "nanofiltration system I" and the "heating evaporation equipment I068 and solid-liquid separator VI070" have the same effect, both of which can separate sodium bromide and sodium carbonate. The "nanofiltration system I" is functionally interchangeable with the "heating evaporation equipment I068 and solid-liquid separator VI070".

[0271] Example 3

[0272] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using concentration equipment 007 (using evaporation and concentration equipment as an example), cooling equipment 012, and filtration equipment I009 as examples), an organic matter removal device (benzene series adsorption equipment, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, an oxidizing agent removal device 057, a nanofiltration membrane 022 of nanofiltration system I, a concentration system III (using reverse osmosis membrane 027 as an example), a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporator 037, or a heated crystallizer II051.

[0273] The solid outlet of the heated crystallizer I001 is connected to the inlet of the mixer II002. The mixer II002 is also provided with a liquid inlet 003. The outlet of the mixer II002 is connected to the inlet of the solid-liquid separator II004. The liquid outlet 006 of the solid-liquid separator II004 is connected to the inlet of the concentration device 007 (using an evaporation and concentration device as an example). The concentration device 007 (using an evaporation and concentration device as an example) is also provided with a heater 008. The outlet of the concentration device 007 (using an evaporation and concentration device as an example) is connected to the inlet of the cooling device 012. The outlet of the cooling device 012 is connected to the inlet of the filter device I009. The liquid outlet 011 of the filter device I009 is connected to the inlet of the mixer I014. The mixer I014 is also provided with a chemical dosing port 015. The outlet of the mixer I014 is connected to the inlet of the solid-liquid separator I016. The liquid outlet 018 of the solid-liquid separator I016 is connected to the alkali addition stirring tank 019. The alkali addition stirring tank 019 is also provided with an alkali addition pipeline I020.

[0274] The solid outlet 005 of the solid-liquid separator II004 is connected to the inlet of the washing tank IV058. The washing tank IV058 is also provided with a washing liquid inlet 059. The outlet of the washing tank IV058 is connected to the inlet of the solid-liquid separator IV060. The liquid outlet 062 of the solid-liquid separator IV060 is connected to the liquid inlet 003 of the mixer II002. The solid outlet 061 of the solid-liquid separator IV060 collects the solids.

[0275] The solid outlet 010 of the filter device I009 is connected to the inlet of the washing tank V063. The washing tank V063 is also provided with a washing liquid inlet 064. The outlet of the washing tank V063 is connected to the inlet of the solid-liquid separator V065. The liquid outlet 067 of the solid-liquid separator V065 is connected to the liquid inlet 003 of the mixer II002. The solid outlet 066 of the solid-liquid separator V065 collects the solids.

[0276] Solids are collected at the solid outlet 017 of the solid-liquid separator I016;

[0277] The outlet of the alkali addition mixing tank 019 is connected to the inlet of the oxidizing agent 057. The outlet of the oxidizing agent 057 is connected to the inlet of the nanofiltration membrane 022 of nanofiltration system I via the high-pressure pump 021 of nanofiltration system I. The concentrate outlet 023 of the nanofiltration membrane 022 of nanofiltration system I is connected to the dosing port 015 of mixer I 014. The desalinated water outlet 024 of the nanofiltration membrane 022 of nanofiltration system I is connected to the inlet of buffer tank 025. The buffer tank 025 is connected to the inlet of the reverse osmosis membrane via the high-pressure pump 021 of reverse osmosis system I. Pump 026 is connected to reverse osmosis membrane 027. The concentrate outlet 028 of reverse osmosis membrane 027 is connected to the inlet of acid addition stirring tank 029. Acid addition stirring tank 029 is also equipped with acid addition pipeline I056. The outlet of acid addition stirring tank 029 is connected to the inlet of organic matter removal equipment (benzene series adsorption equipment, which is filled with benzene series adsorption resin). The outlet of organic matter removal equipment (benzene series adsorption equipment, which is filled with benzene series adsorption resin) 013 has the following four connection methods:

[0278] (1) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the collecting tank 030;

[0279] (2) The outlet of the acid mixing tank 029 is connected to the inlet of the bipolar membrane electrodialysis equipment 031. The bipolar membrane electrodialysis equipment 031 is also equipped with an alkali production tank 032, an acid production tank 034, and a brine tank 033. The outlet of the alkali production tank 032 is connected to the alkali addition pipeline I020 of the alkali mixing tank 019. The outlet of the brine tank 033 is connected to the inlet of the buffer tank 025. The outlet I035 of the acid production tank 034 is connected to the acid addition pipeline I056 of the acid mixing tank 029. The outlet II036 of the acid production tank 034 is connected to the oxidation system of the PTA unit.

[0280] (3) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the evaporator 037. The evaporator 037 is also equipped with a heater 038 and a dosing port 039. The gas phase outlet 040 of the evaporator 037 is connected to the inlet of the water absorption acid generator 041. The water absorption acid generator 041 is also equipped with a water dosing point 042. The liquid outlet of the water absorption acid generator 041 is connected to the inlet of the evaporator '043. The evaporator '043 is also equipped with a heater '044 and a dosing port '045. The gas phase outlet 046 of the evaporator '043 is connected to the inlet of the water absorption acid generator '047. The water absorption acid generator '047 is also equipped with a water dosing point '048. The outlet I 049 of the water absorption acid generator '047 is connected to the acid-adding pipeline I 056 of the acid-adding stirring tank 029. The outlet II 050 of the water absorption acid generator '047 is connected to the oxidation system of the PTA unit.

[0281] (4) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the heating crystallizer II 051. The heating crystallizer II 051 is also equipped with a heater 052. The outlet of the heating crystallizer II 051 is connected to the inlet of the centrifuge 053. The solid outlet of the centrifuge 053 is collected, and the liquid outlet of the centrifuge 053 is connected to the inlet of the heating crystallizer II 051.

[0282] The above system operates as follows:

[0283] The target material processed in this embodiment is the oxidation residue of PTA. In all embodiments of this utility model, the target material processed is the oxidation residue of PTA, and the source of the oxidation residue of PTA is the heated crystallizer I001 equipment.

[0284] The PTA oxidation residue originates from the heated crystallizer I001. The solid outlet of the heated crystallizer I001 contains the PTA oxidation residue, which enters the mixer II002 where 90°C hot water (from the inlet 003, approximately ten times the volume) is added and stirred. After solid-liquid separation in the solid-liquid separator II004, the liquid outlet 006 of the solid-liquid separator II004 mainly contains a solution of benzoic acid dissolved in hot water. This solution is then concentrated in the concentration device 007 (using an evaporation and concentration device as an example), cooled by the cooling device 012, and then separated into solid and liquid components by the filtration device I009. The liquid outlet 011 of the filtration device I009 is a solution with reduced benzoic acid content. It then enters the mixer I014, and sodium carbonate aqueous solution is added to the mixer I014 (from the dosing port 015). After solid-liquid separation by the solid-liquid separator I016, the filtrate from the solid-liquid separator I016 is adjusted for pH by adding sodium hydroxide (sodium hydroxide aqueous solution is added through the alkali addition stirring tank 019 and the alkali addition pipeline I020). It first passes through the oxidizing agent removal device 057 (filled with adsorption packing: activated carbon) to remove oxidizing agents, and then passes through the nanofiltration membrane 022 of the nanofiltration system I.

[0285] The concentrate outlet 023 of nanofiltration membrane 022 in nanofiltration system I is returned to the dosing port 015 of mixer I to provide sodium carbonate. The desalinated water outlet 024 of nanofiltration membrane 022 in nanofiltration system I (mainly sodium bromide) is concentrated by concentration system III (using reverse osmosis membrane 027 as an example). Then, acid is added to neutralize the sodium carbonate with hydrobromic acid (via acid addition stirring tank 029 and acid addition line I056, which provides hydrobromic acid). After passing through the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 to adsorb benzene series compounds, there are four treatment methods:

[0286] (1) Collect using collection container 030;

[0287] (2) The alkali obtained by the bipolar membrane electrodialysis equipment 031 is recycled back to the alkali addition pipeline I020 of the alkali addition stirring tank 019 to provide sodium hydroxide; part of the hydrobromic acid obtained is recycled back to the acid addition pipeline I056 of the acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate therein, and the other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of the PTA unit; the sodium bromide liquid in the brine tank 033 is recycled back to the buffer tank 025, and after being concentrated again by the reverse osmosis membrane, it is recycled back to the bipolar membrane electrodialysis equipment 031 for further treatment;

[0288] (3) The process is carried out using evaporator 037. Sulfuric acid is added from the chemical inlet 039 of evaporator 037 and heated by heater 038 to generate hydrogen bromide gas. Water is added to the acid generator 041 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. The hydrobromic acid aqueous solution then enters evaporator 043. Barium hydroxide is added from the chemical inlet 045 of evaporator 043 and heated by heater 044 to generate hydrogen bromide gas. Water is added to the acid generator 047 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. Part of the hydrobromic acid aqueous solution is recycled back to the acid addition pipeline I056 of acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate in it. The other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of PTA unit.

[0289] (4) Evaporate and concentrate using heating crystallizer II051, and produce sodium bromide solid product using centrifuge 053. The filtrate from centrifuge 053 is then returned to heating crystallizer II051 for reheating. This continuous cycle produces sodium bromide solid product.

[0290] The solids from solid-liquid separator II004 are washed in washing tank IV058. Water (approximately ten times the volume) is added to the washing liquid inlet 059 of washing tank IV058 for washing. Afterwards, solids and liquids are separated in solid-liquid separator IV060. The resulting liquid is recycled back to mixer II002, and the resulting solids are collected.

[0291] The solids in the filter equipment I009 are washed in the washing tank V063. Water (about twenty times the volume) is added to the washing liquid inlet 064 of the washing tank V063 for washing. Then, solid-liquid separation is performed in the solid-liquid separator V065. The resulting liquid is recycled back to the mixer II002, and the resulting solids are collected.

[0292] Solid collection in solid-liquid separator I016;

[0293] Run the experiment using the above system:

[0294] Hot water at 95°C was added to the inlet 003 of mixer II002 and stirred. A sample was taken from the solid outlet 005 of solid separator II004 for analysis: phthalic acid (TA) = 45.18%, benzoic acid (BA) = 0.25%, cobalt ions = 3206 ppm, manganese ions = 1881 ppm, bromide ions = 1991 ppm, and water content was approximately 50%.

[0295] Analysis of samples taken from the solid outlet 061 of the solid-liquid separator Ⅳ060: phthalic acid (TA) = 47.21%, benzoic acid (BA) = 0.13%, cobalt ions = 235 ppm, manganese ions = 199 ppm, bromide ions = 178 ppm, and water content is approximately 50%.

[0296] Analysis of samples taken from the solid outlet 010 of filter equipment I009 showed the following: benzoic acid (BA) = 27.73%, cobalt ions = 15531 ppm, manganese ions = 9891 ppm, bromide ions = 10919 ppm, and water content was approximately 72%.

[0297] Analysis of samples taken from the solid outlet 066 of solid separator V065 showed the following: benzoic acid (BA) = 31.12%, cobalt ions = 771 ppm, manganese ions = 561 ppm, bromide ions = 605 ppm, and water content was approximately 65%.

[0298] Analysis of liquid samples taken from outlet 011 of filter I009: phthalic acid (TA) = 2451 ppm, benzoic acid (BA) = 6911 ppm;

[0299] A sample was taken from the solid outlet 017 of the solid-liquid separator I016: cobalt carbonate 35.1%, manganese carbonate 26.2%, and water content approximately 38%.

[0300] The pH of the effluent from the alkali addition mixing tank 019 was controlled at 11.5. The oxidizing power was tested at 27 ppm using the starch-potassium iodide method. The oxidizing power at the outlet of the oxidizing equipment was not detectable.

[0301] Analysis of the concentrate outlet 023 of nanofiltration membrane 022 of nanofiltration system I020: carbonate 53542 ppm, bromide 1225 ppm; analysis of the desalination outlet 024 of nanofiltration membrane 022 of nanofiltration system I020: carbonate 4845 ppm, bromide 8719 ppm.

[0302] The pH of the acid addition stirring tank 029 was controlled at 3.5; sodium bromide was 61674 ppm, phthalic acid (TA) was 15311 ppm, and benzoic acid (BA) was 35313 ppm; samples were taken from the outlet of the organic matter removal device (benzene series adsorption device) 013: phthalic acid (TA) was 6 ppm, and benzoic acid (BA) was 2 ppm.

[0303] There are four possible processing methods:

[0304] (1) Collected as sodium bromide aqueous solution product;

[0305] (2) The following is the analysis of the acid production tank 034 of the bipolar membrane electrodialysis equipment 031: hydrogen ions 1.35mol / L, bromide ions 10.9%, sodium ions 89ppm, proving that the product is hydrobromic acid;

[0306] (3) The liquid outlet sample analysis of water absorption acid generator 041 is as follows: hydrobromic acid content 28.8%, sulfate 268ppm; the liquid outlet sample analysis of water absorption acid generator '047 is as follows: hydrobromic acid content 30.4%, sulfate undetectable.

[0307] (4) The solid outlet 054 of the centrifuge 053 of the heated crystallizer Ⅱ051 was sampled and analyzed as follows: sodium bromide content 96.2%.

[0308] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate a product mainly containing phthalic acid (TA). Simultaneously, after washing, the cobalt, manganese, and bromide ion content in the phthalic acid (TA) product obtained from the solid outlet 061 of solid-liquid separator IV060 is reduced, meaning the overall system's loss of cobalt, manganese, and bromide ions from the phthalic acid (TA) product is reduced. Similarly, the solid outlet 010 of filter I009 can separate a product mainly containing benzoic acid (BA). Furthermore, after washing, the cobalt, manganese, and bromide ion content in the benzoic acid (BA) product obtained from the solid outlet 066 of solid-liquid separator V065 is reduced, meaning the overall system's loss of cobalt, manganese, and bromide ions from the phthalic acid (TA) product is reduced. The loss of cobalt, manganese, and bromide ions from benzoic acid (BA) products is reduced; the solids in solid-liquid separator I 016 are cobalt carbonate and manganese carbonate products precipitated with sodium carbonate; the filtrate from solid-liquid separator I 016 is separated into an aqueous solution mainly composed of sodium carbonate (concentrated water from nanofiltration membrane 022) and an aqueous solution mainly composed of sodium bromide (dehydrated water from nanofiltration membrane 022) by nanofiltration membrane 022. After the dehydrated water (mainly composed of sodium bromide) from nanofiltration membrane 022 is concentrated by reverse osmosis, and then acid is added to remove residual sodium carbonate, phthalic acid (TA) and benzoic acid (BA) can be removed by organic matter removal equipment (benzene series adsorption equipment) 013, and then can be treated by four methods:

[0309] (1) A sodium bromide aqueous solution can be collected;

[0310] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0311] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0312] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0313] Meanwhile, Example 3 demonstrates that placing the organic matter removal device (benzene series adsorption device, internally filled with benzene series adsorption resin) 013 between the liquid outlet 011 of the filter device I009 and the inlet of the mixer I014 achieves the same effect whether it is placed between the inlet of the acid mixing tank and the collection tank, the inlet of the evaporator, the inlet of the bipolar membrane electrodialysis device, or the inlet of the heated crystallizer II. That is, the purpose of the organic matter removal device (benzene series adsorption device, internally filled with benzene series adsorption resin) 013 is to remove organic matter (benzene series). Its position in the above two locations has the same functional effect, and its position in the above two locations can be interchanged.

[0314] Example 4

[0315] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using concentration equipment 007 (using evaporation and concentration equipment as an example), cooling equipment 012, and filtration equipment I009 as examples), an organic matter removal device (benzene series adsorption equipment, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, a heated evaporation device I068, a solid-liquid separator VI070, a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporation tank 037, or a heated crystallizer II051.

[0316] Based on Example 3, the "nanofiltration system I" in Example 3 is replaced with "heating evaporation equipment I068 and solid-liquid separator VI070".

[0317] Specific connection method:

[0318] Based on Example 3, the outlet of the alkali addition stirring tank 019 in Example 3 is connected to the inlet of the oxidizing agent 057; the outlet of the oxidizing agent 057 is connected to the inlet of the nanofiltration membrane 022 of nanofiltration system I via the high-pressure pump 021 of nanofiltration system I; the concentrate outlet 023 of the nanofiltration membrane 022 of nanofiltration system I is connected to the dosing port 015 of mixer I 014; the desalination outlet 024 of the nanofiltration membrane 022 of nanofiltration system I is connected to the inlet of buffer tank 025; and the buffer tank 025 is connected to the reverse osmosis membrane via the high-pressure pump 026 of reverse osmosis membrane. The phrase “the concentrated water outlet 028 of the reverse osmosis membrane 027 is connected to the inlet of the acid mixing tank 029” is replaced with “the outlet of the alkali mixing tank 019 is connected to the inlet of the heating evaporation equipment I 068, the heating evaporation equipment I 068 is also equipped with a heater 069, the outlet of the heating evaporation equipment I 068 is connected to the inlet of the solid-liquid separator VI 070, the solid outlet 071 of the solid-liquid separator VI 070 is connected to the dosing port 015 of the mixer I 014, and the liquid outlet 072 of the solid-liquid separator VI 070 is connected to the inlet of the acid mixing tank 029”.

[0319] The above system operates as follows:

[0320] Based on Example 3, the process of first removing oxidizing agents using an oxidizing agent removal device 057 (filled with adsorption packing material: activated carbon), then treating the solution through nanofiltration membrane 022 of nanofiltration system I, with the concentrate outlet 023 of nanofiltration membrane 022 of nanofiltration system I returning to the dosing port 015 of mixer I to provide sodium carbonate, and the desalinated water outlet 024 of nanofiltration membrane 022 of nanofiltration system I (mainly sodium bromide) being concentrated by concentration system III (using reverse osmosis membrane 027 as an example), and then neutralizing the sodium carbonate with hydrobromic acid by adding acid (after adding... The phrase “acid stirring tank 029 and acid adding line I056, acid adding line I056 is used to provide hydrobromic acid” is replaced with “processed by heating evaporation equipment I068 and solid-liquid separator VI070; the solid outlet 071 of solid-liquid separator VI070 is connected to the dosing port 015 of mixer I014 to provide sodium carbonate; the liquid outlet 072 of solid-liquid separator VI070 (mainly sodium bromide) is acidified to neutralize sodium carbonate with hydrobromic acid (passing through acid stirring tank 029 and acid adding line I056, acid adding line I056 is used to provide hydrobromic acid)”.

[0321] Run the experiment using the above system:

[0322] Example 2 demonstrates that the "nanofiltration system I" and the "heating evaporation device I068 and solid-liquid separator VI070" have the same effect, both being able to separate sodium bromide and sodium carbonate. The "nanofiltration system I" is functionally interchangeable with the "heating evaporation device I068 and solid-liquid separator VI070". It can be inferred that, based on Example 3, replacing the "nanofiltration system I" with the "heating evaporation device I068 and solid-liquid separator VI070" can also achieve the same effect.

[0323] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate products mainly containing phthalic acid (TA). Simultaneously, after washing, the cobalt, manganese, and bromide ion content in the phthalic acid (TA) product obtained from the solid outlet 061 of solid-liquid separator IV060 is reduced, meaning the overall system's loss of cobalt, manganese, and bromide ions from the phthalic acid (TA) product is reduced. The solid outlet 010 of filter I009 can separate products mainly containing benzoic acid (BA). Furthermore, after washing, the solid outlet 061 of solid-liquid separator V065... The content of cobalt, manganese, and bromide ions in the obtained benzoic acid (BA) product is reduced, meaning the overall system loses less cobalt, manganese, and bromide ions from the benzoic acid (BA) product. The solid in solid-liquid separator I016 is cobalt carbonate and manganese carbonate precipitated with sodium carbonate. After the filtrate from solid-liquid separator I016 is treated by heating evaporation equipment I068 and solid-liquid separator VI070, the filtrate is acidified to remove residual sodium carbonate. The phthalic acid (TA) and benzoic acid (BA) can then be removed by organic matter removal equipment (benzene series adsorption equipment) 013, and subsequently processed using four methods:

[0324] (1) A sodium bromide aqueous solution can be collected;

[0325] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0326] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0327] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0328] Example 5

[0329] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using washing tank II073 and heated crystallizer III077 as examples), an organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, an oxidizing agent removal device 057, a nanofiltration membrane 022 of nanofiltration system I, a concentration system III (using reverse osmosis membrane 027 as an example), a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporator 037, or a heated crystallizer II051.

[0330] The solid outlet of the heated crystallizer Ⅰ001 is connected to the inlet of the mixer Ⅱ002. The mixer Ⅱ002 is also provided with a liquid inlet 003. The outlet of the mixer Ⅱ002 is connected to the inlet of the solid-liquid separator Ⅱ004. The liquid outlet 006 of the solid-liquid separator Ⅱ004 is connected to the inlet of the washing tank Ⅱ073. The washing tank Ⅱ073 is also provided with a washing liquid inlet 074. The aqueous phase outlet 075 of the washing tank Ⅱ073 is connected to the inlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013. The outlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 is connected to the inlet of the mixer Ⅰ014. The mixer Ⅰ014 is also provided with a chemical dosing port 015. The outlet of the mixer Ⅰ014 is connected to the inlet of the solid-liquid separator Ⅰ016. The liquid outlet 018 of the solid-liquid separator Ⅰ016 is connected to the alkali addition stirring tank 019. The alkali addition stirring tank 019 is also provided with an alkali addition pipeline Ⅰ020.

[0331] Solids are collected at the solid outlet 005 of the solid-liquid separator II004;

[0332] The oil phase outlet 076 of the washing tank II 073 is connected to the inlet of the heating crystallizer III 077. The heating crystallizer III 077 is also equipped with a heater 078. The outlet of the heating crystallizer III 077 is connected to the inlet of the centrifuge 079 of the heating crystallizer III 077. The solid outlet 080 of the centrifuge 079 of the heating crystallizer III 077 collects the solids, and the liquid outlet 081 of the centrifuge 079 of the heating crystallizer III 077 is connected to the inlet of the heating crystallizer III 077.

[0333] Solids are collected at the solid outlet 017 of the solid-liquid separator I016;

[0334] The outlet of the alkali addition stirring tank 019 is connected to the inlet of the oxidizing agent 057. The outlet of the oxidizing agent 057 is connected to the inlet of the nanofiltration membrane 022 of the nanofiltration system I via the high-pressure pump 021 of the nanofiltration system I. The concentrate outlet 023 of the nanofiltration membrane 022 of the nanofiltration system I is connected to the dosing port 015 of the mixer I 014. The desalination outlet 024 of the nanofiltration membrane 022 of the nanofiltration system I is connected to the inlet of the buffer tank 025. The buffer tank 025 is connected to the reverse osmosis membrane 027 via the high-pressure pump 026 of the reverse osmosis membrane. The concentrate outlet 028 of the reverse osmosis membrane 027 is connected to the inlet of the acid addition stirring tank 029. The acid addition stirring tank 029 is also equipped with an acid addition pipeline I 056.

[0335] There are then four connection methods:

[0336] (1) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the collecting tank 030;

[0337] (2) The outlet of the acid mixing tank 029 is connected to the inlet of the bipolar membrane electrodialysis equipment 031. The bipolar membrane electrodialysis equipment 031 is also equipped with an alkali production tank 032, an acid production tank 034, and a brine tank 033. The outlet of the alkali production tank 032 is connected to the alkali addition pipeline I020 of the alkali mixing tank 019. The outlet of the brine tank 033 is connected to the inlet of the buffer tank 025. The outlet I035 of the acid production tank 034 is connected to the acid addition pipeline I056 of the acid mixing tank 029. The outlet II036 of the acid production tank 034 is connected to the oxidation system of the PTA unit.

[0338] (3) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the evaporator 037. The evaporator 037 is also equipped with a heater 038 and a dosing port 039. The gas phase outlet 040 of the evaporator 037 is connected to the inlet of the water absorption acid generator 041. The water absorption acid generator 041 is also equipped with a water dosing point 042. The liquid outlet of the water absorption acid generator 041 is connected to the inlet of the evaporator '043. The evaporator '043 is also equipped with a heater '044 and a dosing port '045. The gas phase outlet 046 of the evaporator '043 is connected to the inlet of the water absorption acid generator '047. The water absorption acid generator '047 is also equipped with a water dosing point '048. The outlet I 049 of the water absorption acid generator '047 is connected to the acid-adding pipeline I 056 of the acid-adding stirring tank 029. The outlet II 050 of the water absorption acid generator '047 is connected to the oxidation system of the PTA unit.

[0339] (4) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the heating crystallizer II 051. The heating crystallizer II 051 is also equipped with a heater 052. The outlet of the heating crystallizer II 051 is connected to the inlet of the centrifuge 053. The solid outlet of the centrifuge 053 is collected, and the liquid outlet of the centrifuge 053 is connected to the inlet of the heating crystallizer II 051.

[0340] The above system operates as follows:

[0341] The target material processed in this embodiment is the oxidation residue of PTA. In all embodiments of this utility model, the target material processed is the oxidation residue of PTA, and the source of the oxidation residue of PTA is the heated crystallizer I001 equipment.

[0342] The PTA oxidation residue originates from the heated crystallizer I001. The solid outlet of the heated crystallizer I001 contains the PTA oxidation residue, which enters the mixer II002 and is mixed with solvent benzene (from inlet 003, approximately ten times its volume). The mixture is stirred and then undergoes solid-liquid separation in the solid-liquid separator II004. The liquid outlet 006 of the solid-liquid separator II004 mainly contains a solution of benzoic acid dissolved in solvent benzene. This solution is then washed with water in the washing tank II073. The aqueous phase in the washing tank II073 (containing dissolved ions) passes through an organic matter removal device (benzene series adsorption device). The resin (013) is filled with benzene series adsorption resin to adsorb benzene series compounds. Then it enters the mixer I 014 and sodium carbonate aqueous solution is added to the mixer I 014 (from the dosing port 015). Then it is separated into solid and liquid by the solid-liquid separator I 016. The filtrate of the solid-liquid separator I 016 is adjusted for pH by adding sodium hydroxide (sodium hydroxide aqueous solution is added through the alkali addition stirring tank 019 and the alkali addition pipeline I 020). Then it first passes through the oxidizing agent removal device 057 (filled with adsorption packing: activated carbon) to remove oxidizing agents. Then it is treated by the nanofiltration membrane 022 of the nanofiltration system I.

[0343] Solid collection in solid-liquid separator II004;

[0344] After the oil phase from washing tank II073 is heated to remove solvent benzene in heating crystallizer III077, it is filtered through centrifuge 079 in heating crystallizer III077. The resulting solid BA is collected, and the liquid is recycled back to heating crystallizer III077 for reheating.

[0345] Solid collection in solid-liquid separator I016;

[0346] The concentrate outlet 023 of nanofiltration membrane 022 in nanofiltration system I is returned to the dosing port 015 of mixer I 014 to provide sodium carbonate. The desalinated water outlet 024 of nanofiltration membrane 022 in nanofiltration system I (mainly sodium bromide) is concentrated by concentration system III (using reverse osmosis membrane 027 as an example), and then acid is added to neutralize sodium carbonate with hydrobromic acid (via acid addition stirring tank 029 and acid addition line I 056, which is used to provide hydrobromic acid). After that, there are four treatment methods:

[0347] (1) Collect using collection container 030;

[0348] (2) The alkali obtained by the bipolar membrane electrodialysis equipment 031 is recycled back to the alkali addition pipeline I020 of the alkali addition stirring tank 019 to provide sodium hydroxide; part of the hydrobromic acid obtained is recycled back to the acid addition pipeline I056 of the acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate therein, and the other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of the PTA unit; the sodium bromide liquid in the brine tank 033 is recycled back to the buffer tank 025, and after being concentrated again by the reverse osmosis membrane, it is recycled back to the bipolar membrane electrodialysis equipment 031 for further treatment;

[0349] (3) The process is carried out using evaporator 037. Sulfuric acid is added from the chemical inlet 039 of evaporator 037 and heated by heater 038 to generate hydrogen bromide gas. Water is added to the acid generator 041 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. The hydrobromic acid aqueous solution then enters evaporator 043. Barium hydroxide is added from the chemical inlet 045 of evaporator 043 and heated by heater 044 to generate hydrogen bromide gas. Water is added to the acid generator 047 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. Part of the hydrobromic acid aqueous solution is recycled back to the acid addition pipeline I056 of acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate in it. The other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of PTA unit.

[0350] (4) Evaporate and concentrate using heating crystallizer II051, and produce sodium bromide solid product using centrifuge 053. The filtrate from centrifuge 053 is then returned to heating crystallizer II051 for reheating. This continuous cycle produces sodium bromide solid product.

[0351] Run the experiment using the above system:

[0352] Add solvent benzene to the inlet 003 of mixer Ⅱ002 and stir. Take a sample from the solid outlet 005 of solid separator Ⅱ004 for analysis: phthalic acid (TA) = 62.14%, benzoic acid (BA) = 0.78%, benzene content 36%;

[0353] Analysis of a sample taken from the solid outlet 080 of the centrifuge 079 of the heated crystallizer Ⅲ077 showed: benzoic acid (BA) = 83.15%, benzene content 15%;

[0354] The outlet sampling of the organic matter removal equipment (benzene series adsorption equipment) 013 is as follows: phthalic acid (TA) = 3 ppm, benzoic acid (BA) = 5 ppm;

[0355] A sample was taken from the solid outlet 017 of the solid-liquid separator I016: cobalt carbonate 41.1%, manganese carbonate 31.8%, and water content approximately 26%.

[0356] The pH of the effluent from the alkali addition mixing tank 019 was controlled at 11.5. The oxidizing power was tested at 15 ppm using the starch-potassium iodide method. The oxidizing power at the outlet of the oxidizing equipment was not detectable.

[0357] Analysis of the concentrate outlet 023 of nanofiltration membrane 022 of nanofiltration system I020: carbonate 46137ppm, bromide 1358ppm; analysis of the desalination outlet 024 of nanofiltration membrane 022 of nanofiltration system I020: carbonate 2991ppm, bromide 10008ppm.

[0358] The pH of the acid-adding stirring tank 029 was controlled at 3.5; sodium bromide was controlled at 109112 ppm.

[0359] There are four possible processing methods:

[0360] (1) Collected as sodium bromide aqueous solution product;

[0361] (2) The following is the analysis of the acid production tank 034 of the bipolar membrane electrodialysis equipment 031: hydrogen ions 1.63mol / L, bromide ions 13.3%, sodium ions 25ppm, proving that the product is hydrobromic acid;

[0362] (3) The liquid outlet sample analysis of water absorption acid generator 041 is as follows: hydrobromic acid content 41.3%, sulfate 329ppm; the liquid outlet sample analysis of water absorption acid generator '047 is as follows: hydrobromic acid content 44.5%, sulfate undetectable.

[0363] (4) The solid outlet 054 of the centrifuge 053 of the heated crystallizer Ⅱ051 was sampled and analyzed as follows: sodium bromide content 99.1%.

[0364] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate products mainly containing phthalic acid (TA); the solid outlet 080 of centrifuge 079 of heated crystallizer III077 can separate products mainly containing benzoic acid (BA); the phthalic acid (TA) and benzoic acid (BA) in the liquid outlet 081 of centrifuge 079 of heated crystallizer III077 can be removed by the organic matter removal device (benzene series adsorption device) 013; the solids in solid-liquid separator I016 are cobalt carbonate and manganese carbonate products precipitated with sodium carbonate; the filtrate from solid-liquid separator I016 is separated by nanofiltration membrane 022 of nanofiltration system I into an aqueous solution mainly containing sodium carbonate (concentrated water of nanofiltration membrane 022) and an aqueous solution mainly containing sodium bromide (dehydrated water of nanofiltration membrane 022). The dehydrated water of nanofiltration membrane 022 (mainly sodium bromide) is concentrated by reverse osmosis, and then treated by adding acid to remove residual sodium carbonate. It can be processed by four methods:

[0365] (1) A sodium bromide aqueous solution can be collected;

[0366] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0367] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0368] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0369] Example 6

[0370] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using washing tank II073 and heated crystallizer III077 as examples), a cooling device 012, a filtration device I009 as examples, an organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, a heated evaporation device I068, a solid-liquid separator VI070, a collection tank 030 or a bipolar membrane electrodialysis device 031 or an evaporation tank 037 or a heated crystallizer II051.

[0371] The solid outlet of the heated crystallizer Ⅰ001 is connected to the inlet of the mixer Ⅱ002. The mixer Ⅱ002 is also provided with a liquid inlet 003. The outlet of the mixer Ⅱ002 is connected to the inlet of the solid-liquid separator Ⅱ004. The liquid outlet 006 of the solid-liquid separator Ⅱ004 is connected to the inlet of the washing tank Ⅱ073. The washing tank Ⅱ073 is also provided with a washing liquid inlet 074. The aqueous phase outlet 075 of the washing tank Ⅱ073 is connected to the inlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013. The outlet of the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 is connected to the inlet of the mixer Ⅰ014. The mixer Ⅰ014 is also provided with a chemical dosing port 015. The outlet of the mixer Ⅰ014 is connected to the inlet of the solid-liquid separator Ⅰ016. The liquid outlet 018 of the solid-liquid separator Ⅰ016 is connected to the alkali addition stirring tank 019. The alkali addition stirring tank 019 is also provided with an alkali addition pipeline Ⅰ020.

[0372] Solids are collected at the solid outlet 005 of the solid-liquid separator II004;

[0373] The oil phase outlet 076 of the washing tank II 073 is connected to the inlet of the heating crystallizer III 077. The heating crystallizer III 077 is also equipped with a heater 078. The outlet of the heating crystallizer III 077 is connected to the inlet of the centrifuge 079 of the heating crystallizer III 077. The solid outlet 080 of the centrifuge 079 of the heating crystallizer III 077 collects the solids, and the liquid outlet 081 of the centrifuge 079 of the heating crystallizer III 077 is connected to the inlet of the heating crystallizer III 077.

[0374] Solids are collected at the solid outlet 017 of the solid-liquid separator I016;

[0375] The outlet of the alkali addition stirring tank 019 is connected to the inlet of the heating evaporation equipment I068. The heating evaporation equipment I068 is also equipped with a heater 069. The outlet of the heating evaporation equipment I068 is connected to the inlet of the solid-liquid separator VI070. The solid outlet 071 of the solid-liquid separator VI070 is connected to the dosing port 015 of the mixer I014. The liquid outlet 072 of the solid-liquid separator VI070 is connected to the inlet of the acid addition stirring tank 029. The acid addition stirring tank 029 is also equipped with an acid addition pipeline I056.

[0376] There are then four connection methods:

[0377] (1) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the collecting tank 030;

[0378] (2) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the bipolar membrane electrodialysis equipment 031. The bipolar membrane electrodialysis equipment 031 is also equipped with an alkali-producing tank 032, an acid-producing tank 034, and a brine tank 033. The outlet of the alkali-producing tank 032 is connected to the alkali-adding pipeline I020 of the alkali-adding stirring tank 019. The outlet of the brine tank 033 is connected to the inlet of the heating evaporation equipment I068. The outlet I035 of the acid-producing tank 034 is connected to the acid-adding pipeline I056 of the acid-adding stirring tank 029. The outlet II036 of the acid-producing tank 034 is connected to the oxidation system of the PTA unit.

[0379] (3) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the evaporator 037. The evaporator 037 is also equipped with a heater 038 and a dosing port 039. The gas phase outlet 040 of the evaporator 037 is connected to the inlet of the water absorption acid generator 041. The water absorption acid generator 041 is also equipped with a water dosing point 042. The liquid outlet of the water absorption acid generator 041 is connected to the inlet of the evaporator '043. The evaporator '043 is also equipped with a heater '044 and a dosing port '045. The gas phase outlet 046 of the evaporator '043 is connected to the inlet of the water absorption acid generator '047. The water absorption acid generator '047 is also equipped with a water dosing point '048. The outlet I 049 of the water absorption acid generator '047 is connected to the acid-adding pipeline I 056 of the acid-adding stirring tank 029. The outlet II 050 of the water absorption acid generator '047 is connected to the oxidation system of the PTA unit.

[0380] (4) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the heating crystallizer II 051. The heating crystallizer II 051 is also equipped with a heater 052. The outlet of the heating crystallizer II 051 is connected to the inlet of the centrifuge 053. The solid outlet of the centrifuge 053 is collected, and the liquid outlet of the centrifuge 053 is connected to the inlet of the heating crystallizer II 051.

[0381] The above system operates as follows:

[0382] The target material processed in this embodiment is the oxidation residue of PTA. In all embodiments of this utility model, the target material processed is the oxidation residue of PTA, and the source of the oxidation residue of PTA is the heated crystallizer I001 equipment.

[0383] The PTA oxidation residue originates from the heated crystallizer I001. The solid outlet of the heated crystallizer I001 contains the PTA oxidation residue, which enters the mixer II002 and is mixed with solvent benzene (from inlet 003, approximately ten times its volume). The mixture is stirred and then undergoes solid-liquid separation in the solid-liquid separator II004. The resulting liquid outlet 006 of the solid-liquid separator II004 is primarily a solution of benzoic acid dissolved in solvent benzene. This solution is then washed with water in the washing tank II073. The aqueous phase in the washing tank II073 (containing dissolved ions) undergoes organic... The benzene series adsorption device (which is filled with benzene series adsorption resin) 013 adsorbs benzene series compounds, and then enters the mixer I014. Sodium carbonate aqueous solution is added to the mixer I014 (from the dosing port 015). Then, solid-liquid separation is performed by the solid-liquid separator I016. The filtrate of the solid-liquid separator I016 is adjusted for pH by adding sodium hydroxide (sodium hydroxide aqueous solution is added through the alkali addition stirring tank 019 and the alkali addition pipeline I020), and then treated by the heating evaporation device I068 and the solid-liquid separator VI070.

[0384] Solid collection in solid-liquid separator II004;

[0385] After the oil phase from washing tank II073 is heated to remove solvent benzene in heating crystallizer III077, it is filtered through centrifuge 079 in heating crystallizer III077. The resulting solid BA is collected, and the liquid is recycled back to heating crystallizer III077 for reheating.

[0386] Solid collection in solid-liquid separator I016;

[0387] The solid outlet 071 of solid-liquid separator VI070 is connected to the dosing port 015 of mixer I014 to supply sodium carbonate. The liquid outlet 072 of solid-liquid separator VI070 (mainly sodium bromide) is neutralized with hydrobromic acid by adding acid (via acid addition stirring tank 029 and acid addition line I056, which is used to supply hydrobromic acid). After that, there are four processing methods:

[0388] (1) Collect using collection container 030;

[0389] (2) The alkali obtained by the bipolar membrane electrodialysis equipment 031 is recycled back to the alkali addition pipeline I020 of the alkali addition stirring tank 019 to provide sodium hydroxide; part of the hydrobromic acid obtained is recycled back to the acid addition pipeline I056 of the acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate therein, and the other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of the PTA unit; the sodium bromide liquid in the brine tank 033 is recycled back to the heating evaporation equipment I068 for further treatment;

[0390] (3) The process is carried out using evaporator 037. Sulfuric acid is added from the chemical inlet 039 of evaporator 037 and heated by heater 038 to generate hydrogen bromide gas. Water is added to the acid generator 041 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. The hydrobromic acid aqueous solution then enters evaporator 043. Barium hydroxide is added from the chemical inlet 045 of evaporator 043 and heated by heater 044 to generate hydrogen bromide gas. Water is added to the acid generator 047 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. Part of the hydrobromic acid aqueous solution is recycled back to the acid addition pipeline I056 of acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate in it. The other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of PTA unit.

[0391] (4) Evaporate and concentrate using heating crystallizer II051, and produce sodium bromide solid product using centrifuge 053. The filtrate from centrifuge 053 is then returned to heating crystallizer II051 for reheating. This continuous cycle produces sodium bromide solid product.

[0392] Run the experiment using the above system:

[0393] Add solvent benzene to the inlet 003 of mixer Ⅱ002 and stir. Take a sample from the solid outlet 005 of solid separator Ⅱ004 for analysis: phthalic acid (TA) = 62.14%, benzoic acid (BA) = 0.78%, benzene content 36%;

[0394] Analysis of a sample taken from the solid outlet 080 of the centrifuge 079 of the heated crystallizer Ⅲ077 showed: benzoic acid (BA) = 83.15%, benzene content 15%;

[0395] The outlet sampling of the organic matter removal equipment (benzene series adsorption equipment) 013 is as follows: phthalic acid (TA) = 3 ppm, benzoic acid (BA) = 5 ppm;

[0396] A sample was taken from the solid outlet 017 of the solid-liquid separator I016: cobalt carbonate 41.1%, manganese carbonate 31.8%, and water content approximately 26%.

[0397] The pH of the effluent from the alkali addition stirring tank 019 was controlled at 11.5. Analysis of the solid outlet 071 of the solid separator VI070 showed: carbonate 96.66% and bromide 5447ppm. Analysis of the liquid outlet 072 of the solid separator VI070 showed: carbonate 52527ppm and bromide 233121ppm.

[0398] The pH of the acid-adding stirring tank 029 was controlled at 3.5; sodium bromide at 376737 ppm.

[0399] There are four possible processing methods:

[0400] (1) Collected as sodium bromide aqueous solution product;

[0401] (2) The following is the analysis of the acid production tank 034 of the bipolar membrane electrodialysis equipment 031: hydrogen ions 0.93mol / L, bromide ions 7.4%, sodium ions 32ppm, proving that the product is hydrobromic acid;

[0402] (3) The liquid outlet sample analysis of water absorption acid generator 041 is as follows: hydrobromic acid content 36.5%, sulfate 277ppm; the liquid outlet sample analysis of water absorption acid generator '047 is as follows: hydrobromic acid content 41.2%, sulfate undetectable.

[0403] (4) The solid outlet 054 of the centrifuge 053 of the heated crystallizer II 051 was sampled and analyzed as follows: sodium bromide content 95.7%.

[0404] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate products mainly containing phthalic acid (TA); the solid outlet 080 of centrifuge 079 of heated crystallizer III077 can separate products mainly containing benzoic acid (BA); the phthalic acid (TA) and benzoic acid (BA) in the liquid outlet 081 of centrifuge 079 of heated crystallizer III077 can be removed by the organic matter removal device (benzene series adsorption device) 013; the solid in solid-liquid separator I016 is cobalt carbonate and manganese carbonate precipitated with sodium carbonate; the filtrate of solid-liquid separator I016, after being treated by heated evaporator I068 and solid-liquid separator VI070, and then having residual sodium carbonate removed by adding acid, can be processed according to four methods:

[0405] (1) A sodium bromide aqueous solution can be collected;

[0406] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0407] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0408] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0409] Similar to the relationship between Examples 1 and 2, it is also demonstrated that "nanofiltration system I" and "heating evaporation device I068, solid-liquid separator VI070" have the same effect, both of which can separate sodium bromide and sodium carbonate. "Nanofiltration system I" can be interchanged with "heating evaporation device I068, solid-liquid separator VI070" in terms of function.

[0410] Example 7

[0411] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using washing tank II073 and heated crystallizer III077 as examples), a cooling device 012, a filtration device I009 as an example), an organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, an oxidizing agent removal device 057, a nanofiltration membrane 022 of nanofiltration system I, a concentration system III (using reverse osmosis membrane 027 as an example), a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporator 037, or a heated crystallizer II051.

[0412] The solid outlet of the heated crystallizer I001 is connected to the inlet of the mixer II002. The mixer II002 is also provided with a liquid inlet 003. The outlet of the mixer II002 is connected to the inlet of the solid-liquid separator II004. The liquid outlet 006 of the solid-liquid separator II004 is connected to the inlet of the washing tank II073. The washing tank II073 is also provided with a washing liquid inlet 074. The aqueous phase outlet 075 of the washing tank II073 is connected to the inlet of the mixer I014. The mixer I014 is also provided with a chemical dosing port 015. The outlet of the mixer I014 is connected to the inlet of the solid-liquid separator I016. The liquid outlet 018 of the solid-liquid separator I016 is connected to the alkali addition stirring tank 019. The alkali addition stirring tank 019 is also provided with an alkali addition pipeline I020.

[0413] Solids are collected at the outlet of the solid-liquid separator II004;

[0414] The oil phase outlet 076 of the washing tank II 073 is connected to the inlet of the heating crystallizer III 077. The heating crystallizer III 077 is also equipped with a heater 078. The outlet of the heating crystallizer III 077 is connected to the inlet of the centrifuge 079 of the heating crystallizer III 077. The solid outlet 080 of the centrifuge 079 of the heating crystallizer III 077 collects the solids, and the liquid outlet 081 of the centrifuge 079 of the heating crystallizer III 077 is connected to the inlet of the heating crystallizer III 077.

[0415] Solids are collected at the solid outlet 017 of the solid-liquid separator I016;

[0416] The outlet of the alkali addition mixing tank 019 is connected to the inlet of the oxidizing agent 057. The outlet of the oxidizing agent 057 is connected to the inlet of the nanofiltration membrane 022 of nanofiltration system I via the high-pressure pump 021 of nanofiltration system I. The concentrate outlet 023 of the nanofiltration membrane 022 of nanofiltration system I is connected to the dosing port 015 of mixer I 014. The desalinated water outlet 024 of the nanofiltration membrane 022 of nanofiltration system I is connected to the inlet of buffer tank 025. The buffer tank 025 is connected to the inlet of the reverse osmosis membrane via the high-pressure pump 021 of reverse osmosis system I. Pump 026 is connected to reverse osmosis membrane 027. The concentrate outlet 028 of reverse osmosis membrane 027 is connected to the inlet of acid addition stirring tank 029. Acid addition stirring tank 029 is also equipped with acid addition pipeline I056. The outlet of acid addition stirring tank 029 is connected to the inlet of organic matter removal equipment (benzene series adsorption equipment, which is filled with benzene series adsorption resin). The outlet of organic matter removal equipment (benzene series adsorption equipment, which is filled with benzene series adsorption resin) 013 has the following four connection methods:

[0417] (1) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the collecting tank 030;

[0418] (2) The outlet of the acid mixing tank 029 is connected to the inlet of the bipolar membrane electrodialysis equipment 031. The bipolar membrane electrodialysis equipment 031 is also equipped with an alkali production tank 032, an acid production tank 034, and a brine tank 033. The outlet of the alkali production tank 032 is connected to the alkali addition pipeline I020 of the alkali mixing tank 019. The outlet of the brine tank 033 is connected to the inlet of the buffer tank 025. The outlet I035 of the acid production tank 034 is connected to the acid addition pipeline I056 of the acid mixing tank 029. The outlet II036 of the acid production tank 034 is connected to the oxidation system of the PTA unit.

[0419] (3) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the evaporator 037. The evaporator 037 is also equipped with a heater 038 and a dosing port 039. The gas phase outlet 040 of the evaporator 037 is connected to the inlet of the water absorption acid generator 041. The water absorption acid generator 041 is also equipped with a water dosing point 042. The liquid outlet of the water absorption acid generator 041 is connected to the inlet of the evaporator '043. The evaporator '043 is also equipped with a heater '044 and a dosing port '045. The gas phase outlet 046 of the evaporator '043 is connected to the inlet of the water absorption acid generator '047. The water absorption acid generator '047 is also equipped with a water dosing point '048. The outlet I 049 of the water absorption acid generator '047 is connected to the acid-adding pipeline I 056 of the acid-adding stirring tank 029. The outlet II 050 of the water absorption acid generator '047 is connected to the oxidation system of the PTA unit.

[0420] (4) The outlet of the acid-adding stirring tank 029 is connected to the inlet of the heating crystallizer II 051. The heating crystallizer II 051 is also equipped with a heater 052. The outlet of the heating crystallizer II 051 is connected to the inlet of the centrifuge 053. The solid outlet of the centrifuge 053 is collected, and the liquid outlet of the centrifuge 053 is connected to the inlet of the heating crystallizer II 051.

[0421] The above system operates as follows:

[0422] The target material processed in this embodiment is the oxidation residue of PTA. In all embodiments of this utility model, the target material processed is the oxidation residue of PTA, and the source of the oxidation residue of PTA is the heated crystallizer I001 equipment.

[0423] The PTA oxidation residue originates from the heated crystallizer I001. The solid outlet of the heated crystallizer I001 is the PTA oxidation residue, which enters the mixer II002 and is stirred with the addition of solvent benzene (from the inlet 003, approximately ten times the volume). After solid-liquid separation, it passes through the solid-liquid separator II004. The liquid outlet 006 of the solid-liquid separator II004 is mainly washed with water in the washing tank II073. The aqueous phase of the washing tank II073 (containing dissolved ions) then enters the mixer I014, and sodium carbonate aqueous solution is added to the mixer I014 (from the dosing port 015). After solid-liquid separation, it is separated by the solid-liquid separator I016. The filtrate from the solid-liquid separator I016 is adjusted for pH by adding sodium hydroxide (sodium hydroxide aqueous solution is added through the alkali addition stirring tank 019 and the alkali addition pipeline I020). It first passes through the oxidizing agent removal device 057 (filled with adsorption packing: activated carbon) to remove oxidizing agents, and then is treated by the nanofiltration membrane 022 of the nanofiltration system I.

[0424] After the oil phase from washing tank II073 is heated to remove solvent benzene in heating crystallizer III077, it is filtered through centrifuge 079 in heating crystallizer III077. The resulting solid BA is collected, and the liquid is recycled back to heating crystallizer III077 for reheating.

[0425] The concentrate outlet 023 of nanofiltration membrane 022 in nanofiltration system I is returned to the dosing port 015 of mixer I to provide sodium carbonate. The desalinated water outlet 024 of nanofiltration membrane 022 in nanofiltration system I (mainly sodium bromide) is concentrated by concentration system III (using reverse osmosis membrane 027 as an example). Then, acid is added to neutralize the sodium carbonate with hydrobromic acid (via acid addition stirring tank 029 and acid addition line I056, which provides hydrobromic acid). After passing through the organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013 to adsorb benzene series compounds, there are four treatment methods:

[0426] (1) Collect using collection container 030;

[0427] (2) The alkali obtained by the bipolar membrane electrodialysis equipment 031 is recycled back to the alkali addition pipeline I020 of the alkali addition stirring tank 019 to provide sodium hydroxide; part of the hydrobromic acid obtained is recycled back to the acid addition pipeline I056 of the acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate therein, and the other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of the PTA unit; the sodium bromide liquid in the brine tank 033 is recycled back to the buffer tank 025, and after being concentrated again by the reverse osmosis membrane, it is recycled back to the bipolar membrane electrodialysis equipment 031 for further treatment;

[0428] (3) The process is carried out using evaporator 037. Sulfuric acid is added from the chemical inlet 039 of evaporator 037 and heated by heater 038 to generate hydrogen bromide gas. Water is added to the acid generator 041 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. The hydrobromic acid aqueous solution then enters evaporator 043. Barium hydroxide is added from the chemical inlet 045 of evaporator 043 and heated by heater 044 to generate hydrogen bromide gas. Water is added to the acid generator 047 to absorb the hydrogen bromide gas and form a hydrobromic acid aqueous solution. Part of the hydrobromic acid aqueous solution is recycled back to the acid addition pipeline I056 of acid addition stirring tank 029 to provide hydrobromic acid to neutralize the sodium carbonate in it. The other part is used as the product hydrobromic acid of this unit and reused in the oxidation system of PTA unit.

[0429] (4) Evaporate and concentrate using heating crystallizer II051, and produce sodium bromide solid product using centrifuge 053. The filtrate from centrifuge 053 is then returned to heating crystallizer II051 for reheating. This continuous cycle produces sodium bromide solid product.

[0430] The solids from solid-liquid separator II004 are washed in washing tank IV058. Water (approximately ten times the volume) is added to the washing liquid inlet 059 of washing tank IV058 for washing. Afterwards, solids and liquids are separated in solid-liquid separator IV060. The resulting liquid is recycled back to mixer II002, and the resulting solids are collected.

[0431] The solids in the filter equipment I009 are washed in the washing tank V063. Water (about twenty times the volume) is added to the washing liquid inlet 064 of the washing tank V063 for washing. Then, solid-liquid separation is performed in the solid-liquid separator V065. The resulting liquid is recycled back to the mixer II002, and the resulting solids are collected.

[0432] Solid collection in solid-liquid separator I016;

[0433] Run the experiment using the above system:

[0434] Add solvent benzene to the inlet 003 of mixer Ⅱ002 and stir. Take a sample from the solid outlet 005 of solid separator Ⅱ004 for analysis: phthalic acid (TA) = 62.14%, benzoic acid (BA) = 0.78%, benzene content 36%;

[0435] Analysis of a sample taken from the solid outlet 080 of the centrifuge 079 of the heated crystallizer Ⅲ077 showed: benzoic acid (BA) = 83.15%, benzene content 15%;

[0436] A sample was taken from the solid outlet 017 of the solid-liquid separator I016: cobalt carbonate 32.8%, manganese carbonate 27.7%, and water content approximately 39%.

[0437] The pH of the effluent from the alkali addition stirring tank 019 was controlled at 11.5. Analysis of the concentrate outlet 023 of the nanofiltration membrane 022 of nanofiltration system I 020 showed: carbonate 50085 ppm and bromide 1446 ppm. Analysis of the desalination outlet 024 of the nanofiltration membrane 022 of nanofiltration system I 020 showed: carbonate 3221 ppm and bromide 9898 ppm.

[0438] The pH of the acid addition stirring tank 029 was controlled at 3.5; sodium bromide was 98137 ppm, phthalic acid (TA) was 9812 ppm, and benzoic acid (BA) was 28172 ppm; samples were taken from the outlet of the organic matter removal device (benzene series adsorption device) 013: phthalic acid (TA) was 8 ppm, and benzoic acid (BA) was 5 ppm.

[0439] There are four possible processing methods:

[0440] (1) Collected as sodium bromide aqueous solution product;

[0441] (2) The following is the analysis of the acid production tank 034 of the bipolar membrane electrodialysis equipment 031: hydrogen ions 1.77mol / L, bromide ions 13.9%, sodium ions 90ppm, proving that the product is hydrobromic acid;

[0442] (3) The liquid outlet sample analysis of water absorption acid generator 041 is as follows: hydrobromic acid content 22.3%, sulfate 126ppm; the liquid outlet sample analysis of water absorption acid generator '047 is as follows: hydrobromic acid content 36.5%, sulfate undetectable.

[0443] (4) The solid outlet 054 of the centrifuge 053 of the heated crystallizer Ⅱ051 was sampled and analyzed as follows: sodium bromide content 97.1%.

[0444] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate products mainly containing phthalic acid (TA); the solid outlet 010 of filtration device I009 can separate products mainly containing benzoic acid (BA); the solids of solid-liquid separator I016 are cobalt carbonate and manganese carbonate products precipitated with sodium carbonate; the filtrate of solid-liquid separator I016 is separated by nanofiltration membrane 022 of nanofiltration system I into an aqueous solution mainly containing sodium carbonate (concentrated water of nanofiltration membrane 022) and an aqueous solution mainly containing sodium bromide (dehydrated water of nanofiltration membrane 022). The dehydrated water of nanofiltration membrane 022 (mainly containing sodium bromide) is concentrated by reverse osmosis, and then acidified to remove residual sodium carbonate. The phthalic acid (TA) and benzoic acid (BA) can be removed by organic matter removal device (benzene series adsorption device) 013, and then can be processed by four methods:

[0445] (1) A sodium bromide aqueous solution can be collected;

[0446] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0447] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0448] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

[0449] Meanwhile, Example 7 demonstrates that placing the organic matter removal device (benzene series adsorption device, internally filled with benzene series adsorption resin) 013 between the benzoic acid extraction device (using washing tank II 073 and heating crystallizer III 077 as examples) and the inlet of mixer I 014, or placing the organic matter removal device (benzene series adsorption device, internally filled with benzene series adsorption resin) 013 between the acid stirring tank 029 and the inlet of the collection tank, the inlet of the evaporator, the inlet of the bipolar membrane electrodialysis device, or the inlet of the heating crystallizer II, achieves the same effect. That is, the purpose of the organic matter removal device (benzene series adsorption device, internally filled with benzene series adsorption resin) 013 is to remove organic matter (benzene series), and its position in the above two locations has the same functional effect, and its position in the above two locations can be interchanged.

[0450] Example 8

[0451] A PTA oxidation residue treatment system mainly includes a heated crystallizer I001, a phthalic acid extraction device (using mixer II002 and solid-liquid separator II004 as examples), a benzoic acid extraction device (using washing tank II073 and heated crystallizer III077 as examples), an organic matter removal device (benzene series adsorption device, which is filled with benzene series adsorption resin) 013, a mixer I014, a solid-liquid separator I016, a heated evaporation device I068, a solid-liquid separator VI070, a collection tank 030, or a bipolar membrane electrodialysis device 031, or an evaporation tank 037, or a heated crystallizer II051.

[0452] Based on Example 7, the "nanofiltration system I" in Example 7 is replaced with "heating evaporation equipment I068 and solid-liquid separator VI070".

[0453] Specific connection method:

[0454] Based on Example 7, the outlet of the alkali addition stirring tank 019 in Example 7 is connected to the inlet of the oxidizing agent 057; the outlet of the oxidizing agent 057 is connected to the inlet of the nanofiltration membrane 022 of nanofiltration system I via the high-pressure pump 021 of nanofiltration system I; the concentrate outlet 023 of the nanofiltration membrane 022 of nanofiltration system I is connected to the dosing port 015 of mixer I 014; the desalination outlet 024 of the nanofiltration membrane 022 of nanofiltration system I is connected to the inlet of buffer tank 025; and the buffer tank 025 is connected to the reverse osmosis membrane via the high-pressure pump 026 of reverse osmosis membrane. The phrase “the concentrated water outlet 028 of the reverse osmosis membrane 027 is connected to the inlet of the acid mixing tank 029” is replaced with “the outlet of the alkali mixing tank 019 is connected to the inlet of the heating evaporation equipment I 068, the heating evaporation equipment I 068 is also equipped with a heater 069, the outlet of the heating evaporation equipment I 068 is connected to the inlet of the solid-liquid separator VI 070, the solid outlet 071 of the solid-liquid separator VI 070 is connected to the dosing port 015 of the mixer I 014, and the liquid outlet 072 of the solid-liquid separator VI 070 is connected to the inlet of the acid mixing tank 029”.

[0455] The above system operates as follows:

[0456] Based on Example 7, the process of "first removing oxidizing agents through an oxidizing agent removal device 057 (filled with adsorption packing material: activated carbon), then treating with nanofiltration membrane 022 of nanofiltration system I, the concentrate outlet 023 of nanofiltration membrane 022 of nanofiltration system I returning to the dosing port 015 of mixer I to provide sodium carbonate, the desalinated water outlet 024 of nanofiltration membrane 022 of nanofiltration system I (mainly sodium bromide) being concentrated by concentration system III (using reverse osmosis membrane 027 as an example), and then adding acid to neutralize the sodium carbonate with hydrobromic acid (after adding acid)" is further modified. The phrase “acid stirring tank 029 and acid adding line I056, acid adding line I056 is used to provide hydrobromic acid” is replaced with “processed by heating evaporation equipment I068 and solid-liquid separator VI070; the solid outlet 071 of solid-liquid separator VI070 is connected to the dosing port 015 of mixer I014 to provide sodium carbonate; the liquid outlet 072 of solid-liquid separator VI070 (mainly sodium bromide) is acidified to neutralize sodium carbonate with hydrobromic acid (passing through acid stirring tank 029 and acid adding line I056, acid adding line I056 is used to provide hydrobromic acid)”.

[0457] Run the experiment using the above system:

[0458] Example 6 demonstrates that the "nanofiltration system I" and the "heating evaporation device I068 and solid-liquid separator VI070" have the same effect, both being able to separate sodium bromide and sodium carbonate. The "nanofiltration system I" is functionally interchangeable with the "heating evaporation device I068 and solid-liquid separator VI070". It can be inferred that, based on Example 7, replacing the "nanofiltration system I" with the "heating evaporation device I068 and solid-liquid separator VI070" can also achieve the same effect.

[0459] Conclusion: After processing by this system, the solid outlet 005 of solid-liquid separator II004 can separate products mainly containing phthalic acid (TA); the solid outlet 010 of filter I009 can separate products mainly containing benzoic acid (BA); the solids of solid-liquid separator I016 are cobalt carbonate and manganese carbonate products precipitated with sodium carbonate; after the filtrate of solid-liquid separator I016 is treated by heating evaporation equipment I068 and solid-liquid separator VI070, the filtrate is acidified to remove residual sodium carbonate, and the phthalic acid (TA) and benzoic acid (BA) can be removed by organic matter removal equipment (benzene series adsorption equipment) 013, and then can be processed by four methods:

[0460] (1) A sodium bromide aqueous solution can be collected;

[0461] (2) Hydrobromic acid can be obtained by conversion using bipolar membrane electrodialysis equipment 031;

[0462] (3) Evaporator 037 can be used in conjunction with water absorption acid generator 041 to convert hydrobromic acid product, but it contains a small amount of sulfuric acid. At the same time, the hydrobromic acid product obtained by using evaporator 043 in conjunction with water absorption acid generator 047 does not contain sulfuric acid.

[0463] (4) Sodium bromide solid was obtained by treating with heated crystallizer II.

Claims

1. A system for treating PTA oxidation residue, characterized in that, The system includes: a heated crystallizer I, a phthalic acid extraction device, an organic matter removal device, and also includes a collection tank, a heated crystallizer II, a bipolar membrane electrodialysis device or an evaporator; The solid outlet of the heated crystallizer I is connected to the inlet of the phthalic acid extraction device, the liquid outlet of the phthalic acid extraction device is connected to the inlet of the mixer I, the mixer I is also provided with a dosing port, the outlet of the mixer I is connected to the inlet of the solid-liquid separator I, and the liquid outlet of the solid-liquid separator I is connected to the inlet of the collection tank, the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, or the inlet of the evaporator. Alternatively, the solid outlet of the heated crystallizer I can be connected to the inlet of the phthalic acid extraction device, the liquid outlet of the phthalic acid extraction device can be connected to the inlet of the cobalt-manganese adsorption device, and the outlet of the cobalt-manganese adsorption device can be connected to the inlet of the collection tank, the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, or the inlet of the evaporator. The organic matter removal device is located between the liquid outlet of the phthalic acid extraction device and the inlet of the mixer I; or the organic matter removal device is located between the liquid outlet of the phthalic acid extraction device and the inlet of the cobalt-manganese adsorption device; or the organic matter removal device is located between the liquid outlet of the solid-liquid separator I and the inlet of the heated crystallizer II; or the organic matter removal device is located between the liquid outlet of the solid-liquid separator I and the inlet of the bipolar membrane electrodialysis device; or the organic matter removal device is located between the liquid outlet of the solid-liquid separator I and the inlet of the collector. The organic matter removal device is located between the inlet of the collecting tank; or between the liquid outlet of the solid-liquid separator I and the inlet of the evaporator; or between the outlet of the cobalt-manganese adsorption device and the inlet of the heated crystallizer II; or between the outlet of the cobalt-manganese adsorption device and the inlet of the bipolar membrane electrodialysis device; or between the outlet of the cobalt-manganese adsorption device and the inlet of the collecting tank; or between the outlet of the cobalt-manganese adsorption device and the inlet of the evaporator.

2. The processing system according to claim 1, characterized in that, The organic matter removal equipment is a benzene series adsorption equipment or an incineration equipment; And / or, the phthalic acid extraction device includes a mixer II and a solid-liquid separator II. The inlet of the mixer II is the inlet of the phthalic acid extraction device. The mixer II is also provided with a liquid inlet. The outlet of the mixer II is connected to the inlet of the solid-liquid separator II. The liquid outlet of the solid-liquid separator II is the liquid outlet of the phthalic acid extraction device.

3. The processing system according to claim 1 or 2, characterized in that, It also includes a benzoic acid extraction device; the liquid outlet of the benzoic acid extraction device is connected to the inlet of the benzoic acid extraction device, and the liquid outlet of the benzoic acid extraction device is connected to the inlet of the mixer I, the inlet of the cobalt-manganese adsorption device, or the inlet of the organic matter elimination device; The benzoic acid extraction device includes: a cooling device and a filtration device I; the inlet of the cooling device is the inlet of the benzoic acid extraction device, the outlet of the cooling device is connected to the inlet of the filtration device I, and the liquid outlet of the filtration device I is the liquid outlet of the benzoic acid extraction device; Alternatively, the benzoic acid extraction device may include: a concentration device and a filtration device I; the inlet of the concentration device is the inlet of the benzoic acid extraction device, the outlet of the concentration device is connected to the inlet of the filtration device I, and the liquid outlet of the filtration device I is the liquid outlet of the benzoic acid extraction device; Alternatively, the benzoic acid extraction device may include: a concentration device, a cooling device, and a filtration device I; the inlet of the concentration device is the inlet of the benzoic acid extraction device, the outlet of the concentration device is connected to the inlet of the cooling device, the outlet of the cooling device is connected to the inlet of the filtration device I, and the liquid outlet of the filtration device I is the liquid outlet of the benzoic acid extraction device; or the inlet of the cooling device is the inlet of the benzoic acid extraction device, the outlet of the cooling device is connected to the inlet of the concentration device, the outlet of the concentration device is connected to the inlet of the filtration device I, and the liquid outlet of the filtration device I is the liquid outlet of the benzoic acid extraction device. Alternatively, the benzoic acid extraction device may include: an integrated cooling and filtration unit; the inlet of the integrated cooling and filtration unit is the inlet of the benzoic acid extraction device, and the liquid outlet of the integrated cooling and filtration unit is the liquid outlet of the benzoic acid extraction device; Alternatively, the benzoic acid extraction device may include: a concentration device and a cooling and filtration integrated machine, wherein the inlet of the concentration device is the inlet of the benzoic acid extraction device, the outlet of the concentration device is connected to the inlet of the cooling and filtration integrated machine, and the liquid outlet of the cooling and filtration integrated machine is the liquid outlet of the benzoic acid extraction device. Alternatively, the benzoic acid extraction device may include: a mixer III and a filter II, wherein the inlet of the mixer III is the inlet of the benzoic acid extraction device, the mixer III is also provided with a liquid inlet, the outlet of the mixer III is connected to the inlet of the filter II, and the liquid outlet of the filter II is the liquid outlet of the benzoic acid extraction device. Alternatively, the benzoic acid extraction device may include: a heated crystallizer III, the inlet of which is also the inlet of the benzoic acid extraction device; the solid outlet of the heated crystallizer III is connected to the inlet of a washing tank I; the washing tank I also has a washing liquid inlet; the outlet of the washing tank I is connected to the inlet of a filtration device III; and the liquid outlet of the filtration device III is also the liquid outlet of the benzoic acid extraction device. Alternatively, the inlet of the heated crystallizer III is also the inlet of the benzoic acid extraction device; the solid outlet of the heated crystallizer III is connected to the inlet of a washing and filtration integrated machine I; the washing and filtration integrated machine I also has a washing liquid inlet; and the liquid outlet of the washing and filtration integrated machine I is also the liquid outlet of the benzoic acid extraction device. Alternatively, the inlet of the heated crystallizer III is also the inlet of the benzoic acid extraction device; the heated crystallizer III also has a washing liquid inlet; the outlet of the heated crystallizer III is connected to the inlet of a filtration device III; and the liquid outlet of the filtration device III is also the liquid outlet of the benzoic acid extraction device. Alternatively, the benzoic acid extraction device may include: a heating crystallizer III and a washing tank II. The inlet of the washing tank II is the inlet of the benzoic acid extraction device. The washing tank II is also provided with a washing liquid inlet. The aqueous phase outlet of the washing tank II is the liquid outlet of the benzoic acid extraction device. The oil phase outlet of the washing tank II is connected to the inlet of the heating crystallizer III, and the solid phase outlet of the heating crystallizer III is used for collection.

4. The processing system according to claim 1, characterized in that, It also includes a nanofiltration system I; The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the nanofiltration system I. The freshwater outlet of the nanofiltration system I is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporator. Alternatively, the inlet of the organic matter removal device may be connected to the inlet of the nanofiltration system I, and the freshwater outlet of the nanofiltration system I may be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

5. The processing system according to claim 2, characterized in that, It also includes a nanofiltration system I; The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the nanofiltration system I. The freshwater outlet of the nanofiltration system I is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporator. Alternatively, the inlet of the organic matter removal device may be connected to the inlet of the nanofiltration system I, and the freshwater outlet of the nanofiltration system I may be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

6. The processing system according to claim 3, characterized in that, It also includes a nanofiltration system I; The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the nanofiltration system I. The freshwater outlet of the nanofiltration system I is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporator. Alternatively, the inlet of the organic matter removal device may be connected to the inlet of the nanofiltration system I, and the freshwater outlet of the nanofiltration system I may be connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

7. The processing system according to claim 1, characterized in that, It is also equipped with heating and evaporation equipment I and solid-liquid separator VI; The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the outlet of the organic matter removal device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the cooling device ', the outlet of the cooling device ' may be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the outlet of the organic matter removal device can be first connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II may be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the fresh water outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device can be first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I can be connected to the inlet of the cooling device '. The outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II. The freshwater outlet of the nanofiltration system II can be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank.

8. The processing system according to claim 2, characterized in that, It is also equipped with heating and evaporation equipment I and solid-liquid separator VI; The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the outlet of the organic matter removal device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the cooling device ', the outlet of the cooling device ' may be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the outlet of the organic matter removal device can be first connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II may be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the fresh water outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device can be first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I can be connected to the inlet of the cooling device '. The outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II. The freshwater outlet of the nanofiltration system II can be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank.

9. The processing system according to claim 3, characterized in that, It is also equipped with heating and evaporation equipment I and solid-liquid separator VI; The liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device is first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I is connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI is connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the organic matter removal device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the outlet of the organic matter removal device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the cooling device ', the outlet of the cooling device ' may be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the outlet of the organic matter removal device can be first connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, and the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I may be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI may be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II may be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank; Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the fresh water outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the liquid outlet of the solid-liquid separator I or the outlet of the cobalt-manganese adsorption device can be first connected to the inlet of the heating evaporation device I. The outlet of the heating evaporation device I can be connected to the inlet of the cooling device '. The outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI. The liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II. The freshwater outlet of the nanofiltration system II can be connected to the inlet of the organic matter removal device, the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank. Alternatively, the outlet of the organic matter removal device can be connected to the inlet of the heating evaporation device I, the outlet of the heating evaporation device I can be connected to the inlet of the cooling device ', the outlet of the cooling device ' can be connected to the inlet of the solid-liquid separator VI, the liquid outlet of the solid-liquid separator VI can be connected to the inlet of the nanofiltration system II, and the freshwater outlet of the nanofiltration system II can be connected to the inlet of the heating crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporation tank.

10. The processing system according to claim 4, 5 or 6, characterized in that, It is also equipped with an alkali addition pipeline I or a heating device I; The alkali addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the nanofiltration system I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the nanofiltration system I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the organic matter removal device and the inlet of the nanofiltration system I, and the connection point is called connection point a. The outlet of the organic matter removal device, the liquid outlet of the solid-liquid separator I, or the outlet of the cobalt-manganese adsorption device is connected to the inlet of the heating device I, and the outlet of the heating device I is connected to the inlet of the nanofiltration system I.

11. The processing system according to claim 7, 8 or 9, characterized in that, It is also equipped with an alkali addition pipeline I or a heating device I; The alkali addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the heating evaporation device I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the heating evaporation device I, and the connection point is called connection point a; or the alkali addition pipeline I is connected between the outlet of the organic matter removal device and the inlet of the heating evaporation device I, and the connection point is called connection point a. Alternatively, the outlet of the organic matter removal device, the liquid outlet of the solid-liquid separator I, or the outlet of the cobalt-manganese adsorption device may be connected to the inlet of the heating device I, and the outlet of the heating device I may be connected to the inlet of the heating evaporation device I.

12. The processing system according to claim 4, 5 or 6, characterized in that, It is also equipped with acid addition pipeline I; The acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the heated crystallizer II, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the bipolar membrane electrodialysis device, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the organic matter removal device, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the collection tank, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the evaporator, and the connection point is called connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the heated crystallizer II, with the acid addition line I connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the bipolar membrane electrodialysis device, with the acid addition line I connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the organic matter removal device. Between the inlets and outlets, the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is set between the freshwater outlet of the nanofiltration system I and the inlet of the collection tank, and the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is set between the freshwater outlet of the nanofiltration system I and the inlet of the evaporator, and the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b.

13. The processing system according to claim 10, characterized in that, It is also equipped with acid addition pipeline I; The acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the heated crystallizer II, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the bipolar membrane electrodialysis device, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the organic matter removal device, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the collection tank, and the connection point is called connection point b; or the acid addition line I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the evaporator, and the connection point is called connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the heated crystallizer II, with the acid addition line I connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the bipolar membrane electrodialysis device, with the acid addition line I connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I may be installed between the freshwater outlet of the nanofiltration system I and the inlet of the organic matter removal device. Between the inlets and outlets, the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is set between the freshwater outlet of the nanofiltration system I and the inlet of the collection tank, and the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is set between the freshwater outlet of the nanofiltration system I and the inlet of the evaporator, and the acid addition pipeline I is connected between the freshwater outlet of the nanofiltration system I and the inlet of the decarbonization tower I, and the connection point is called connection point b.

14. The processing system according to claim 7, 8 or 9, characterized in that, It is also equipped with acid addition pipeline I; The acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the heated crystallizer II, and the connection point is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the bipolar membrane electrodialysis device, and the connection point is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the organic matter removal device, and the connection point is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the collection tank, and the connection point is called connection point b; or the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the evaporator, and the connection point is called connection point b. Alternatively, a decarbonization tower I can be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the heated crystallizer II, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I can be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the bipolar membrane electrodialysis equipment, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I; this connection point is referred to as connection point b. Alternatively, a decarbonization tower I can be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the organic matter removal equipment. Between the inlets and outlets, the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is provided, which is located between the liquid outlet of the solid-liquid separator VI and the inlet of the collection tank, and the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I, and the connection point is called connection point b; or a decarbonization tower I is provided, which is located between the liquid outlet of the solid-liquid separator VI and the inlet of the evaporator, and the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the decarbonization tower I, and the connection point is called connection point b.

15. The processing system according to claim 1, 4, 5, 6, 7, 8 or 9, characterized in that, It is also equipped with acid addition pipeline I; The acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the organic matter removal device, and the connection position is called connection point e; or the acid addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, and the connection position is called connection point e; Alternatively, a decarbonization tower I may be installed, located between the liquid outlet of the solid-liquid separator I and the inlet of the organic matter removal device, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separator I and the inlet of the decarbonization tower I, the connection point being referred to as connection point e; or a decarbonization tower I may be installed, located between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, with the acid addition pipeline I connected between the outlet of the cobalt-manganese adsorption device and the inlet of the decarbonization tower I, the connection point being referred to as connection point e.

16. The processing system according to claim 10, characterized in that, It is also equipped with acid addition pipeline I; The acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the organic matter removal device, and the connection position is called connection point e; or the acid addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, and the connection position is called connection point e; Alternatively, a decarbonization tower I may be installed, located between the liquid outlet of the solid-liquid separator I and the inlet of the organic matter removal device, with the acid addition pipeline I connected between the liquid outlet of the solid-liquid separator I and the inlet of the decarbonization tower I, the connection point being referred to as connection point e; or a decarbonization tower I may be installed, located between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, with the acid addition pipeline I connected between the outlet of the cobalt-manganese adsorption device and the inlet of the decarbonization tower I, the connection point being referred to as connection point e.

17. The processing system according to claim 11, characterized in that, It is also equipped with acid addition pipeline I; The acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the organic matter removal device, and the connection point is called connection point e; or the acid addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, and the connection point is called connection point e; or a decarbonization tower I is provided, which is located between the liquid outlet of the solid-liquid separator I and the inlet of the organic matter removal device, and the acid addition pipeline I is connected between the liquid outlet of the solid-liquid separator I and the inlet of the decarbonization tower I, and the connection point is called connection point e; or a decarbonization tower I is provided, which is located between the outlet of the cobalt-manganese adsorption device and the inlet of the organic matter removal device, and the acid addition pipeline I is connected between the outlet of the cobalt-manganese adsorption device and the inlet of the decarbonization tower I, and the connection point is called connection point e.

18. The processing system according to claim 7, 8 or 9, characterized in that, It is also equipped with an alkali addition pipeline II and a heating device II or an acid addition pipeline II; The alkali addition pipeline II is connected between the liquid outlet of the solid-liquid separator VI and the inlet of the nanofiltration system II, and the connection point is called connection point c; Alternatively, the heating device II may be installed between the liquid outlet of the solid-liquid separator VI and the inlet of the nanofiltration system II; Alternatively, the acid addition line II can be connected between the liquid outlet of the solid-liquid separator VI and the inlet of the nanofiltration system II, and the connection point is called connection point d.

19. The processing system according to claim 4, 5 or 6, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the nanofiltration system I.

20. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the nanofiltration system I.

21. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the heating device I.

22. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the heating device I.

23. The processing system according to claim 1, 4, 5, 6, 7, 8, 9, 16 or 17, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the organic matter removal device.

24. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the organic matter removal device.

25. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the organic matter removal device.

26. The processing system according to claim 15, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the organic matter removal device.

27. The processing system according to claim 7, 8 or 9, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the heating evaporation device I.

28. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the heating evaporation device I.

29. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the connection point a.

30. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the connection point a.

31. The processing system according to claim 15, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the connection point e.

32. The processing system according to claim 16 or 17, characterized in that, It also includes a concentration system II; The liquid outlet of the solid-liquid separator I is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the connection point e.

33. The processing system according to claim 4, 5 or 6, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the nanofiltration system I.

34. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the nanofiltration system I.

35. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrated liquid of the concentration system II is connected to the inlet of the heating device I.

36. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrated liquid of the concentration system II is connected to the inlet of the heating device I.

37. The processing system according to claim 1, 4, 5, 6, 7, 8, 9, 16 or 17, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the organic matter elimination device.

38. The processing system according to claim 3, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the organic matter elimination device.

39. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the organic matter elimination device.

40. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the organic matter elimination device.

41. The processing system according to claim 15, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the organic matter elimination device.

42. The processing system according to claim 7, 8 or 9, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrated liquid of the concentration system II is connected to the inlet of the heating evaporation device I.

43. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrated liquid of the concentration system II is connected to the inlet of the heating evaporation device I.

44. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point a.

45. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point a.

46. ​​The processing system according to claim 15, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point e.

47. The processing system according to claim 16 or 17, characterized in that, It also includes a concentration system II; The outlet of the cobalt-manganese adsorption device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point e.

48. The processing system according to claim 4, 5, 6 or 13, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the concentrate outlet of the concentration system II is connected to the inlet of the nanofiltration system I.

49. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the concentrate outlet of the concentration system II is connected to the inlet of the nanofiltration system I.

50. The processing system according to claim 12, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the concentrate outlet of the concentration system II is connected to the inlet of the nanofiltration system I.

51. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the heating device I.

52. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the heating device I.

53. The processing system according to claim 7, 8 or 9, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the heating evaporation device I.

54. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the organic matter removal device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the inlet of the heating evaporation device I.

55. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of the organic matter elimination device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point a.

56. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of the organic matter elimination device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point a.

57. The processing system according to claim 12, characterized in that, It also includes a concentration system II; The outlet of the organic matter elimination device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point b.

58. The processing system according to claim 13, characterized in that, It also includes a concentration system II; The outlet of the organic matter elimination device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point b.

59. The processing system according to claim 14, characterized in that, It also includes a concentration system II; The outlet of the organic matter elimination device is connected to the inlet of the concentration system II, and the outlet of the concentrate of the concentration system II is connected to the connection point b.

60. The processing system according to claim 10, characterized in that, It also includes a concentration system II; Connection point a is connected to the inlet of the concentration system II, and the concentrate outlet of the concentration system II is connected to the inlet of the nanofiltration system I.

61. The processing system according to claim 11, characterized in that, It also includes a concentration system II; Connection point a is connected to the inlet of the concentration system II, and the concentrated liquid outlet of the concentration system II is connected to the inlet of the heating and evaporation equipment I.

62. The processing system according to claim 10, characterized in that, It also includes a concentration system II; The outlet of heating device I is connected to the inlet of concentration system II, and the concentrate outlet of concentration system II is connected to the inlet of nanofiltration system I.

63. The processing system according to claim 11, characterized in that, It also includes a concentration system II; The outlet of heating device I is connected to the inlet of concentration system II, and the outlet of concentrated liquid from concentration system II is connected to the inlet of heating evaporation device I.

64. The processing system according to claim 4, 5, 6 or 13, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to the inlet of heated crystallizer II, the inlet of bipolar membrane electrodialysis equipment, the inlet of collection tank, or the inlet of evaporator.

65. The processing system according to claim 12, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to the inlet of heated crystallizer II, the inlet of bipolar membrane electrodialysis equipment, the inlet of collection tank, or the inlet of evaporator.

66. The processing system according to claim 12, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to connection point b.

67. The processing system according to claim 13, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to connection point b.

68. The processing system according to claim 4, 5, 6 or 13, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to the inlet of organic matter removal equipment.

69. The processing system according to claim 10, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to the inlet of organic matter removal equipment.

70. The processing system according to claim 12, characterized in that, It also includes a concentration system III; The freshwater outlet of nanofiltration system I is connected to the inlet of concentration system III, and the concentrate outlet of concentration system III is connected to the inlet of organic matter removal equipment.

71. The processing system according to claim 7, 8 or 9, characterized in that, It also includes a concentration system III; The freshwater outlet of the nanofiltration system II is connected to the inlet of the concentration system III, and the concentrate outlet of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, or the inlet of the organic matter removal device.

72. The processing system according to claim 7, 8 or 9, characterized in that, It also includes a concentration system III; The liquid outlet of the solid-liquid separator VI is connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, or the inlet of the organic matter removal device.

73. The processing system according to claim 14, characterized in that, It also includes a concentration system III; The liquid outlet of the solid-liquid separator VI is connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, or the inlet of the organic matter removal device.

74. The processing system according to claim 14, characterized in that, It also includes a concentration system III; The liquid outlet of the solid-liquid separator VI is connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III is connected to the connection point b.

75. The processing system according to claim 12, characterized in that, It also includes a concentration system III; The outlet of the decarbonization tower I is connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, the connection point b, or the inlet of the organic matter removal device.

76. The processing system according to claim 13, characterized in that, It also includes a concentration system III; The outlet of the decarbonization tower I is connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, the connection point b, or the inlet of the organic matter removal device.

77. The processing system according to claim 14, characterized in that, It also includes a concentration system III; The outlet of the decarbonization tower I is connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, the inlet of the evaporator, the connection point b, or the inlet of the organic matter removal device.

78. The processing system according to claim 15, characterized in that, It also includes a concentration system III; The outlet of the decarbonization tower I is connected to the inlet of the organic matter removal equipment.

79. The processing system according to claim 16 or 17, characterized in that, It also includes a concentration system III; The outlet of the decarbonization tower I is connected to the inlet of the organic matter removal equipment.

80. The processing system according to claim 12, characterized in that, It also includes a concentration system III; The outlet of connection point b is connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis equipment, the inlet of the collection tank, or the inlet of the evaporator.

81. The processing system according to claim 13, characterized in that, It also includes a concentration system III; The outlet of connection point b is connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis equipment, the inlet of the collection tank, or the inlet of the evaporator.

82. The processing system according to claim 14, characterized in that, It also includes a concentration system III; The outlet of connection point b is connected to the inlet of the concentration system III, and the concentrated liquid outlet of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis equipment, the inlet of the collection tank, or the inlet of the evaporator.

83. The processing system according to claim 1, 4, 5, 6, 7, 8, 9 or 13, characterized in that, It also includes a concentration system III; The outlet of the organic matter removal device is connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

84. The processing system according to claim 12, characterized in that, It also includes a concentration system III; The outlet of the organic matter removal device is connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

85. The processing system according to claim 14, characterized in that, It also includes a concentration system III; The outlet of the organic matter removal device is connected to the inlet of the concentration system III, and the outlet of the concentrate of the concentration system III is connected to the inlet of the heated crystallizer II, the inlet of the bipolar membrane electrodialysis device, the inlet of the collection tank, or the inlet of the evaporator.

86. The processing system according to any one of claims 1, 4, 5, 6, 7, 8, 9, 13, 65, 73, 74, 75, 76, 77, 80, 81, 82, 84 or 85, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

87. The processing system according to claim 12, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

88. The processing system according to claim 14, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

89. The processing system according to claim 64, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

90. The processing system according to claim 71, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

91. The processing system according to claim 72, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

92. The processing system according to claim 83, characterized in that, The evaporator is also equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to a collection tank or a water absorption acid generator.

93. The processing system according to claim 86, characterized in that, The liquid outlet of the water absorption acid generator is also equipped with a heater, or the liquid outlet of the water absorption acid generator is connected to the inlet of the evaporator, the evaporator is equipped with a heater, and the gas phase outlet of the evaporator is connected to the collection tank or the water absorption acid generator; or the liquid outlet of the water absorption acid generator is connected to the inlet of the evaporator, the evaporator is equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to the collection tank or the water absorption acid generator.

94. The processing system according to claim 2, characterized in that, It also includes a dryer I; The solid outlet of the solid-liquid separator II is connected to the inlet of the dryer I.

95. The processing system according to claim 3, characterized in that, It also includes a dryer II; The solid outlet of the filter device I, the solid outlet of the integrated cooling and filtration machine, the solid outlet of the filter device II, the solid outlet of the filter device III, or the solid outlet of the integrated washing and filtration machine I are connected to the inlet of the dryer II.

96. The processing system according to claim 2 or 94, characterized in that, The solid outlet of the solid-liquid separator II is collected or connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator II is connected to a pulping tank, which is also provided with a liquid inlet, and the outlet of the pulping tank is connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator II is first connected to a pipeline mixer and then connected to the oxidation system of the PTA unit. Alternatively, the solid outlet of the solid-liquid separator II can be connected to the inlet of the washing tank IV, which also has a washing liquid inlet. The outlet of the washing tank IV can be connected to the inlet of the solid-liquid separator IV, and the solid outlet of the solid-liquid separator IV can be collected or connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator IV can be connected to a pulping tank, which also has a liquid inlet. The outlet of the pulping tank can be connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator IV can be mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA unit; the liquid outlet of the solid-liquid separator IV can be connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter removal device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device. Alternatively, the solid outlet of the solid-liquid separator II can be connected to the inlet of the washing and filtering integrated machine II, which also has a washing liquid inlet. The solid outlet of the washing and filtering integrated machine II can be collected or connected to the oxidation system of the PTA unit. Alternatively, the solid outlet of the washing and filtering integrated machine II can be connected to a pulping tank, which also has a liquid inlet. The outlet of the pulping tank can be connected to the oxidation system of the PTA unit. Alternatively, the solid outlet of the washing and filtering integrated machine II can be mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA unit. The liquid outlet of the washing and filtering integrated machine II can be connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter removal device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device.

97. The processing system according to claim 94, characterized in that, The solid outlet of the dryer I is collected or connected to the oxidation system of the PTA unit; or the solid outlet of the dryer I is connected to a pulping tank, which is also provided with a liquid inlet, and the outlet of the pulping tank is connected to the oxidation system of the PTA unit; or the solid outlet of the dryer I is first connected to a pipe mixer and then connected to the oxidation system of the PTA unit. Alternatively, the solid outlet of the dryer I can be connected to the inlet of the washing tank IV, which also has a washing liquid inlet. The outlet of the washing tank IV can be connected to the inlet of the solid-liquid separator IV, and the solid outlet of the solid-liquid separator IV can be collected or connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator IV or the solid outlet of the dryer I can be connected to a pulping tank, which also has a liquid inlet. The outlet of the pulping tank can be connected to the oxidation system of the PTA unit; or the solid outlet of the solid-liquid separator IV can be mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA unit; the liquid outlet of the solid-liquid separator IV can be connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter removal device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device. Alternatively, the solid outlet of the dryer I can be connected to the inlet of the washing and filtering integrated machine II, which also has a washing liquid inlet. The solid outlet of the washing and filtering integrated machine II can be collected or connected to the oxidation system of the PTA unit. Alternatively, the solid outlet of the washing and filtering integrated machine II can be connected to a pulping tank, which also has a liquid inlet. The outlet of the pulping tank can be connected to the oxidation system of the PTA unit. Alternatively, the solid outlet of the washing and filtering integrated machine II can be mixed with liquid through a pipeline mixer and brought back to the oxidation system of the PTA unit. The liquid outlet of the washing and filtering integrated machine II can be connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter removal device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device.

98. The processing system according to claim 3, characterized in that, The solid outlet of the filter device I, the solid outlet of the integrated cooling filter, the solid outlet of the filter device II, the solid outlet of the filter device III, or the solid outlet of the integrated washing filter I are first connected to the inlet of the washing tank V. The washing tank V is also provided with a washing liquid inlet. The outlet of the washing tank V is connected to the inlet of the solid-liquid separator V, and the solid outlet of the solid-liquid separator V collects the solids. The liquid outlet of the solid-liquid separator V is connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter elimination device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device.

99. The processing system according to claim 95, characterized in that, The solid outlets of the filtration device I, the cooling filtration unit, the filtration device II, the filtration device III, the washing filtration unit I, or the dryer II are first connected to the inlet of the washing tank V. The washing tank V also has a washing liquid inlet. The outlet of the washing tank V is connected to the inlet of the solid-liquid separator V, and the solid outlet of the solid-liquid separator V collects the solids. The liquid outlet of the solid-liquid separator V is connected to the inlet of the phthalic acid extraction device, the inlet of the organic matter elimination device, the inlet of the mixer I, or the inlet of the cobalt-manganese adsorption device.

100. The processing system according to claim 3, characterized in that, Oxidizing devices are provided between the liquid outlet of the benzoic acid extraction device and the organic matter elimination device, between the liquid outlet of the benzoic acid extraction device and the inlet of the mixer I, or between the liquid outlet of the benzoic acid extraction device and the inlet of the cobalt-manganese adsorption device.

101. The processing system according to claim 1, 2, 97, 98 or 99, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the mixer I.

102. The processing system according to claim 96, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the mixer I.

103. The processing system according to claims 1, 2, 4, 5, 6, 7, 8, 9, 16, 17, 38, 39, 40, 97 or 99, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

104. The processing system according to claim 3, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

105. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

106. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

107. The processing system according to claim 15, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

108. The processing system according to claim 37, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

109. The processing system according to claim 96, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the cobalt-manganese adsorption device, or between the outlet of the cobalt-manganese adsorption device and the organic matter removal device.

110. The processing system according to claim 1, 4, 5, 6, 7, 8, 9, 16, 17, 24, 25 or 26, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the organic matter removal device.

111. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the organic matter removal device.

112. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the organic matter removal device.

113. The processing system according to claim 15, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the organic matter removal device.

114. The processing system according to claim 23, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the organic matter removal device.

115. The processing system according to claim 4, 5, 6, 13, 49, 50, 69 or 70, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the nanofiltration system I.

116. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the nanofiltration system I.

117. The processing system according to claim 12, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the nanofiltration system I.

118. The processing system according to claim 48, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the nanofiltration system I.

119. The processing system according to claim 68, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the nanofiltration system I.

120. The processing system according to claim 4, 5, 6 or 34, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the nanofiltration system I.

121. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the nanofiltration system I.

122. The processing system according to claim 33, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the nanofiltration system I.

123. The processing system according to claim 4, 5, 6 or 20, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the inlet of the nanofiltration system I.

124. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the inlet of the nanofiltration system I.

125. The processing system according to claim 19, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the inlet of the nanofiltration system I.

126. The processing system according to claim 7, 8, 9 or 54, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the heating evaporation device I.

127. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the heating evaporation device I.

128. The processing system according to claim 53, characterized in that, An oxidizing agent removal device is installed between the outlet of the organic matter removal device and the inlet of the heating evaporation device I.

129. The processing system according to claim 7, 8, 9 or 43, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the heating evaporation device I.

130. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the heating evaporation device I.

131. The processing system according to claim 42, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the heating evaporation device I.

132. The processing system according to claim 7, 8, 9 or 28, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the heating evaporation device I.

133. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the heating evaporation device I.

134. The processing system according to claim 27, characterized in that, An oxidizing agent removal device is installed between the liquid outlet of the solid-liquid separator I and the heating evaporation device I.

135. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the connection point a.

136. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the connection point a.

137. The processing system according to claim 44 or 45, characterized in that, An oxidizing agent removal device is installed between the outlet of the cobalt-manganese adsorption device and the connection point a.

138. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the connection point a.

139. The processing system according to claim 11, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the connection point a.

140. The processing system according to claim 55 or 56, characterized in that, An oxidizing agent removal device is provided between the outlet of the organic matter removal device and the inlet of the connection point a.

141. The processing system according to claim 10, characterized in that, An oxidizing agent is installed between the liquid outlet of the solid-liquid separator I and the inlet of the connection point a.

142. The processing system according to claim 11, characterized in that, An oxidizing agent is installed between the liquid outlet of the solid-liquid separator I and the inlet of the connection point a.

143. The processing system according to claim 29 or 30, characterized in that, An oxidizing agent is installed between the liquid outlet of the solid-liquid separator I and the inlet of the connection point a.

144. The processing system according to claim 10, characterized in that, An oxidizing agent removal device is installed between connection point a and the inlet of nanofiltration system I.

145. The processing system according to claim 15, characterized in that, An oxidizing agent removal device is installed between the connection point e and the inlet of the organic matter removal device.

146. The processing system according to claim 16 or 17, characterized in that, An oxidizing agent removal device is installed between the connection point e and the inlet of the organic matter removal device.

147. The processing system according to claim 15, characterized in that, An oxidizing agent removal device is installed between connection point e and the inlet of decarbonization tower I.

148. The processing system according to claim 16 or 17, characterized in that, An oxidizing agent removal device is installed between connection point e and the inlet of decarbonization tower I.

149. The processing system according to claim 1, characterized in that, The heating crystallizer I is a thin-film evaporator.

150. The processing system according to claim 18, characterized in that, The concentrate outlet of the nanofiltration system II is connected to the connection point c.

151. The processing system according to claim 7, 8 or 9, characterized in that, The concentrate outlet of the nanofiltration system II is connected to the inlet of the heating and evaporation equipment I.

152. The processing system according to claim 1, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank, and the outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the mixer I.

153. The processing system according to claim 7, 8 or 9, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank. The outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the heating evaporation equipment I.

154. The processing system according to claim 1, 4, 5, 6, 7, 8, 9, 13, 75, 76, 77, 84 or 85, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank, and the outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the organic matter removal equipment.

155. The processing system according to claim 12, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank, and the outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the organic matter removal equipment.

156. The processing system according to claim 14, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank, and the outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the organic matter removal equipment.

157. The processing system according to claim 83, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank, and the outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the organic matter removal equipment.

158. The system according to claim 12, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a saline tank, and the outlet of the saline tank of the bipolar membrane electrodialysis equipment is connected to the connection point b.

159. The system according to claim 13, 75, 76, 77, 80, 81 or 82, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a saline tank, and the outlet of the saline tank of the bipolar membrane electrodialysis equipment is connected to the connection point b.

160. The processing system according to claim 14, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a saline tank, and the outlet of the saline tank of the bipolar membrane electrodialysis equipment is connected to the connection point b.

161. The processing system according to claim 4, 5, 6, 13 or 65, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a saline tank. The outlet of the saline tank of the bipolar membrane electrodialysis equipment is connected to the inlet of nanofiltration system I.

162. The processing system according to claim 12, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a saline tank. The outlet of the saline tank of the bipolar membrane electrodialysis equipment is connected to the inlet of nanofiltration system I.

163. The processing system according to claim 64, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a saline tank. The outlet of the saline tank of the bipolar membrane electrodialysis equipment is connected to the inlet of nanofiltration system I.

164. The system according to claim 65, 73, 75, 76, 77, 80, 81, 82, 84 or 85, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank. The outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the concentration system III.

165. The processing system according to claim 64, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank. The outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the concentration system III.

166. The processing system according to claim 71, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank. The brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the concentration system III.

167. The processing system according to claim 72, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank. The outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the concentration system III.

168. The processing system according to claim 83, characterized in that, The bipolar membrane electrodialysis equipment is equipped with an acid production tank, an alkali production tank, and / or a brine tank. The outlet of the brine tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the concentration system III.

169. The processing system according to claim 87, 88, 89, 90, 91 or 92, characterized in that, The liquid outlet of the water absorption acid generator is also equipped with a heater, or the liquid outlet of the water absorption acid generator is connected to the inlet of the evaporator, the evaporator is equipped with a heater, and the gas phase outlet of the evaporator is connected to the collection tank or the water absorption acid generator; or the liquid outlet of the water absorption acid generator is connected to the inlet of the evaporator, the evaporator is equipped with a heater and a dosing port, and the gas phase outlet of the evaporator is connected to the collection tank or the water absorption acid generator.

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