CN219341816U - System for treating acid wastewater by active coke analysis gas - Google Patents
System for treating acid wastewater by active coke analysis gas Download PDFInfo
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- CN219341816U CN219341816U CN202320065176.XU CN202320065176U CN219341816U CN 219341816 U CN219341816 U CN 219341816U CN 202320065176 U CN202320065176 U CN 202320065176U CN 219341816 U CN219341816 U CN 219341816U
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Abstract
The utility model relates to the technical field of industrial wastewater treatment, in particular to an acid wastewater treatment system for an active coke analysis gas system. Including concentrating system, drying system, heat recovery and useless ammonia recycling system, concentrating system includes concentration tower and at least one plate heat exchanger, plate heat exchanger is connected with concentration tower, drying system is including the high-speed centrifugal atomizer that connects gradually, drying tower and first flue gas processing unit, high-speed centrifugal atomizer is connected with concentration tower, heat recovery and useless ammonia recycling system includes phase change heat exchanger and second flue gas processing unit, phase change heat exchanger's both ends are connected with high temperature flue gas and second flue gas processing unit, phase change heat exchanger still is connected with plate heat exchanger. The system utilizes low-grade heat in sintering (pellet) flue gas to carry out decrement concentration on the wastewater, adopts a drying and spraying method to recycle byproducts in the concentrated wastewater, realizes zero emission of dilute acid wastewater, and fundamentally solves the pollution problem of dilute acid wastewater.
Description
Technical Field
The utility model relates to the technical field of industrial wastewater treatment, in particular to an acid wastewater treatment system for an active coke analysis gas system.
Background
The sintering (pellet) flue gas is led into an adsorption tower by a booster fan, purified in the adsorption tower and then enters a chimney for emission. Active coke is added from the top of the absorption tower and moves downwards under the action of gravity and a tower bottom discharging device. Active coke absorption SO 2 、NO x The pollutants such as heavy metals and the like are sent to an analysis tower through a conveying device, and sulfur-rich active coke is analyzed to obtain high-concentration SO at high temperature 2 The gas is used for preparing concentrated sulfuric acid.
High concentration SO 2 The resolved gas passes through an acid preparation pretreatment working section and generates a certain amount of dilute acid wastewater. The wastewater has complex components and contains anions (Cl) - 、F - 、SO 4 2- ) Ammonia Nitrogen (NH) 4+ ) Heavy metals (Hg, fe, pb) and suspended substances, and has strong acidity, high salt content, high hardness,Easy scaling and the like.
At present, most dilute acid wastewater treatment methods adopt liquid alkali for neutralization, and then the dilute acid wastewater is sent to blast furnace slag flushing or enters a sintering wastewater pool for recycling, so that the problem of wastewater pollution can not be fundamentally solved. Part of steel plants consider newly creating a set of mature wastewater treatment systems, such as a stripping deamination method, a gaseous membrane method evaporation, a low-temperature multi-effect evaporation (or MVR evaporation) and the like, and the methods have the advantages of complex systems, high failure rate, high treatment cost and high consumption of a large amount of heat energy or electric energy. Therefore, in order to fundamentally solve the pollution problem of dilute acid wastewater, it is necessary to design an efficient and energy-saving active coke analysis gas system acid wastewater treatment system.
Disclosure of Invention
In order to solve the problems, the utility model provides an acid wastewater treatment system for preparing an acid by using active coke resolving gas, which comprises a concentration system, a drying system and a heat energy recovery and waste ammonia recycling system, wherein the concentration system comprises a concentration tower and at least one plate heat exchanger, the plate heat exchanger is connected with the concentration tower and is used for heating wastewater in the concentration tower, the drying system comprises a high-speed centrifugal atomizer, a drying tower and a first smoke treatment unit, the high-speed centrifugal atomizer is connected with a discharge end of the concentration tower, the drying tower is connected with a discharge end of the high-speed centrifugal atomizer, the drying tower comprises a smoke inlet and a smoke outlet, the smoke outlet of the drying tower is connected with the first smoke treatment unit, the heat energy recovery and waste ammonia recycling system comprises a phase change heat exchanger and a second smoke treatment unit, an air inlet end of the phase change heat exchanger is connected with high-temperature smoke, an air outlet end of the phase change heat exchanger is connected with the second smoke treatment unit, and an air outlet end of the first smoke treatment unit is connected with the second smoke treatment unit.
Further, the concentration tower comprises an air inlet and an air outlet, air enters the concentration tower from the air inlet and is output from the air outlet of the concentration tower after reversely exchanging heat with sprayed wastewater, and the air outlet of the concentration tower is connected with the second flue gas treatment unit.
Further, the number of the plate heat exchangers is two, the two plate heat exchangers are connected with the lower end part of the concentration tower, and the two plate heat exchangers are used for heating wastewater and then enabling the wastewater to enter the concentration tower through an atomization spraying layer at the upper end part of the concentration tower.
Further, the plate heat exchanger heats the wastewater flowing through the concentration tower to 75-80 ℃.
Further, the drying system further comprises a concentrated wastewater buffer tank, and the concentrated wastewater buffer tank is arranged between the concentration tower and the high-speed centrifugal atomizer.
Further, a flue gas inlet of the drying tower is communicated with waste heat flue gas.
Further, the first flue gas treatment unit comprises a cyclone separator, a bag-type dust collector and a draught fan which are sequentially arranged along the flue gas flowing direction, and the air inlet end of the cyclone separator is connected with the flue gas outlet of the drying tower.
Further, the phase change heat exchanger comprises a phase change heat exchanger heating section and a phase change heat exchanger condensing section, high-temperature flue gas flows through the phase change heat exchanger heating section, enters the second flue gas treatment unit after being cooled, one side of the phase change heat exchanger condensing section is connected with the phase change heat exchanger heating section, and the other side of the phase change heat exchanger condensing section is connected with the plate heat exchanger.
Further, the second flue gas treatment unit comprises a desulfurizing tower, a denitration tower and a chimney which are sequentially arranged along the flue gas flowing direction, the desulfurizing tower is connected with the air outlet end of the phase change heat exchanger, and the air inlet end of the denitration tower is also connected with the air outlet end of the first flue gas treatment unit.
Further, the second flue gas treatment unit further comprises a booster fan, and the booster fan is arranged between the phase change heat exchanger and the desulfurizing tower.
Compared with the prior art, the utility model has the following beneficial effects due to the adoption of the technical scheme:
1) According to the acid wastewater treatment system for the active coke analysis gas system, provided by the utility model, in the wastewater concentration stage, air is used as a carrier to carry out wastewater evaporation concentration, heated wastewater is uniformly sprayed into the concentration tower through the atomization spraying layer, low-temperature saturated wet air enters the concentration tower to carry out reverse uniform mass transfer heat exchange with the wastewater, and evaporation water is carried by the air, so that the air is discharged in a high-temperature saturated state, the operation is simple, the equipment arrangement is flexible, the occupied area is small, the investment can be effectively reduced, and the power consumption for ton water operation is lower;
2) According to the acid wastewater treatment system for the active coke desorption gas provided by the utility model, the gas inlet end of the phase change heat exchanger can adopt sintering (pellet) flue gas, low-grade heat in the flue gas is recovered for heating wastewater, no additional auxiliary energy source is needed, the energy consumption is reduced, and a large amount of energy sources are saved;
3) The utility model provides an acid wastewater treatment system for an active coke desorption gas, waste heat flue gas is introduced into a drying tower, the waste heat flue gas is in reverse contact heat exchange with concentrated wastewater in the drying tower, the concentrated wastewater is sufficiently dried and crystallized to generate industrial salt or anhydrous CaCl 2 The first flue gas treatment unit can further recover crystallization products in the flue gas to finish zero wastewater discharge;
4) According to the acid wastewater treatment system for the active coke desorption gas provided by the utility model, the first flue gas treatment unit is connected with the second flue gas treatment unit, and the ammonia-containing waste gas discharged from the drying tower enters the denitration tower after being treated by the first flue gas treatment unit, so that secondary atmospheric pollution is not generated, and the ammonia water consumption of the denitration system can be saved.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present utility model, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of the structure of the acid wastewater treatment system with active coke analysis gas system.
1-a first plate heat exchanger; 2-a second plate heat exchanger; 3-concentrating tower; 4-a centrifuge; 5-a waste water buffer tank; 6-concentrating the wastewater cache tank; 7-a high-speed centrifugal atomizer; 8-a drying tower; 9-cyclone separator; 10-a bag-type dust remover; 11-induced draft fan; 12-a heating section of the phase-change heat exchanger; 13-a condensing section of the phase-change heat exchanger; 14-a booster fan; 15-a desulfurizing tower; 16-a denitration tower; 17-chimney.
Detailed Description
The technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are only some embodiments of the present utility model, but not all embodiments, and all other embodiments obtained by those skilled in the art without making creative efforts based on the embodiments of the present utility model are included in the protection scope of the present utility model. In the drawings, the size and relative sizes of certain parts may be exaggerated for clarity.
In the description of the present utility model, unless explicitly stated and limited otherwise, the terms "connected" and "coupled" should be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; the terms may be used in any form, such as directly or indirectly through an intermediate medium, or may be used in any form of communication between two elements or in any form of interaction between two elements, and the terms are specifically understood by those of ordinary skill in the art.
In the description of the present utility model, the terms "upper", "lower", "left", "right", "front", "rear", "center", "horizontal", "vertical", "top", "bottom", "inner", "outer", and the like are orientation or positional relationships based on those shown in the drawings, merely for convenience of description and simplicity of operation, and do not indicate or imply that the apparatus or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
Furthermore, in the description of the present utility model, the terms "first," "second," and the like, are used merely for distinguishing between descriptions and not necessarily for indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Furthermore, features defining "first", "second" may include one or more such features, either explicitly or implicitly.
As shown in an attached drawing 1 of the specification, the utility model provides an acid wastewater treatment system for preparing an acid by analyzing gas by active coke, which comprises a concentration system, a drying system and a heat energy recovery and waste ammonia recycling system, wherein the concentration system comprises a concentration tower 3 and at least one plate heat exchanger, the plate heat exchanger is arranged outside the concentration tower 3 and is connected with the concentration tower 3 for heating wastewater in the concentration tower 3, the drying system comprises a high-speed centrifugal atomizer 7, a drying tower 8 and a first smoke treatment unit, the high-speed centrifugal atomizer 7 is connected with a discharge end of the concentration tower 3, the drying tower 8 is connected with a discharge end of the high-speed centrifugal atomizer 7, concentrated wastewater after concentration treatment by the concentration tower 3 enters the high-speed centrifugal atomizer 7 for atomization and enters the drying tower 8 for drying, a heating device is arranged in the drying tower 8 for heating the atomized concentrated wastewater, the heating medium may be gas or liquid, in this embodiment, high temperature waste heat flue gas is used to dry the concentrated waste water, where the waste heat flue gas comes from flue gas exhausted from the previous working section, heat energy can be fully recycled, the temperature of the waste heat flue gas is 300-350 ℃, the drying tower 8 includes a flue gas inlet and a flue gas outlet, the waste heat flue gas enters the concentrated waste water in the drying tower 8 from the flue gas inlet and is exhausted from the flue gas outlet after reversely contacting with the concentrated waste water in the drying tower 8, most of generated crystals are exhausted from the bottom of the drying tower 8 after the concentrated waste water is fully dried, the flue gas outlet of the drying tower 8 is connected with the first flue gas treatment unit for purifying the exhausted waste heat flue gas containing crystals, the heat energy recovery and waste ammonia gas recycling system includes a phase change heat exchanger and a second flue gas treatment unit, the air inlet end of the phase change heat exchanger is connected with the high temperature flue gas, the gas outlet end is connected with the second flue gas treatment unit, the phase change heat exchanger is also connected with the plate heat exchanger, and the gas outlet end of the first flue gas treatment unit is connected with the second flue gas treatment unit.
In the embodiment, the number of the plate heat exchangers is two, namely a first plate heat exchanger 1 and a second plate heat exchanger 2, the two plate heat exchangers are connected with the lower end part of the concentration tower 3 and are used for heating wastewater, then the wastewater enters the concentration tower 3 from an atomization spray layer at the upper end part of the concentration tower 3, specifically, a circulating pump is arranged between the concentration tower 3 and the plate heat exchangers, the wastewater at the lower end part of the concentration tower 3 is pressurized by the circulating pump and then enters the plate heat exchangers for heating, then the wastewater is sprayed in the concentration tower from the upper part to the lower part by an atomization spray layer at the upper end part of the concentration tower 3, two atomization spray layers are arranged in the concentration tower 3, the first plate heat exchanger 1 heats the wastewater at the bottom of the concentration tower 3 to 75-80 ℃ by the circulating pump, then enters the tower by the first atomization spray layer of the concentration tower 3, and the second plate heat exchanger 2 heats the wastewater at the bottom of the concentration tower 3 to 75-80 ℃ by the circulating pump and enters the second atomization spray layer of the concentration tower 3; of course, the number of plate type circulation pumps and the spraying positions can be set according to actual needs, and the embodiment is not limited.
In an optimized implementation manner, the concentration tower 3 comprises an air inlet and an air outlet, the concentration tower 3 is connected with a centrifugal machine 4, the centrifugal machine 4 guides ambient air into the concentration tower 3 from the air inlet and outputs the ambient air from the air outlet of the concentration tower 3 after reverse uniform mass transfer and heat exchange with sprayed wastewater, specifically, the centrifugal machine 4 is connected to the lower end part of the concentration tower 3, the air enters the concentration tower 3 from the lower end part of the concentration tower 3 and is output from the upper end part of the concentration tower 3 after reverse mass transfer and heat exchange with wastewater, the air and atomized heating wastewater reversely transfer and exchange with each other, evaporated water is carried by the air, the wastewater is gradually concentrated into concentrated wastewater in continuous circulation heating, the concentrated wastewater enters the next stage of drying treatment process, the air becomes a high-temperature saturated state, the gas coming out of the concentration tower 3 is ammonia-containing waste gas, and the air outlet of the concentration tower 3 is connected with the second flue gas treatment unit, and the ammonia-containing waste gas is discharged after being treated by the second flue gas treatment unit to reach standards.
In an optimized embodiment, the concentration tower 3 is also connected with a waste water buffer tank 5, and the waste water buffer tank 5 is used for storing clear liquid waste water pretreated by the acid making system and is pumped into the concentration tower 3 through a feeding pump; of course, the waste water of the acid making system can be directly sent into the concentration tower 3, and the waste water buffer tank 5 can be arranged according to actual requirements.
In an optimized embodiment, the drying system further comprises a concentrated wastewater buffer tank 6, the concentrated wastewater buffer tank 6 is arranged between the concentrating tower 3 and the high-speed centrifugal atomizer 7, specifically, concentrated wastewater in the concentrating tower 3 automatically flows into the concentrated wastewater buffer tank 6, enters the high-speed centrifugal atomizer 7 through a feeding pump, and atomized concentrated wastewater enters the drying tower 8.
In a refinement mode, the drying tower 8 heats and dries the concentrated wastewater through high-temperature flue gas, a flue gas inlet of the drying tower 8 is communicated with waste heat flue gas, the waste heat flue gas is from waste heat flue gas recovered in the previous process, the energy of the waste heat flue gas can be recycled, the temperature of the waste heat flue gas is 300-350 ℃, the concentrated wastewater enters from the upper end part of the drying tower 8, the waste heat flue gas enters from the lower end part of the drying tower, the upper end part of the waste heat flue gas is discharged, the concentrated wastewater and the waste heat flue gas are in countercurrent contact in the drying tower 8, after full drying, the produced crystals are discharged from the bottom of the drying tower 8, and the crystals are mainly industrial salt or anhydrous CaCl 2 The flue gas outlet of the drying tower 8 is connected with a first flue gas treatment system, and further purifies the flue gas exhausted from the drying tower 8.
According to a refinement embodiment, the first flue gas treatment unit comprises a cyclone separator 9, a cloth bag dust collector 10 and an induced draft fan 11 which are sequentially arranged along the flue gas flowing direction, the air inlet end of the cyclone separator 9 is connected with a flue gas outlet of the drying tower 8, most crystals carried in waste heat flue gas can be removed by the cyclone separator 9, collected crystals are discharged from the bottom of the cyclone separator 9, the waste heat flue gas enters the cloth bag dust collector 10 after passing through the cyclone separator 9, crystals in the waste heat flue gas are further removed, the crystals can be recovered, waste heat flue gas discharged from the drying tower 8 contains ammonia, and the induced draft fan 11 guides the waste heat flue gas into a second flue gas treatment system to be recycled.
In an optimized embodiment, the phase-change heat exchanger comprises a phase-change heat exchanger heating section 12 and a phase-change heat exchanger condensing section 13, high-temperature flue gas flows through the phase-change heat exchanger heating section 12 and enters the second flue gas treatment unit after being cooled, the high-temperature flue gas can be from sintering (pellet) flue gas, heat of the high-temperature flue gas is recovered, one side of the phase-change heat exchanger condensing section 13 is connected with the phase-change heat exchanger heating section 12 through a pipeline, the other side of the phase-change heat exchanger condensing section 13 is connected with the first plate heat exchanger 1 and the second plate heat exchanger 2 through pipelines, and the phase-change heat exchanger is used for heating wastewater flowing through the plate heat exchanger, so that heat of sintering (pellet) flue gas can be recycled, energy consumption is saved, and cost is reduced.
In an optimized embodiment, the second flue gas treatment unit comprises a desulfurizing tower 15, a denitrating tower 16 and a chimney 17 which are sequentially arranged along the flue gas flowing direction, a booster fan 14 is further arranged between the phase-change heat exchanger heating section 12 and the desulfurizing tower 15, the desulfurizing tower 15 is connected with the air outlet end of the phase-change heat exchanger heating section 12, the induced draft fan 11 guides waste heat flue gas to the inlet flue of the denitrating tower 16, the sintered (pellet) flue gas is subjected to low-grade heat recovery through the phase-change heat exchanger, the circulating waste water is heated through the first plate heat exchanger 1 and the second plate heat exchanger 2, the cooled flue gas is pressurized by the booster fan 14, sequentially enters the desulfurizing tower 15 and the denitrating tower 16 for purification treatment, and is emptied through the chimney after reaching the emission standard, preferably, the ammonia-containing waste gas discharged by the concentrating tower 3 is also guided to the inlet flue of the denitrating tower 16, ammonia in the denitrating tower 16 can be fully recycled, and the ammonia consumption in the denitrating tower 16 is saved.
And all that is not described in detail in this specification is well known to those skilled in the art.
In the application, the wastewater adopts a wastewater evaporation concentration method using an air source as a carrier in a concentration stage, heated wastewater is uniformly sprayed into a concentration tower through multilayer atomization spraying, low-temperature saturated wet air enters the concentration tower to exchange heat with reverse uniform mass transfer of the wastewater, and simultaneously evaporated water is carried by the air, and the air is changed into a high-temperature saturated state.
In the application, in the heat energy recovery and waste ammonia gas recycling stage, the phase change heat exchanger is adopted to recover low-grade heat energy in sintering (pellet) flue gas for heating circulating wastewater, so that a large amount of external heat sources can be saved, the safety of the desulfurizing tower can be ensured, the phase change temperature of working medium in the phase change heat exchanger is preferably 105-110 ℃, and acid corrosion in the flue gas is avoided.
In the application, in the drying stage, the drying tower and the first flue gas treatment system can recover industrial salt crystallized in the wastewater or anhydrous CaCl 2 Zero discharge of wastewater is completed; the ammonia-containing waste gas exhausted from the concentration tower and the drying tower is led into the denitration tower, so that secondary atmospheric pollution is not generated, ammonia in the denitration tower can be recycled, the ammonia water consumption of the denitration tower is saved, and the cost is saved while the environment is protected.
It will be appreciated by those skilled in the art that the utility model can be embodied in many other specific forms without departing from the spirit or scope of the utility model. Although an embodiment of the present utility model has been described, it is to be understood that the utility model is not limited to this embodiment, and that variations and modifications may be effected by one skilled in the art within the spirit and scope of the utility model as defined in the appended claims.
Claims (10)
1. The utility model provides an active burnt desorption gas system acid wastewater treatment system, its characterized in that, includes concentrating system, drying system, heat recovery and useless ammonia recycling system, concentrating system includes concentrating tower and at least one plate heat exchanger, plate heat exchanger with concentrating tower is connected and is used for heating waste water in the concentrating tower, drying system includes high-speed centrifugal atomizer, drying tower and first flue gas processing unit, high-speed centrifugal atomizer with concentrating tower's discharge end is connected, the drying tower with high-speed centrifugal atomizer's discharge end is connected, the drying tower includes flue gas import and flue gas export, drying tower's flue gas export is connected with first flue gas processing unit, heat recovery and useless ammonia recycling system includes phase change heat exchanger and second flue gas processing unit, phase change heat exchanger's inlet end is connected with high temperature flue gas, the outlet end is connected with second flue gas processing unit, phase change heat exchanger still with plate heat exchanger is connected, first flue gas processing unit's outlet end with second flue gas processing unit is connected.
2. The acid wastewater treatment system for activated coke and resolving gas according to claim 1, wherein the concentration tower comprises an air inlet and an air outlet, air enters the concentration tower from the air inlet and is output from the air outlet of the concentration tower after reversely exchanging heat with sprayed wastewater, and the air outlet of the concentration tower is connected with the second flue gas treatment unit.
3. The acid wastewater treatment system for preparing active coke analysis gas according to claim 2, wherein the number of the plate heat exchangers is two, and the two plate heat exchangers are connected with the lower end part of the concentration tower and used for heating the wastewater and then entering the concentration tower from an atomization spraying layer at the upper end part of the concentration tower.
4. The system for treating acid wastewater from activated coke resolution gas production according to claim 1, wherein the plate heat exchanger heats the wastewater flowing through the concentration tower to 75-80 ℃.
5. The activated coke resolution gas to acid wastewater treatment system of claim 1, wherein the drying system further comprises a concentrated wastewater buffer tank disposed between the concentration tower and the high-speed centrifugal atomizer.
6. The acid wastewater treatment system of activated coke resolving gas system according to claim 1, wherein the flue gas inlet of the drying tower is in communication with waste heat flue gas.
7. The acid wastewater treatment system of activated coke analysis gas system according to claim 1, wherein the first flue gas treatment unit comprises a cyclone separator, a bag-type dust collector and an induced draft fan which are sequentially arranged along the flow direction of flue gas, and the air inlet end of the cyclone separator is connected with the flue gas outlet of the drying tower.
8. The acid wastewater treatment system of the active coke analysis gas system according to claim 1, wherein the phase change heat exchanger comprises a phase change heat exchanger heating section and a phase change heat exchanger condensing section, high-temperature flue gas flows through the phase change heat exchanger heating section to enter the second flue gas treatment unit after being cooled, one side of the phase change heat exchanger condensing section is connected with the phase change heat exchanger heating section, and the other side of the phase change heat exchanger condensing section is connected with the plate heat exchanger.
9. The acid wastewater treatment system of activated coke analysis gas system according to claim 1, wherein the second flue gas treatment unit comprises a desulfurizing tower, a denitrating tower and a chimney which are sequentially arranged along the flue gas flowing direction, the desulfurizing tower is connected with the air outlet end of the phase change heat exchanger, and the air inlet end of the denitrating tower is also connected with the air outlet end of the first flue gas treatment unit.
10. The activated coke resolution gas system acid wastewater treatment system according to claim 9, wherein the second flue gas treatment unit further comprises a booster fan disposed between the phase change heat exchanger and the desulfurization tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320065176.XU CN219341816U (en) | 2023-01-10 | 2023-01-10 | System for treating acid wastewater by active coke analysis gas |
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| CN202320065176.XU CN219341816U (en) | 2023-01-10 | 2023-01-10 | System for treating acid wastewater by active coke analysis gas |
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