CN218879677U - High-concentration salt wastewater treatment device - Google Patents
High-concentration salt wastewater treatment device Download PDFInfo
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- CN218879677U CN218879677U CN202320112708.0U CN202320112708U CN218879677U CN 218879677 U CN218879677 U CN 218879677U CN 202320112708 U CN202320112708 U CN 202320112708U CN 218879677 U CN218879677 U CN 218879677U
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Abstract
The utility model provides a processing apparatus of high enriched salt waste water, include: the efficient reaction system comprises a first-stage reaction tank, a second-stage reaction tank and a third-stage reaction tank, wherein the second-stage reaction tank is respectively communicated with the first-stage reaction tank and the third-stage reaction tank, the first-stage reaction tank can sterilize the wastewater, the second-stage reaction tank can remove fluorine ions in the wastewater, and the third-stage reaction tank can remove silicon dioxide in the wastewater; the circulating system comprises a circulating sedimentation tank which is communicated with the third-stage reaction tank and can remove part of sludge in the wastewater treated by the third-stage reaction tank; and the tubular microfiltration system is communicated with the circulating sedimentation tank and can filter the wastewater treated by the circulating sedimentation tank so as to separate the sludge mixed liquid from the water solution. The technical scheme of the utility model fluoride ion and silica in the high enriched salt waste water can effectively be got rid of to promote the later stage recycle of high enriched salt waste water.
Description
Technical Field
The utility model relates to a high enriched brine processing technology field, in particular to processing apparatus of high enriched brine waste water.
Background
The coking wastewater has complex components, high organic matter content and high polycyclic aromatic hydrocarbon and macromolecular matter content, and even after biochemical treatment, long-chain and persistent organic matters in the coking wastewater reach the discharge standard and still possibly cause harm to the environment. The conventional coking wastewater is subjected to biochemical treatment and physicochemical treatment, and the physicochemical effluent is discharged or recycled after advanced treatment.
The treatment of high-concentration brine is a key technology for restricting zero discharge of coal chemical wastewater.
In general, a wastewater advanced treatment or wastewater zero discharge device adopts resin softening, a membrane concentration technology, a nano-filtration salt separation or Electrodialysis (ED) concentration technology and an evaporation crystallization technology to further and deeply treat wastewater, so as to obtain sodium sulfate and sodium chloride industrial salt.
The concentration of fluoride ions in raw water in the coking wastewater is high, the content is 70 mg/L-90 mg/L, and after reverse osmosis and high-pressure reverse osmosis treatment, the water quality in high-concentration salt water is as follows: the Total Dissolved Solids (TDS) is 40000mg/L to 95000mg/L, and the concentration of the fluorinion is 120mg/L to 270mg/L.
The chloride content of the sintering acid-making wastewater is 45000 mg/L-60000 mg/L, the sulfate is 20000 mg/L-30000 mg/L, the soluble silicon dioxide is 100 mg/L-130 mg/L, the fluoride content is 600 mg/L-800 mg/L, and the TDS is 110000 mg/L-120000 mg/L.
After high-concentration coking wastewater or acid-making wastewater is treated by a membrane concentration separation technology, pollution factors are concentrated, the content of silicon dioxide is 300-500 mg/L, the concentration of fluoride is 550-850 mg/L, and high-concentration fluorine-containing silicon-containing wastewater enters a subsequent concentration and crystallization device to easily cause scaling of the concentration device and corrosion of equipment, so that the equipment is damaged.
The treatment mode of high concentration salt-containing concentrated water is from selecting electrodialysis treatment technology to evaporating crystallization device, and in the electrodialysis concentration treatment process, the residual calcium ions in the concentrated brine can react with fluoride ions to generate calcium fluoride precipitate, so that scaling fouling of an electrodialysis membrane is caused, and meanwhile, the fluoride ions can penetrate through a negative membrane and a positive membrane in the electrodialysis membrane and enter polar water. Because the common stainless steel material is not resistant to the corrosion of the high-salt-content wastewater, the electrode plates for electrodialysis are made of titanium alloy materials, and the corrosion of the electrodes for electrodialysis is easily caused when fluorine ions enter into polar water, so that the service life of the electrodes is shortened and the performance of equipment is influenced. The high-silicon dioxide salt-containing wastewater can be directly adhered to the electrodialysis membrane, and the silicon dioxide is uncharged, so that ionization concentration of the electrodialysis membrane is influenced, and pollution and blockage of an electrodialysis membrane system are caused.
In the zero discharge system of high concentration salt water, mechanical Vapor Recompression (MVR) evaporation crystallization technology is usually used, because the material that evaporation system heat exchanger, evaporation crystallization separator used is the titanium alloy, when high concentration fluorine-containing, siliceous strong brine gets into sodium chloride evaporation crystallizer in, silica can directly adsorb and cause the heat exchanger to block up in the heat exchanger, make evaporation system can not normal heat exchange and crystallization salt extraction, simultaneously, high concentration fluorine ion strong brine can get into evaporation crystallizer's heat exchanger, evaporation crystallization separator, in the evaporation process, strong brine can separate and form partly hydrogen ion, hydrogen ion and fluorine-containing strong brine's fluorine ion reaction generate hydrogen fluoride, hydrogen fluoride can preferentially adsorb and combine with titanium ion on the titanium surface and form soluble fluoride, make titanium take place the pitting corrosion, influence evaporation crystallizer life-span.
In the traditional process of treating fluorine-containing wastewater, lime or calcium chloride is added, calcium ions react with fluoride ions to generate calcium fluoride precipitate, so that the fluoride ions are removed through precipitation, but other ions in high-concentration salt water influence the solubility of the calcium fluoride, the concentration of the fluoride ions is higher when water is discharged, and the calcium ions are taken out, so that scaling phenomenon is easily caused to a subsequent system. The traditional desiliconization method mainly comprises flocculation desiliconization (common magnesium agent and lime), electric flocculation, ion exchange, reverse osmosis and the like, but the method has the problems of low desiliconization efficiency, large sludge amount, high operation cost and the like, thereby seriously influencing the normal operation of a subsequent system.
Therefore, how to effectively remove fluorine ions and silica in the high-concentration salt wastewater, thereby promoting the later recycling of the high-concentration salt wastewater is a problem which needs to be solved at present.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a processing apparatus of high enriched salt waste water can effectively get rid of fluoride ion and silica in the high enriched salt waste water to promote the later stage recycle of high enriched salt waste water.
In order to solve the technical problem, the utility model provides a processing apparatus of high enriched salt waste water, include:
the efficient reaction system comprises a first-stage reaction tank, a second-stage reaction tank and a third-stage reaction tank, wherein the second-stage reaction tank is respectively communicated with the first-stage reaction tank and the third-stage reaction tank, the first-stage reaction tank is used for sterilizing microorganisms in wastewater, the second-stage reaction tank is used for removing fluoride ions in the wastewater treated by the first-stage reaction tank, and the third-stage reaction tank is used for removing silicon dioxide in the wastewater treated by the second-stage reaction tank;
the circulating system comprises a circulating sedimentation tank, the circulating sedimentation tank is communicated with the third-stage reaction tank, and the circulating sedimentation tank is used for removing part of sludge in the wastewater treated by the third-stage reaction tank;
and the tubular microfiltration system is communicated with the circulating sedimentation tank and is used for filtering the wastewater treated by the circulating sedimentation tank so as to separate sludge mixed liquor from aqueous solution.
Preferably, stirrers are arranged in the first-stage reaction tank, the second-stage reaction tank and the third-stage reaction tank, and pH meters are arranged on the second-stage reaction tank and the third-stage reaction tank.
Preferably, the circulation system further comprises: the device comprises a mud scraper, a mud scraper rake, a circulating sedimentation tank liquid level meter, a flushing pipe, a mud pump, a mud pneumatic valve and a first connecting pipeline; the mud scraper is arranged inside the circulating sedimentation tank, and the mud scraper rake is connected with the mud scraper so as to stir the sludge in the circulating sedimentation tank through the mud scraper rake; the circulating sedimentation tank liquid level meter is arranged on the circulating sedimentation tank; the flushing pipe is arranged in the circulating sedimentation tank and is used for flushing sludge settled at the bottom of the sedimentation circulating tank; the first connecting pipeline is communicated with the bottom of the circulating sedimentation tank, and the sludge discharge pump and the sludge discharge pneumatic valve are arranged on the first connecting pipeline so as to discharge sludge precipitated at the bottom of the circulating sedimentation tank through the first connecting pipeline.
Preferably, the tubular microfiltration system comprises:
the device comprises a tubular microfiltration membrane device and a water production pool, wherein the water production pool is arranged below the tubular microfiltration membrane device and is communicated with the tubular microfiltration membrane device through a second connecting pipeline, the tubular microfiltration membrane device is used for filtering the wastewater treated by the circulating sedimentation tank, and the water production pool is used for collecting the aqueous solution.
Preferably, a water outlet of the tubular microfiltration membrane device is communicated with the top of the circulating sedimentation tank through a third connecting pipeline, so that the sludge mixed liquor enters the circulating sedimentation tank through the third connecting pipeline; and the water inlet of the tubular microfiltration membrane device is communicated with the bottom of the circulating sedimentation tank through a fourth connecting pipeline, so that the wastewater treated by the circulating sedimentation tank enters the tubular microfiltration membrane device through the fourth connecting pipeline.
Preferably, a flow meter and a water return pneumatic valve are arranged on the third connecting pipeline.
Preferably, a water inlet basket filter, a circulating pump and a water inlet pneumatic valve are arranged on the fourth connecting pipeline.
Preferably, a water production pool liquid level meter and a pH meter are arranged on the water production pool.
Compared with the prior art, the utility model provides a processing apparatus of high enriched salt waste water, include: the efficient reaction system comprises a first-stage reaction tank, a second-stage reaction tank and a third-stage reaction tank, wherein the second-stage reaction tank is respectively communicated with the first-stage reaction tank and the third-stage reaction tank, the first-stage reaction tank is used for sterilizing microorganisms in wastewater, the second-stage reaction tank is used for removing fluoride ions in the wastewater treated by the first-stage reaction tank, and the third-stage reaction tank is used for removing silicon dioxide in the wastewater treated by the second-stage reaction tank; the circulating system comprises a circulating sedimentation tank, the circulating sedimentation tank is communicated with the third-stage reaction tank, and the circulating sedimentation tank is used for removing part of sludge in the wastewater treated by the third-stage reaction tank; the tubular microfiltration system, the tubular microfiltration system with the circulation sedimentation tank is linked together, the tubular microfiltration system is used for filtering the waste water that the circulation sedimentation tank was handled for mud mixed liquor separates with the aqueous solution, can effectively get rid of the fluoride ion and the silica in the high enriched salt waste water, thereby promotes the later stage recycle of high enriched salt waste water.
Drawings
FIG. 1 is a schematic view of a high-salinity wastewater treatment apparatus according to an embodiment of the present invention;
FIG. 2 is a flow chart of a method for treating high salinity wastewater in accordance with an embodiment of the present invention;
fig. 3 is a graph of fluoride ion and silica removal rates at different phs in accordance with an embodiment of the present invention.
Wherein the reference numerals of figures 1-3 are as follows:
10-a stirrer; 11-a first-stage reaction tank; 12-a secondary reaction tank; 121-a first pH meter; 13-a third-stage reaction tank; 131-a second pH meter; 132-a water inlet pipe; 133-a stirring barrel; 134-water distribution device; 14-circulating a sedimentation tank; 141-mud scraper; 142-circulating sedimentation tank level gauge; 143-mud scraper rake; 144-a flush tube; 145-dredge pump; 146-mud discharge pneumatic valve; 147-a first connecting line; 15-a water producing pool; 151-third pH meter; 152-a pool level meter; 153-second connecting line; 16-tubular microfiltration membrane devices; 161-water inlet; 162-water outlet; 163-third connecting line; 164-a flow meter; 165-backwater pneumatic valve; 166-influent basket filter; 167-circulation pump; 168-fourth connecting line; 169-water pneumatic valve.
Detailed Description
In order to make the objects, advantages and features of the present invention clearer, the following will explain the present invention in further detail with reference to the accompanying drawings and specific embodiments. It should be noted that the drawings are in simplified form and are not to precise scale, and are provided for convenience and clarity in order to facilitate the description of the embodiments of the present invention. Further, the structures illustrated in the drawings are often part of actual structures. In particular, the drawings may have different emphasis points and may sometimes be scaled differently.
An embodiment of the utility model provides a processing apparatus of high salt waste water, include: the efficient reaction system comprises a first-stage reaction tank, a second-stage reaction tank and a third-stage reaction tank, wherein the second-stage reaction tank is respectively communicated with the first-stage reaction tank and the third-stage reaction tank, the first-stage reaction tank is used for sterilizing microorganisms in wastewater, the second-stage reaction tank is used for removing fluoride ions in the wastewater treated by the first-stage reaction tank, and the third-stage reaction tank is used for removing silicon dioxide in the wastewater treated by the second-stage reaction tank; the circulating system comprises a circulating sedimentation tank, the circulating sedimentation tank is communicated with the third-stage reaction tank, and the circulating sedimentation tank is used for removing part of sludge in the wastewater treated by the third-stage reaction tank; and the tubular microfiltration system is communicated with the circulating sedimentation tank and is used for filtering the wastewater treated by the circulating sedimentation tank, so that the sludge mixed liquid is separated from the water solution.
The treatment apparatus for high salinity wastewater provided in this embodiment will be described in detail with reference to fig. 1 and 3.
In order to realize zero discharge of the high-concentration salt wastewater, the high-concentration salt wastewater needs to be subjected to desalination technical treatment. The desalting treatment of the high-concentration brine wastewater mainly adopts a physical method, and the mature desalting technology mainly selects an electrodialysis treatment technology and an evaporation crystallization device. Before desalting treatment, fluoride ions and silicon dioxide in the high-salinity wastewater need to be removed, otherwise, residual fluoride ions and silicon dioxide in the high-salinity wastewater influence the performances of an electrodialysis membrane and an evaporative crystallization device, and therefore the desalting effect of the high-salinity wastewater is influenced.
Therefore, the treatment device for the high-concentration salt wastewater provided by the embodiment is used for removing fluorine ions and silicon dioxide in the high-concentration salt wastewater. The treatment device for the high-concentration salt wastewater comprises a high-efficiency reaction system, a circulating system and a tubular microfiltration system.
The high-efficiency reaction system comprises a first-stage reaction tank 11, a second-stage reaction tank 12 and a third-stage reaction tank 13. The secondary reaction tank 12 is respectively communicated with the primary reaction tank 11 and the tertiary reaction tank 13, the wastewater is firstly introduced into the primary reaction tank 11, and sodium hypochlorite is added into the primary reaction tank 11 to sterilize microorganisms in the wastewater; then, the wastewater treated by the primary reaction tank 11 enters the secondary reaction tank 12, and aluminum chloride is polymerized in the secondary reaction tank 12 by adding a high-efficiency fluorine removal agent, wherein a complexing effect exists between aluminum ions and fluorine ions, and aluminum hydroxide flocs generated by hydrolysis of the aluminum ions exchange, adsorb and sweep the fluorine ions, so that sodium hexafluoroaluminate, aluminum fluoride, sodium fluoride and the like are generated, and the fluorine ions in the wastewater are removed; then, the wastewater treated by the secondary reaction tank 12 enters the tertiary reaction tank 13, and sodium metaaluminate and polyferric sulfate are added into the tertiary reaction tank 13 to enable silica in the wastewater to react to generate precipitates, so that the silica in the wastewater is removed.
Preferably, the first-stage reaction tank 11, the second-stage reaction tank 12 and the third-stage reaction tank 13 are all provided with a stirrer 10, so that wastewater in the first-stage reaction tank 11, the second-stage reaction tank 12 and the third-stage reaction tank 13 is fully contacted with additives added into each reaction tank, the wastewater can be fully treated, and the wastewater treatment efficiency is improved.
Preferably, a first pH meter 121 is disposed on the second-stage reaction tank 12, a second pH meter 131 is disposed on the third-stage reaction tank 13, and the first pH meter 121 and the second pH meter 131 can timely feed back pH conditions of wastewater in the second-stage reaction tank 12 and the third-stage reaction tank 13, and automatically track and adjust pH of wastewater in the second-stage reaction tank 12 and the third-stage reaction tank 13 by automatically adding hydrochloric acid and sodium hydroxide according to actually required pH conditions of wastewater in the second-stage reaction tank 12 and the third-stage reaction tank 13.
According to FIG. 3, the removal rate of fluoride ions and silica was changed at different pH. In fig. 3, a curve L1 is a removal rate of silica, a curve L2 is a removal rate of fluoride ions, an abscissa is a magnitude of pH of wastewater, and an ordinate is a removal rate of fluoride ions and silica under a condition corresponding to pH. According to the curve L1, the silica removal effect is best at about 90% when the pH is in the range of 8.0 to 9.0. According to the curve L2, the effect of removing fluoride ions is best, about 90%, when the pH is in the range of 6.8 to 7.5. Thus, according to the results shown in FIG. 3, it is preferable that the pH of the solution in the secondary reaction tank 12 is in the range of 6.8 to 7.5 and the pH of the solution in the tertiary reaction tank 13 is in the range of 8.0 to 9.0.
Preferably, a stirring barrel 133 is arranged in the third-stage reaction tank 13, a water inlet pipe 132 is arranged above the stirring barrel 133, a water distribution device 134 is arranged at the bottom of the stirring barrel 133, the water distribution device 134 is connected with the stirring barrel 133, the water distribution device 134 is used for controlling the water distribution amount at the bottom of the stirring barrel 133, the wastewater treated by the second-stage reaction tank 12 enters the stirring barrel 133 through the water inlet pipe 132, the wastewater fully treated by the stirrer 10 then enters the third-stage reaction tank 13 outside the stirring barrel 133 through the water distribution device 134, and the wastewater finally and automatically enters the circulation system along with the increase of the wastewater entering the third-stage reaction tank 13.
The wastewater treated by the third-stage reaction tank 13 enters a circulating system through gravity flow, the circulating system comprises a circulating sedimentation tank 14, the circulating sedimentation tank 14 is communicated with the third-stage reaction tank 13, the circulating sedimentation tank 14 is used for removing part of sludge in the wastewater treated by the third-stage reaction tank 13, and the sludge comprises relevant fluoride ions and silicide sediments generated in the high-efficiency reaction system and other sediments containing aluminum ions, calcium ions and magnesium ions.
In addition, the first order reaction tank 11, the second order reaction tank 12 and the medicament of the third order reaction tank 13 are thrown and are thrown with the waste water intake pump chain of the first order reaction tank 11 to make waste water get into when the first order reaction tank 11, the second order reaction tank 12 and the medicament of the third order reaction tank 13 is thrown and can be started automatically, and when waste water stops adding when the first order reaction tank 11, the second order reaction tank 12 and the third order reaction tank 13 also stops the medicament and throws.
Preferably, the circulation system further comprises: a mud scraper 141, a circulating sedimentation tank level gauge 142, a mud scraper rake 143, a flushing pipe 144, a mud pump 145, a mud pneumatic valve 146 and a first connecting line 147.
The mud scraper 141 is arranged inside the circulating sedimentation tank 14, the mud scraper rake 143 is connected with the mud scraper 141 so as to stir the sludge in the circulating sedimentation tank 14 through the mud scraper rake 143, and the mud scraper 141 can increase the reaction contact time and area of the sludge in the circulating sedimentation tank 14, so that the sludge is gathered together as much as possible, thereby facilitating the subsequent sludge discharge treatment.
The circulating sedimentation tank liquid level meter 142 is arranged on the circulating sedimentation tank 14, and the circulating sedimentation tank liquid level meter 142 is used for monitoring the volume of the solution in the circulating sedimentation tank 14 in real time.
The flushing pipe 144 is arranged inside the circulating sedimentation tank 14, the flushing pipe 144 is used for flushing the sludge settled at the bottom of the sedimentation circulating tank 14, the bottom of the circulating sedimentation tank 14 is in a cone bucket shape, and the sludge generated by the reaction is helped to settle at the bottom of the circulating sedimentation tank 14, so that the flushing pipe 144 is helped to regularly flush the sludge at the bottom of the circulating sedimentation tank 14, and then the sludge at the bottom of the circulating sedimentation tank 14 can be effectively discharged.
The first connection pipe 147 is communicated with the bottom of the circulation sedimentation tank 14, and the sludge discharge pump 145 and the sludge discharge pneumatic valve 146 are provided on the first connection pipe 147 to discharge the sludge settled at the bottom of the circulation sedimentation tank 14 through the first connection pipe 147. The sludge discharge pump 145 and the sludge discharge pneumatic valve 146 can automatically and periodically discharge the sludge settled at the bottom of the circulating sedimentation tank 14 out of the circulating sedimentation tank 14 through the first connecting pipeline 147.
The wastewater treated by the third-stage reaction tank 13 automatically enters the circulating sedimentation tank 14, and the wastewater treated by the high-efficiency reaction system is made to generate sludge sediment in the circulating sedimentation tank 14 through the mud scraper 141 and is precipitated. Subsequently, the bottom of the circulating sedimentation tank 14 is periodically washed through the washing pipe 144, and the sludge at the bottom of the circulating sedimentation tank 14 is automatically discharged out of the circulating sedimentation tank 14 through the first connection pipe 147 by the sludge discharge pump 145 and the sludge discharge pneumatic valve 146, thereby achieving the removal of a part of the sludge in the wastewater treated by the tertiary reaction tank 13. In addition, when the sludge concentration at the bottom of the circulation sedimentation tank 14 is more than 5%, the sludge can be automatically discharged out of the circulation sedimentation tank 14 from the first connection pipe 147 through the sludge discharge pump 145 and the sludge discharge pneumatic valve 146.
The tubular microfiltration system is communicated with the circulating sedimentation tank 14, a part of sludge sediment in the wastewater treated by the circulating sedimentation tank 14 is discharged from the circulating sedimentation tank 14 through the first connecting pipeline 147, and the other part of wastewater enters the tubular microfiltration system. The tubular microfiltration system is used for filtering the wastewater treated by the circulating sedimentation tank 14, so that the sludge mixed liquor is separated from the water solution.
Preferably, the tubular microfiltration system comprises: the device comprises a tubular microfiltration membrane device 16 and a water production tank 15, wherein the water production tank 15 is arranged below the tubular microfiltration membrane device 16, the water production tank 15 is communicated with the tubular microfiltration membrane device 16 through a second connecting pipeline 153, the tubular microfiltration membrane device 16 is used for filtering the wastewater treated by the circulating sedimentation tank 14, and the water production tank 15 is used for collecting the aqueous solution.
Preferably, the water outlet 162 of the tubular microfiltration membrane device is communicated with the top of the circulating sedimentation tank 14 through a third connecting pipeline 163, so that the sludge mixed liquor enters the circulating sedimentation tank 14 through the third connecting pipeline 163; the water inlet 161 of the tubular microfiltration membrane device is communicated with the bottom of the circulating sedimentation tank 14 through a fourth connecting pipeline 168, so that the wastewater treated by the circulating sedimentation tank 14 enters the tubular microfiltration membrane device 16 through the fourth connecting pipeline 168.
Preferably, a flow meter 164 and a water return pneumatic valve 165 are disposed on the third connecting pipeline 163, the flow meter 164 can monitor the throughput of the sludge mixed liquid passing through the third connecting pipeline 163 in real time, and the sludge mixed liquid passing through the water return pneumatic valve 165 can automatically enter the circulating sedimentation tank 14 through the third connecting pipeline 163.
Preferably, the fourth connecting line 168 is provided with a water inlet basket filter 166, a circulating pump 167 and a water inlet pneumatic valve 169. The wastewater treated by the circulating sedimentation tank 14 firstly enters the water inlet basket filter 166 through the fourth connecting pipeline 168, then enters the circulating pump 167, and then enters the tubular microfiltration membrane device 16 through the water inlet pneumatic valve 169 under the action of the circulating pump 167. The middle lower part of the circulating sedimentation tank 14 is provided with a bell-mouth-shaped water suction port, so that when wastewater enters the fourth connecting pipeline 168, the wastewater in the circulating sedimentation tank 14 is not disturbed, and in order to prevent the circulating pump 167 from being blocked by sludge at the inlet, the flushing pipe 144 can regularly flush the circulating pump 167. The inlet basket filter 166 prevents large particles in the wastewater from entering the tubular microfiltration membrane device 16 and prevents clogging and scratching of the tubular microfiltration membrane device 16. The circulating pump 167 can ensure that the wastewater treated by the circulating sedimentation tank 14 automatically enters the tubular microfiltration membrane device 16, and the inlet pneumatic valve 169 and the return pneumatic valve 165 can ensure that the tubular microfiltration membrane device 16 automatically filters the wastewater.
Preferably, a third pH meter 151 and a water producing tank liquid level meter 152 are arranged on the water producing tank 15. The third pH meter 151 is used for monitoring the pH of the solution in the water production tank 15 in real time, and the third pH meter 151 is connected with a hydrochloric acid pump, so that hydrochloric acid can be automatically added into the water production tank 15 and the pH of the solution in the water production tank 15 can be adjusted. The circulating sedimentation tank liquid level meter 142, the water production tank liquid level meter 152 and the circulating pump 167 are in on-off linkage, namely when the circulating sedimentation tank liquid level meter 142 is at a high liquid level or the water production tank liquid level meter 152 is at a low liquid level, the circulating pump 167 is automatically started, and when the circulating sedimentation tank liquid level meter 142 is at a low liquid level or the water production tank liquid level meter 152 is at a high liquid level, the circulating pump 167 is automatically stopped. Therefore, automatic precipitation and filtration reaction of the wastewater in the circulating sedimentation tank 14 and the tubular microfiltration system can be realized, and the precipitation and filtration efficiency of the wastewater is improved.
The wastewater treated in the circulating sedimentation tank 14 automatically enters the tubular microfiltration membrane device 16 through the fourth connecting pipeline 168 in the presence of the circulating pump 167, the wastewater is filtered in the tubular microfiltration membrane device 16, the generated sludge mixed liquid enters the circulating sedimentation tank 14 through the third connecting pipeline 163 for sedimentation and discharge, and the filtered water solution enters the product water tank 15 through the second connecting pipeline 153 for collection. In the filtering process, when the concentration of the sludge in the sludge mixed liquid is greater than 5%, the sludge mixed liquid automatically enters the circulating sedimentation tank 14 through the third connecting pipeline 163, and the flow rate of the wastewater in the tubular microfiltration membrane device 16 is 9-10 times of the flow rate of the effluent entering the water production tank 15 through the second connecting pipeline 153. The tubular microfiltration system and the circulating system can effectively control the floc concentration in the wastewater, and in the tubular microfiltration membrane device 16, the floc concentration of the wastewater is 3000 mg/L-6000 mg/L, so that the aluminum ions and the fluorine ions in the wastewater can be ensured to be fully and effectively contacted and reacted to form precipitates, and the filtering efficiency of the wastewater is improved.
In this embodiment, at first, through high-efficient reaction system disinfects waste water to get rid of fluorinion and silica in the waste water, afterwards, through circulation system with tubular micro-filtration system coupling, it is right waste water that high-efficient reaction system has handled carries out precipitation filtration processing, gets rid of the remaining mud precipitate that contains magnesium, calcium and aluminium ion in the waste water, and passes through product water pond 15 collects the aqueous solution after filtering, just circulation system with tubular micro-filtration system can carry out circulating filtration to waste water many times, and until effluent quality of water reaches follow-up technological requirement. The water solution collected in the water producing tank 15 basically contains no calcium, magnesium, aluminum, fluoride ions and silicon dioxide, and can effectively avoid blockage and corrosion of subsequent instruments after the water solution is discharged, so that the subsequent recycling of high-concentration salt wastewater is improved.
To sum up, the utility model provides a processing apparatus of high enriched salt waste water, include: the efficient reaction system comprises a first-stage reaction tank, a second-stage reaction tank and a third-stage reaction tank, wherein the second-stage reaction tank is respectively communicated with the first-stage reaction tank and the third-stage reaction tank, the first-stage reaction tank is used for sterilizing microorganisms in wastewater, the second-stage reaction tank is used for removing fluoride ions in the wastewater treated by the first-stage reaction tank, and the third-stage reaction tank is used for removing silicon dioxide in the wastewater treated by the second-stage reaction tank; the circulating system comprises a circulating sedimentation tank, the circulating sedimentation tank is communicated with the third-stage reaction tank, and the circulating sedimentation tank is used for removing part of sludge in the wastewater treated by the third-stage reaction tank; the tubular microfiltration system, the tubular microfiltration system with the circulation sedimentation tank is linked together, the tubular microfiltration system is used for filtering the waste water that the circulation sedimentation tank was handled for mud mixed liquor separates with the aqueous solution, can effectively get rid of the fluoride ion and the silica in the high enriched salt waste water, promotes the later stage recycle of high enriched salt waste water.
An embodiment of the present invention further provides a method for treating high-concentration salt wastewater, referring to fig. 2, the method for treating high-concentration salt wastewater includes:
step S1, providing a treatment device for wastewater and the high-concentration salt wastewater;
s2, carrying out microbial sterilization on microorganisms in the wastewater by adopting the primary reaction tank;
s3, removing fluorine ions in the wastewater treated by the primary reaction tank by using the secondary reaction tank;
s4, removing silicon dioxide in the wastewater treated by the second-stage reaction tank by using the third-stage reaction tank;
s5, removing partial sludge in the wastewater treated by the third-stage reaction tank by using the circulating sedimentation tank;
and S6, filtering the wastewater treated by the circulating sedimentation tank by using the tubular microfiltration system so as to separate sludge mixed liquor from aqueous solution.
The method for treating high salinity wastewater provided in this example will be described in more detail with reference to fig. 3.
According to step S1, a wastewater and a treatment apparatus for the high-salinity wastewater are provided, the wastewater containing fluorine ions and silica to be removed.
In order to realize zero discharge of the high-concentration salt wastewater, the wastewater needs to be subjected to desalination technical treatment. The desalting treatment of the wastewater mainly adopts a physical method, and the technically mature desalting technology mainly comprises an electrodialysis treatment technology and an evaporative crystallization device. Before desalting treatment, fluoride ions and silica in the wastewater need to be removed, otherwise, residual fluoride ions and silica in the wastewater influence the performance of an electrodialysis membrane and an evaporative crystallization device, and thus influence the desalting effect of the wastewater.
The device for treating high-salinity wastewater is specifically described above, and is not described in detail herein.
And (3) according to the step S2, carrying out microbial sterilization on the microorganisms in the wastewater by adopting the primary reaction tank 11.
Preferably, the step of performing the microbial sterilization of the microorganisms in the wastewater by using the primary reaction tank 11 comprises: sodium hypochlorite is added to the wastewater in the primary reaction tank 11.
According to the step S3, the secondary reaction tank 12 is adopted to remove the fluorine ions in the wastewater treated by the primary reaction tank 11.
The step S3 may include: firstly, monitoring the pH value of the wastewater in the secondary reaction tank 12 by the first pH meter 121; then, adding hydrochloric acid into the wastewater in the secondary reaction tank 12, and adjusting the pH range of the wastewater to 6.8-7.5; subsequently, polyaluminum chloride is added to the wastewater after the pH adjustment is completed, thereby removing the fluoride ions in the wastewater. According to a curve L2 in fig. 3, the removal rate of the fluoride ions changes with the change of the pH of the wastewater, and when the pH of the wastewater ranges from 6.8 to 7.5, the removal rate of the fluoride ions is the highest and can reach 90%, so that the pH of the wastewater in the secondary reaction tank 12 is regulated and controlled, and the optimal fluoride removal effect of the secondary reaction tank 12 is achieved.
And according to the step S4, removing silicon dioxide in the wastewater treated by the secondary reaction tank 12 by using the tertiary reaction tank 13.
The step S4 may include: firstly, monitoring the pH value of the wastewater in the tertiary reaction tank 13 by the second pH meter 131; subsequently, adding sodium hydroxide into the wastewater in the third-stage reaction tank 13, and adjusting the pH range of the wastewater to 8.0-9.0; subsequently, sodium metaaluminate and polymeric ferric sulfate are added to the wastewater after the pH adjustment is completed, thereby removing the silica in the wastewater. According to a curve L1 in fig. 3, the removal rate of silica varies with the pH of the wastewater, and when the pH of the wastewater ranges from 8.0 to 9.0, the removal rate of silica is the highest and can reach 90%, so that the pH of the wastewater in the tertiary reaction tank 13 is regulated and controlled, thereby achieving the optimal silica removal efficiency of the tertiary reaction tank 13.
And according to the step S5, removing part of sludge in the wastewater treated by the third-stage reaction tank 13 by using the circulating sedimentation tank 14.
The step S5 may include: firstly, the wastewater treated by the tertiary reaction tank 13 is stirred by the mud scraper 141 and the mud scraper rake 143, so that part of sludge in the wastewater is precipitated; subsequently, the sludge accumulated at the bottom of the circulation sedimentation tank 14 is washed through the washing pipe 144; then, the sludge accumulated at the bottom of the circulation sedimentation tank 14 is automatically discharged out of the circulation sedimentation tank 14 through the first connection pipe 147 by the sludge discharge pump 145.
According to step S6, the wastewater treated by the circulating sedimentation tank 14 is filtered by the tubular microfiltration system, so that the sludge mixed liquor is separated from the aqueous solution.
The step S6 may include: firstly, the wastewater treated by the circulation sedimentation tank 14 is automatically moved into the tubular microfiltration membrane device 16 from the fourth connecting pipeline 168 through the circulation pump 167; subsequently, the wastewater is subjected to filtration treatment by the tubular microfiltration membrane device 16; then, the filtered sludge mixed liquid is returned to the circulating sedimentation tank 14 through the third connecting pipe 163 for circulating sedimentation, and the filtered aqueous solution enters the water production tank 15 through the second connecting pipe 153 and is collected.
Preferably, the fluoride ion concentration in the provided wastewater is 160 mg/L-190 mg/L, and the silicon dioxide concentration in the provided wastewater is 200 mg/L-430 mg/L; the fluorine ion concentration in the aqueous solution is 15 mg/L-20 mg/L, and the silicon dioxide concentration in the aqueous solution is 20 mg/L-30 mg/L. Under the treatment method of the high-concentration salt wastewater, the removal rate of fluoride ions can reach 90%, the removal rate of silicon dioxide can reach 92%, and through the treatment method of the high-concentration salt wastewater, aluminum ions, calcium ions and magnesium ions in the wastewater can be effectively removed, so that the blockage and corrosion of a follow-up instrument caused by water solution yielding can be effectively avoided, and the follow-up recycling of the high-concentration salt wastewater is improved.
To sum up, the utility model discloses still provide a high enriched salt waste water's processing method, include: providing a wastewater and a treatment device for the high-salinity wastewater; carrying out microbial sterilization on microorganisms in the wastewater by adopting the primary reaction tank; removing fluorine ions in the wastewater treated by the primary reaction tank by using the secondary reaction tank; removing silicon dioxide in the wastewater treated by the second-stage reaction tank by using the third-stage reaction tank; removing part of sludge in the wastewater treated by the third-stage reaction tank by adopting the circulating sedimentation tank; adopt tubular microfiltration system filters the waste water that the circulation sedimentation tank was handled for mud mixed liquor separates with the aqueous solution, can effectively get rid of the fluorinion and the silica in the high enriched salt waste water, promotes the later stage recycle of high enriched salt waste water.
The above description is only for the preferred embodiment of the present invention and is not intended to limit the scope of the present invention, and any modification and modification made by those skilled in the art according to the above disclosure are all within the scope of the claims.
Claims (8)
1. A treatment device for high-concentration salt wastewater is characterized by comprising:
the efficient reaction system comprises a first-stage reaction tank, a second-stage reaction tank and a third-stage reaction tank, wherein the second-stage reaction tank is respectively communicated with the first-stage reaction tank and the third-stage reaction tank, the first-stage reaction tank is used for sterilizing microorganisms in wastewater, the second-stage reaction tank is used for removing fluoride ions in the wastewater treated by the first-stage reaction tank, and the third-stage reaction tank is used for removing silicon dioxide in the wastewater treated by the second-stage reaction tank;
the circulating system comprises a circulating sedimentation tank, the circulating sedimentation tank is communicated with the third-stage reaction tank, and the circulating sedimentation tank is used for removing part of sludge in the wastewater treated by the third-stage reaction tank;
and the tubular microfiltration system is communicated with the circulating sedimentation tank and is used for filtering the wastewater treated by the circulating sedimentation tank so as to separate sludge mixed liquor from aqueous solution.
2. The apparatus for treating high salinity wastewater according to claim 1, wherein said primary reaction tank, said secondary reaction tank and said tertiary reaction tank are all provided with a stirrer, and said secondary reaction tank and said tertiary reaction tank are all provided with a pH meter.
3. The apparatus for treating high salinity wastewater according to claim 1, wherein, the circulation system further comprises: the device comprises a mud scraper, a mud scraper rake, a circulating sedimentation tank liquid level meter, a flushing pipe, a mud pump, a mud pneumatic valve and a first connecting pipeline; the mud scraper is arranged inside the circulating sedimentation tank, and the mud scraper rake is connected with the mud scraper so as to stir the sludge in the circulating sedimentation tank through the mud scraper rake; the circulating sedimentation tank liquid level meter is arranged on the circulating sedimentation tank; the flushing pipe is arranged in the circulating sedimentation tank and is used for flushing sludge settled at the bottom of the circulating sedimentation tank; the first connecting pipeline is communicated with the bottom of the circulating sedimentation tank, and the sludge discharge pump and the sludge discharge pneumatic valve are arranged on the first connecting pipeline so as to discharge sludge precipitated at the bottom of the circulating sedimentation tank through the first connecting pipeline.
4. The apparatus for treating high salinity wastewater according to claim 1, wherein, the tubular microfiltration system comprises:
the device comprises a tubular microfiltration membrane device and a water production pool, wherein the water production pool is arranged below the tubular microfiltration membrane device and is communicated with the tubular microfiltration membrane device through a second connecting pipeline, the tubular microfiltration membrane device is used for filtering the wastewater treated by the circulating sedimentation tank, and the water production pool is used for collecting the aqueous solution.
5. The apparatus for treating high-salinity wastewater according to claim 4, wherein the water outlet of the tubular microfiltration membrane device is communicated with the top of the circulating sedimentation tank through a third connecting pipeline, so that the sludge mixed liquor enters the circulating sedimentation tank through the third connecting pipeline; and a water inlet of the tubular microfiltration membrane device is communicated with the bottom of the circulating sedimentation tank through a fourth connecting pipeline, so that the wastewater treated by the circulating sedimentation tank enters the tubular microfiltration membrane device through the fourth connecting pipeline.
6. The apparatus for treating high salinity wastewater according to claim 5, wherein, a flow meter and a backwater pneumatic valve are arranged on the third connecting pipeline.
7. The apparatus for treating high salinity wastewater according to claim 5, wherein the fourth connecting line is provided with an inlet basket filter, a circulating pump and an inlet pneumatic valve.
8. The apparatus for treating high salinity wastewater according to claim 4, characterized in that the water producing tank is provided with a water producing tank liquid level meter and a pH meter.
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| CN202320112708.0U CN218879677U (en) | 2023-01-18 | 2023-01-18 | High-concentration salt wastewater treatment device |
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| CN202320112708.0U CN218879677U (en) | 2023-01-18 | 2023-01-18 | High-concentration salt wastewater treatment device |
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