CN216513312U - Near zero discharge system of advanced treatment coking strong brine - Google Patents
Near zero discharge system of advanced treatment coking strong brine Download PDFInfo
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- CN216513312U CN216513312U CN202122558684.5U CN202122558684U CN216513312U CN 216513312 U CN216513312 U CN 216513312U CN 202122558684 U CN202122558684 U CN 202122558684U CN 216513312 U CN216513312 U CN 216513312U
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Abstract
The utility model discloses a near-zero emission system for deeply treating coking strong brine, which comprises a regulating pond system, a DTRO pretreatment system, a filter, a DTRO membrane concentration system, a water production tank, a strong water tank, an evaporation pretreatment system, an evaporation crystallization system, a mother liquor drying system, a temporary sludge storage pond, a sludge concentration pond and a sludge disposal system; the adjusting tank system, the DTRO pretreatment system, the filter, the DTRO membrane concentration system, the concentrated water tank, the evaporation pretreatment system, the evaporation crystallization system and the mother liquor drying system are communicated in sequence; the DTRO pretreatment system and the evaporation pretreatment system are both communicated with a temporary sludge storage tank; the temporary sludge storage tank, the sludge concentration tank and the sludge disposal system are communicated in sequence; the filter reaches the sludge concentration tank all with the governing pond system is linked together.
Description
Technical Field
The utility model relates to the technical field of coking wastewater treatment systems, in particular to a near-zero discharge system for deeply treating coking strong brine.
Background
The coking wastewater has complex components, contains pollutants such as phenols, polycyclic aromatic compounds, heterocyclic compounds of nitrogen, oxygen and sulfur and the like, is typical industrial wastewater which contains refractory organic compounds, has high concentration, high pollution, toxicity and difficult treatment, and contains a large amount of organic and inorganic harmful substances which are harmful to human bodies and pollute the environment. At present, enterprises mostly adopt a treatment process of 'biochemical treatment and advanced treatment', the produced water of a system after treatment is used for recycling, the recovery rate is generally about 70%, the concentrated water produced by the system is used for coke quenching and blast furnace slag flushing treatment or direct discharge after standard treatment, near zero emission is not realized, surface water and underground water are polluted, and waste of water resources is caused.
Therefore, how to improve the generation amount of reuse water in the coking wastewater treatment system, reduce the waste of water resources and realize the near-zero discharge of coking wastewater is a problem to be solved urgently by enterprises in the current stage.
Through search, the following two patent publications related to the present patent application are found.
The prior art discloses a zero discharge treatment system for coking wastewater, which consists of an advanced treatment process and a deamination nitrogen film device. Performing advanced treatment on the coking wastewater on the basis of the primary treatment, and then separating the amlodipine and the water by adopting an advanced deamination nitrogen membrane (modified anti-pollution membrane) separation technology, wherein the splashed water of the membrane after the treatment is low-purity water and can be recycled as circulating condensate water; the concentrated water (rich in oxygen and ammonia) of the membrane can also be recycled as coke quenching water, so that zero discharge of the coking wastewater is achieved.
The patent zero emission system mainly has the following problems: (1) the coking wastewater after biochemical treatment adopts an advanced deamination nitrogen membrane separation technology, only ammonia nitrogen in the wastewater is removed, and other organic matters, COD and other pollutants are not removed; (2) the concentrated water of the membrane is used as coke quenching water, and zero emission is not really realized.
The prior art also discloses a zero-discharge treatment method of coking wastewater. The system comprises: pretreating the coking wastewater, wherein the pretreatment comprises flocculation treatment, ultrafiltration treatment and softened water treatment; carrying out primary nanofiltration treatment on the pretreated coking wastewater to obtain primary nanofiltration produced water and primary nanofiltration concentrated water; carrying out secondary nanofiltration treatment, activated carbon adsorption treatment, tubular microfiltration treatment and tertiary nanofiltration treatment on the primary nanofiltration concentrated water to obtain tertiary nanofiltration concentrated water and tertiary nanofiltration water; carrying out electrically driven membrane concentration treatment and evaporative crystallization treatment on the three-stage nanofiltration concentrated water to obtain an industrial-grade sodium sulfate product; and carrying out reverse osmosis membrane concentration treatment, tubular microfiltration treatment, electric driven membrane concentration treatment and evaporative crystallization treatment on the primary nanofiltration water production water, the secondary nanofiltration water production water and the tertiary nanofiltration water production water to obtain an industrial grade sodium chloride product. By removing pollutants such as organic matters and inorganic matters in the coking wastewater and separating and concentrating sodium chloride and sodium sulfate, zero discharge of the coking wastewater is realized.
According to the method, nanofiltration is adopted to separate salt, sodium chloride and sodium sulfate in the coking wastewater are separated, and sodium chloride salt and sodium sulfate salt products are obtained through evaporation and concentration, so that zero discharge of wastewater is realized. There are problems in that: (1) the COD content in the coking wastewater is high, the pollution of a common nanofiltration membrane is serious, the flushing frequency is high, and the service life of the membrane is greatly reduced; (2) the concentration multiple of the nanofiltration membrane is low, so that the evaporation load is large and the cost is high; (3) because the coking wastewater has complex components, the product obtained by nanofiltration salt separation and evaporation has low salt purity and low market utilization value.
SUMMERY OF THE UTILITY MODEL
Therefore, the utility model provides a near zero emission system for deeply treating coking strong brine, which aims to solve at least one problem in the prior art.
In order to achieve the above purpose, the utility model provides the following technical scheme:
according to the utility model, the near zero emission system for deeply treating the coking strong brine comprises a regulating pond system, a DTRO pretreatment system, a filter, a DTRO membrane concentration system, a water production tank, a concentrated water tank, an evaporation pretreatment system, an evaporation crystallization system, a mother liquor drying system, a temporary sludge storage pond, a sludge concentration pond and a sludge disposal system; the adjusting pond system, the DTRO pretreatment system, the filter, the DTRO membrane concentration system, the concentrated water tank, the evaporation pretreatment system, the evaporation crystallization system and the mother liquor drying system are communicated in sequence; the DTRO pretreatment system and the evaporation pretreatment system are both communicated with a temporary sludge storage tank; the temporary sludge storage tank, the sludge concentration tank and the sludge disposal system are communicated in sequence; the filter reaches the sludge concentration tank all with the governing pond system is linked together.
Further, the filter is provided with a backwashing water outlet, and the filter is communicated with the regulating pond system through the backwashing water outlet.
Further, the water production tank is communicated with the filter.
Further, the regulating reservoir system comprises a regulating reservoir and a stirrer, and the stirrer is arranged in the regulating reservoir.
Further, the stirrer is a submersible stirrer or a top-feed stirrer.
Further, the evaporative crystallization system is a triple effect evaporative crystallization system.
Further, the mother liquor drying system comprises a roller scraper type dryer, a miscellaneous salt outlet of the roller scraper type dryer is connected with a miscellaneous salt collecting device, and a waste gas outlet of the roller scraper type dryer is connected with a waste gas treatment system.
Further, the filter is a fiber filter; the fiber filter is characterized in that a filter unit is arranged in the tank body of the fiber filter, and the filter unit comprises a fiber bundle.
Further, the DTRO pretreatment system and the evaporation pretreatment system are both provided with high-density sedimentation tanks, and the high-density sedimentation tanks are provided with reaction zones, flocculation zones and sedimentation zones.
Further, the DTRO membrane concentration system comprises a DTRO cartridge filter, a DTRO membrane module and a DTRO cleaning device, wherein the DTRO cartridge filter is a core filter, and the DTRO membrane module comprises a high-pressure pump, a circulating pump, a DTRO membrane column, a water production tank and a concentrated water tank; the DTRO cleaning device comprises an alkaline washing dosing tank and an acid washing dosing tank.
The utility model has the following advantages:
according to the utility model, a plurality of process systems are reasonably combined together, so that a near zero emission system for deeply treating the coking strong brine is formed, and the problems that the coking strong brine is difficult to treat, the water yield is low, the system is easy to block in structure, zero emission cannot be realized and the like due to the influence factors of complex components, high organic matter content, high COD concentration and the like of the coking strong brine are solved, so that the water yield of the strong brine is improved, the cleaning frequency of the system is reduced, the risk of system blockage and corrosion is reduced, and the near zero emission of the coking strong brine is realized.
The DTRO pretreatment system and the evaporation pretreatment system in the utility model adopt a high-density sedimentation tank, which integrates the functions of coagulation, flocculation, inclined tube sedimentation and sludge concentration, and provides a nucleus body for the flocculation process through the backflow of the sediment sludge, thereby ensuring that the formed floc particles are large and compact, and being beneficial to the sedimentation separation effect of solid and liquid. The high-density sedimentation tank adopts a rectangular tank body, has a simple structure and occupies less land; the sludge is refluxed, so that the flocculation effect is greatly improved, and the flocculation time is shortened; by adopting a magnetic flocculation technology, insoluble pollutants such as tiny suspended matters, colloids and bacteria in a water body are effectively combined with magnetic powder through flocculation, attraction, attachment, electric charge adsorption and other effects to form magnetic flocs with larger volume and density, and then the microclocculates overcome the resistance of fluid and the self gravity under the action of a high-intensity magnetic field generated by a super-magnetic separation device, so that rapid directional motion is generated, the flocculation effect is enhanced, the pollutants with more tiny particle sizes can be captured and coagulated, the flocs settle quickly, the water body purification effect is excellent, and the effluent is clear and transparent; magnetic powder and sludge are separated from the mixed sludge discharged from the sedimentation tank through a magnetic separation device, and the separated magnetic powder returns to the flocculation tank to participate in reaction, so that recycling is realized, and the cost is saved; the separated sludge partially flows back to the flocculation tank, the sludge concentration in the strong brine is increased, alum flocs are quickly formed in the strong brine, the sedimentation speed of the flocs can be increased by the returned sludge particles, the removal rate of pollutants can be greatly improved by the flocculation adsorption effect of biological flocs in the sludge, the effect of strengthening the treatment of suspended matters is achieved, and excessive addition of medicaments can be avoided; and conveying the separated residual sludge to a temporary sludge storage tank for subsequent treatment.
The filter is a fiber filter, and fiber bundles are utilized to intercept suspended matters, organic matters and partial heavy metal ions in the concentrated salt water, so that the turbidity of raw water is reduced, and the long-term stable operation of a DTRO (draw texturing yarn) membrane concentration system is ensured.
The DTRO membrane concentration system adopts a disc tube type reverse osmosis membrane to perform decrement concentration on strong brine; the DTRO membrane system is a closed system, is not interfered by the outside world, is not influenced by factors such as biodegradability and the like, and has stable system and high water yield; the strong brine flow of the membrane component is short, the flow channel is wide, the pollution degree of the membrane is reduced, the defect that other membrane components are easy to block is overcome, and the strong adaptability to high-concentration organic wastewater is realized.
In addition, because the concentrated salt water contains COD, the concentration of the COD contained in the concentrated salt water is higher through membrane concentration and evaporation crystallization, and a certain amount of evaporation mother liquor needs to be discharged to ensure the evaporation efficiency. According to the utility model, a mother liquor drying system is adopted to carry out drying treatment on the evaporation mother liquor to obtain dry miscellaneous salt and waste gas, and the waste gas is washed by a washing tower and discharged after reaching the standard, so that near zero emission of coking strong brine is realized.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. It should be apparent that the drawings in the following description are merely exemplary, and that other embodiments can be derived from the drawings provided by those of ordinary skill in the art without inventive effort.
The structures, ratios, sizes, and the like shown in the present specification are only used for matching with the contents disclosed in the specification, so as to be understood and read by those skilled in the art, and are not used to limit the conditions that the present invention can be implemented, so that the present invention has no technical significance, and any structural modifications, changes in the ratio relationship, or adjustments of the sizes, without affecting the effects and the achievable by the present invention, should still fall within the range that the technical contents disclosed in the present invention can cover.
FIG. 1 is a schematic flow diagram illustrating a near zero emission system for the advanced treatment of coker brine in accordance with an exemplary embodiment;
in the figure: 1. the system comprises a regulating pond system, a DTRO pretreatment system, a filter, a DTRO membrane concentration system, a water production tank, a concentrated water tank, a 7 evaporation pretreatment system, a 8 evaporation crystallization system, a 9 mother liquor drying system, a 10 sludge temporary storage pond, a 11 sludge concentration pond, a 12 sludge disposal system.
Detailed Description
The present invention is described in terms of particular embodiments, other advantages and features of the utility model will become apparent to those skilled in the art from the following disclosure, and it is to be understood that the described embodiments are merely exemplary of the utility model and that it is not intended to limit the utility model to the particular embodiments disclosed. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
According to an embodiment of the present invention, a near zero emission system for deep treatment of coking strong brine is provided, as shown in fig. 1, including a regulating pond system 1, a DTRO (Disc tube reverse osmosis) pretreatment system 2, a filter 3, a DTRO membrane concentration system 4, a water production tank 5, a thick water tank 6, an evaporation pretreatment system 7, an evaporation crystallization system 8, a mother liquor drying system 9, a sludge temporary storage pond 10, a sludge concentration pond 11, and a sludge disposal system 12; wherein the regulating pond system 1, the DTRO pretreatment system 2, the filter 3, the DTRO membrane concentration system 4, the concentrated water tank 6, the evaporation pretreatment system 7, the evaporation crystallization system 8 and the mother liquor drying system 9 are communicated in sequence; the DTRO pretreatment system 2 and the evaporation pretreatment system 7 are both communicated with a temporary sludge storage tank 10; the temporary sludge storage tank 10, the sludge concentration tank 11 and the sludge disposal system 12 are communicated in sequence; the filter 3 and the sludge concentration tank 11 are communicated with the regulating tank system 1.
The filter 3 is provided with a backwashing water outlet, and the filter 3 is communicated with the regulating pond system 1 through the backwashing water outlet. Wherein the filter 3 delivers backwash wastewater to the regulating tank system 1 through the backwash water discharge port, thereby treating the backwash wastewater.
The water production tank 5 is communicated with the filter 3, and backwash water in the water production tank 5 can be conveyed into the filter 3 for filtering.
The regulating pond system 1 comprises a regulating pond and a stirrer, wherein the stirrer is arranged in the regulating pond and used for homogenizing incoming water of the regulating pond. The stirrer is a submersible stirrer or a jacking stirrer. The equalizing basin is provided with a strong brine water inlet, a filter backwashing water return inlet, a sludge concentration tank supernatant return inlet and the like, and the strong brine water inlet, the filter backwashing water return inlet, the sludge concentration tank supernatant return inlet and the like are respectively used for realizing the inflow of coking wastewater, the inflow of backwashing wastewater and liquid in the sludge concentration tank 11. Both submersible mixers and jack-in mixers are common components in the prior art and their construction is not described in detail here.
The evaporative crystallization system 8 is a triple effect evaporative crystallization system. The triple-effect evaporative crystallization system adopts a downstream evaporation process and mainly comprises a preheater, a heater, a separator, a final-effect condenser, a forced circulation pump, a thickener, a centrifuge, a mother liquor tank and the like; fresh steam condensate water and secondary steam condensate water generated by the system are recycled in a unified manner, DTRO concentrated solution sequentially passes through a preheater, a heater and a separator, enters a thickener after reaching the discharge concentration, materials in the thickener enter a centrifugal machine for centrifugation after thickening, crystallized miscellaneous salt after centrifugation is packed by a ton bag, mother liquor generated by centrifugation returns to a system for continuous evaporation and concentration, and COD (Chemical Oxygen Demand) in the mother liquor reaches a certain concentration and is discharged to a mother liquor drying system for drying treatment.
The mother liquor drying system 9 comprises a roller scraper type dryer, a miscellaneous salt outlet of the roller scraper type dryer is connected with a miscellaneous salt collecting device, miscellaneous salts collected by the miscellaneous salt collecting device are disposed by outsourcing, and a waste gas outlet of the roller scraper type dryer is connected with a waste gas treatment system. The roller scraper type dryer adopts steam as a heat source; the waste gas treatment device comprises an induced draft fan and a washing tower; the inlet of the induced draft fan is connected with the waste gas outlet of the roller scraper dryer, the outlet of the induced draft fan is connected with the inlet of the washing tower, and the outlet of the washing tower is connected with the atmosphere; the washing tower adopts a multi-stage spraying device; the washing tower is internally provided with the filler, so that gas-liquid contact is increased, and the washing effect is improved.
The filter 3 is a fiber filter; the fiber filter is characterized in that a filter unit is arranged in the tank body of the fiber filter, and the filter unit comprises a fiber bundle. The filter unit is provided with a plurality of sets and consists of a certain number of fiber bundles; the fiber filter is matched with a backwashing fan and a backwashing pump. And the inlet of the backwashing pump is connected with the water production tank 5, and the outlet of the backwashing pump is connected with the fiber filter. When the filter tank works, the rotary mechanism arranged outside the tank body drives the filter unit to rotate, so that the fiber tows are tightly wound on the central water production assembly to form a tiny and fine filter layer, and therefore, the filter tank plays a role in intercepting and adsorbing dirt in water. When the trapped dirt is increased and the pressure difference reaches a set value, the filter automatically enters a back washing step. During backwashing, the external slewing mechanism drives the fiber tows to be completely loosened, and under the combined action of backwashing water flow and backwashing air, intercepted matters of the fiber filtering layer are discharged through the blow-off pipe and then automatically enter a filtering state.
The DTRO pretreatment system 2 and the evaporation pretreatment system 7 are both provided with high-density sedimentation tanks, and the high-density sedimentation tanks are provided with reaction zones, flocculation zones and sedimentation zones. The reaction zone is provided with a plurality of reaction tanks, and according to the actual water quality condition, agents such as lime, PFS (Polymeric ferric sulfate), sodium hydroxide, sodium carbonate, PAM (Polyacrylamide) and the like are respectively added to reduce the hardness, alkalinity and fluoride ion concentration of the concentrated brine; magnetic powder is added into the flocculation area, and the magnetic flocculation technology is adopted, so that the magnetic powder and pollutants are flocculated and combined into a whole, the coagulation and flocculation effects are enhanced, the density of generated flocs is higher and firmer, and the purpose of high-speed sedimentation is achieved; the system is provided with magnetic separation equipment for separating magnetic powder from sludge, the separated magnetic powder is recycled, and the separated sludge is discharged to a temporary sludge storage tank 10; the magnetic separation equipment is placed above the pretreatment tank body, the separated magnetic powder directly falls into the flocculation tank for recycling, and the separated sludge flows to the sludge temporary storage tank 10 by gravity.
The DTRO membrane concentration system 4 comprises a DTRO cartridge filter, a DTRO membrane assembly and a DTRO cleaning device, wherein the DTRO cartridge filter is a core filter, and the DTRO membrane assembly comprises a high-pressure pump, a circulating pump, a DTRO membrane column, a produced water tank and a concentrated water tank; the DTRO cleaning device comprises an alkaline washing dosing tank and an acid washing dosing tank. The DTRO cartridge filter is a core type filter and is used for intercepting large-particle substances in the strong brine and simultaneously uniformly mixing medicaments such as a scale inhibitor and the like with the strong brine; the DTRO membrane assembly is a skid-mounted module; the high-pressure pump is a centrifugal pump or a plunger pump; the circulating pumps are centrifugal pumps, and the number of the circulating pumps can be 1-3 according to different water production rate requirements; the DTRO membrane component can be arranged into 1-3 sections according to the requirement of water yield; the inlet of the DTRO cartridge filter is connected with the outlet of the fiber filter, the outlet of the DTRO cartridge filter is connected with the inlet of the high-pressure pump, the outlet of the high-pressure pump is connected with a plurality of sections of DTRO module assemblies, each section consists of a circulating pump and a plurality of membrane columns, the water production outlet of the DTRO skid-mounted module is connected with the water production tank 5, and the concentrated water outlet is connected with the concentrated water tank 6; the DTRO cleaning device is provided with an alkaline washing dosing tank and an acid washing dosing tank; adding a sodium hydroxide solution into the alkaline washing dosing tank, and adding a hydrochloric acid solution into the acid washing dosing tank; the alkaline washing dosing tank is provided with a washing heater; the cleaning heater can be an electric heater or a steam coil heater; the DTRO cleaning device is communicated with an inlet pipeline of the high-pressure pump, and the DTRO membrane assembly is connected with the DTRO cleaning device, so that a cleaning circulation loop is formed.
The sludge temporary storage tank 10 is connected with the sludge concentration tank 11, sludge is conveyed to the sludge concentration tank 11 through a sludge pump for concentration and layering, supernatant of the concentration tank returns to the regulating tank system 1 for retreatment, and underflow sludge of the sludge concentration tank 11 is conveyed to the sludge disposal system 12 through a screw pump.
The sludge disposal system 12 adopts a belt filter press or a plate-and-frame filter press, the water content of the produced sludge is less than 70%, and the sludge is transported outside for disposal.
The work flow of the near zero emission system for deeply treating the coking strong brine can be as follows:
after the quality of the incoming water of the raw strong brine after the biochemical treatment is stabilized by the regulating reservoir, the incoming water is conveyed to the DTRO pretreatment system 2 by the raw water lift pump for the chemical softening treatment, the softened water enters the buffer water reservoir, adding hydrochloric acid into a buffer water tank to adjust the pH value to be neutral, conveying the pH value to a filter 3 by a pump for filtering, removing colloid and suspended matters in concentrated salt water, lifting filtrate by a high-pressure pump, conveying the filtrate into a DTRO membrane concentration system 4 for concentration treatment, conveying DTRO produced water into a water production tank 5 for reuse, conveying the DTRO concentrated water into a concentrated water tank 6 by the pump, conveying the DTRO concentrated water into an evaporation pretreatment system 7 for softening treatment, conveying the treated concentrated water to an evaporation crystallization system 8 by a feed pump for evaporation treatment, collecting and reusing condensed water of the evaporated produced water, collecting and disposing miscellaneous salts generated by evaporation, conveying the evaporated mother liquor to a mother liquor drying system 9 for drying treatment, and externally conveying miscellaneous salts generated by the drying system for disposal; chemical sludge generated by the DTRO pretreatment system 2 and the evaporation pretreatment system 7 flows into a temporary sludge storage tank 10 by gravity, is conveyed to a sludge concentration tank 11 by a pump, is kept stand to remove supernatant, and is lifted to a sludge disposal system 12 for dehydration. For coking strong brine treatment after biochemical treatment, strong brine of the system firstly enters a DTRO pretreatment system 2, and enters a DTRO membrane concentration system 4 after the hardness and alkalinity of raw water are removed, so that the cleaning frequency of DTRO membrane concentration is reduced, and the long-term stable operation of the system is ensured; concentrated water enters the DTRO membrane concentration system 4 for reduction treatment, the water yield can reach more than 80 percent, the treatment capacity of the evaporative crystallization system 8 is greatly reduced, and the system investment cost is reduced; the DTRO concentrated water firstly enters an evaporation pretreatment system 7 for hardness removal, silicon removal and fluorine removal treatment, and then enters an evaporation crystallization system 8, evaporation condensate water is recycled, and evaporation crystal salt is recycled and transported to be disposed, so that near zero emission of coking wastewater is realized.
More specifically, the coking strong brine after biochemical treatment in a certain steel mill is subjected to advanced treatment by using the near zero discharge system for deeply treating the coking strong brine to obtain qualified produced water. The water treatment amount of the system is 25m3/h, and the main parameters of the inlet water quality of the concentrated brine are shown in the table 1:
TABLE 1 quality of the incoming strong brine
| Serial number | Index (I) | Numerical value | Unit of | Serial number | Index (I) | Numerical value | Unit of |
| 1 | Na+ | 4458 | mg/L | 8 | Total hardness | 1260 | mg/L |
| 2 | Ca2+ | 184 | mg/L | 9 | pH | 8.1 | |
| 3 | Mg2+ | 192 | mg/L | 10 | Total salt content | 16240 | mg/L |
| 4 | Cl | 2820 | mg/L | 11 | Ammonia nitrogen | 33.6 | mg/L |
| 5 | SO4 2- | 3010 | mg/L | 12 | CODcr | 551 | mg/L |
| 6 | HCO3- | 1210 | mg/L | 13 | Suspended matter | 75 | mg/L |
| 7 | F | 100 | mg/L | 14 | all-Silicon (SiO)2) | 30 | mg/L |
The deep treatment of the concentrated brine after the biochemical treatment by using the system of the embodiment comprises the following steps:
1) the strong brine and the back washing water of the filter 3, the supernatant of the sludge concentration tank 11 and other incoming water enter the regulating tank, are subjected to conditioning under the action of a stirrer, are uniformly mixed and are conveyed to the DTRO pretreatment system 2 through a centrifugal pump.
2) The concentrated brine enters a DTRO pretreatment system 2, and is softened by adding medicaments such as lime, PFS, sodium hydroxide, sodium carbonate, PAM, high-efficiency defluorinating agent and the like, so that calcium ions, magnesium ions and fluorine in the concentrated brine are removedIons and other pollutants to make the total hardness of the softened strong brine reach 150mg/L, the concentration of fluorine ions reach 10mg/L and the total Silicon (SiO)2) The concentration reaches 20mg/L, thereby reducing the cleaning frequency and the scaling risk of the rear-end DTRO membrane concentration system 4 and ensuring that the system can stably run for a long time.
3) The softened strong brine enters a filter 3, and the concentration of suspended matters reaches 20mg/L after the suspended matters are filtered and intercepted by the filter 3. The filter 3 is provided with a backwashing pump and a backwashing fan in a matching way, and the backwashing is carried out on the fiber filter at regular intervals so as to recover the filtering function of the fiber filter.
4) The filtered strong brine enters a DTRO membrane concentration system 4, and is concentrated by a DTRO membrane to obtain produced water of 20m3H, 5m of concentrated water3The water yield reaches 80 percent. The produced water can be recycled after meeting the water quality standard of regenerated water for HG/T3923 and 2007 circulating cooling water, and the concentrated water enters the next system for treatment. Part of the produced water is used for chemical cleaning of the backwashing filter 3 and the DTRO membrane concentration system 4, so that the system is prevented from scaling and blocking.
5) The strong brine passes through a DTRO membrane concentration system 4, so that the total hardness of DTRO concentrated water, the pollutants such as fluoride ion concentration and the like are increased by 5 times, the total hardness reaches 750mg/L, the fluoride ion concentration reaches 50mg/L, the total silicon reaches 100mg/L, the direct entering of an evaporation crystallization system 8 easily causes scaling of the evaporation system, the corrosion of titanium materials and the like, the heat exchange efficiency is greatly reduced, therefore, an evaporation pretreatment system 7 is additionally arranged to carry out softening treatment on the DTRO concentrated water again, the total hardness of the concentrated water is reduced to be below 150mg/L, the fluoride ion concentration is reduced to be below 10mg/L, and the total Silicon (SiO) (the concentration of the fluoride ion and the like) is reduced to below 10mg/L2) The concentration is reduced to below 20mg/L, thereby reducing the cleaning frequency of the evaporative crystallization system. The evaporation pretreatment system 7 also adopts a high-density sedimentation tank and a magnetic flocculation technology, so that the softening treatment effect is improved.
6) The softened concentrated water enters an evaporation crystallization system 8, the concentrated water is evaporated and concentrated to obtain mixed salt with the water content of 5% after being centrifuged by a centrifuge, the mixed salt is transported outside after being collected and is evaporated to generate about 4m3The/h condensed water is conveyed to a DTRO water production tank for recycling, the evaporation mother liquor after centrifugation by a centrifuge contains high-concentration COD, and a part of the evaporation mother liquor needs to be periodically discharged until the mother liquor is driedThe system 9 performs a drying process.
7) And drying the evaporation mother liquor by a mother liquor drying system 9 to obtain dried miscellaneous salt, transporting the dried miscellaneous salt for disposal, spraying and washing the COD containing ammonia nitrogen and light components in the obtained waste gas by a washing tower, and discharging the waste gas into the atmosphere after reaching the standard.
8) The DTRO pretreatment system 2 and the evaporation pretreatment system 7 generate sludge with the water content of 97%, the sludge flows to the temporary sludge storage tank 10 by gravity, then the sludge is conveyed to the sludge concentration tank 11 by the sludge conveying pump for concentration and precipitation, the water content of the sludge reaches 95%, the sludge is conveyed to the belt filter press by the sludge screw pump for sludge treatment, and the sludge with the water content of less than 70% is obtained and then is transported out for treatment.
Although the utility model has been described in detail above with reference to a general description and specific examples, it will be apparent to one skilled in the art that modifications or improvements may be made thereto based on the utility model. Accordingly, such modifications and improvements are intended to be within the scope of the utility model as claimed.
Claims (10)
1. A near zero emission system for deeply treating coking strong brine is characterized by comprising a regulating pond system (1), a DTRO pretreatment system (2), a filter (3), a DTRO membrane concentration system (4), a water production tank (5), a concentrated water tank (6), an evaporation pretreatment system (7), an evaporation crystallization system (8), a mother liquor drying system (9), a sludge temporary storage pond (10), a sludge concentration pond (11) and a sludge disposal system (12); wherein the regulating pond system (1), the DTRO pretreatment system (2), the filter (3), the DTRO membrane concentration system (4), the concentrated water tank (6), the evaporation pretreatment system (7), the evaporation crystallization system (8) and the mother liquor drying system (9) are communicated in sequence; the DTRO pretreatment system (2) and the evaporation pretreatment system (7) are both communicated with a temporary sludge storage tank (10); the temporary sludge storage tank (10), the sludge concentration tank (11) and the sludge disposal system (12) are communicated in sequence; the filter (3) and the sludge concentration tank (11) are communicated with the regulating tank system (1).
2. The near-zero emission system for the advanced treatment of coking brine according to claim 1 is characterized in that the filter (3) is provided with a backwash water outlet through which the filter (3) communicates with the conditioning pond system (1).
3. The near zero emission system for the advanced treatment of coking brine according to claim 1 is characterized in that the water production tank (5) is communicated with the filter (3).
4. The near-zero emission system for deeply treating coking strong brine according to claim 1, characterized in that the regulating pond system (1) comprises a regulating pond and a stirrer, and the stirrer is arranged inside the regulating pond.
5. The near zero emission system of claim 4, wherein the agitator is a submersible agitator or a top-feed agitator.
6. The near-zero emission system for deeply treating coking concentrated brine according to claim 1, characterized in that the evaporative crystallization system (8) is a triple effect evaporative crystallization system.
7. The near-zero emission system for deeply treating coking concentrated brine according to claim 1, characterized in that the mother liquor drying system (9) comprises a roller scraper dryer, wherein a miscellaneous salt outlet of the roller scraper dryer is connected with a miscellaneous salt collecting device, and a waste gas outlet of the roller scraper dryer is connected with a waste gas treatment system.
8. The near zero emission system for deep treatment of coking brine according to claim 1 is characterized in that the filter (3) is a fiber filter; the fiber filter is characterized in that a filter unit is arranged in the tank body of the fiber filter, and the filter unit comprises a fiber bundle.
9. The near-zero emission system for deeply treating coking strong brine according to claim 1, characterized in that the DTRO pretreatment system (2) and the evaporation pretreatment system (7) are both provided with a high-density sedimentation tank, and the high-density sedimentation tank is provided with a reaction zone, a flocculation zone and a sedimentation zone.
10. The near zero emission system for deeply treating coking strong brine according to claim 1, characterized in that the DTRO membrane concentration system (4) comprises a DTRO cartridge filter, a DTRO membrane module and a DTRO cleaning device, wherein the DTRO cartridge filter is a cartridge filter, and the DTRO membrane module comprises a high-pressure pump, a circulating pump, a DTRO membrane column, a product water tank and a concentrated water tank; the DTRO cleaning device comprises an alkaline washing dosing tank and an acid washing dosing tank.
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