CN112851048A - Semi-coke wastewater treatment method - Google Patents
Semi-coke wastewater treatment method Download PDFInfo
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- CN112851048A CN112851048A CN202110263446.3A CN202110263446A CN112851048A CN 112851048 A CN112851048 A CN 112851048A CN 202110263446 A CN202110263446 A CN 202110263446A CN 112851048 A CN112851048 A CN 112851048A
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- 238000012546 transfer Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
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- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2101/00—Nature of the contaminant
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- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C02F2101/00—Nature of the contaminant
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- C02F2101/18—Cyanides
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- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C02F2305/02—Specific form of oxidant
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Abstract
The invention relates to the technical field of wastewater treatment, in particular to a semi-coke wastewater treatment method, which comprises pretreatment, biochemical treatment and advanced treatment, wherein the pretreatment comprises the following steps: the semi-coke wastewater sequentially passes through a pH adjusting unit, an evaporation concentration unit and an ammonia blowing unit to obtain pretreated wastewater; performing biochemical treatment on the pretreated wastewater to obtain biochemical treatment wastewater; the deep treatment comprises the following steps: the biochemical treatment wastewater is treated by a heterogeneous catalytic oxidation unit to obtain reuse water. The invention removes units such as deacidification, dephenolization and deoiling, utilizes an evaporation concentration unit, controls the operating temperature to be 40-60 ℃, reduces the volatilization of phenolic substances by adjusting the pH value, retains most organic substances in concentrated solution, lightens the pressure of subsequent biochemical treatment, and can effectively solve the wall attachment and scaling phenomena of oils and organic substances at the temperature.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a semi-coke wastewater treatment method.
Background
The semi-coke wastewater is wastewater generated in the medium-low temperature carbonization (about 650 ℃) process of coal, and mainly comes from circulating water of cooling and washing coal gas and separated water in the chemical production process. Semi coke is dry distilled at low temperature, the produced tar in the production process is large, and the low molecular organic matters are more, so that the waste water contains a large amount of pollutants which are not oxidized at high temperature, the concentration of the pollutants is about 10 times higher than that of coking waste water, and the pollutants are more difficult to treat than the coking waste water.
The semi-coke wastewater has complex components and more than 300 pollutants. The inorganic pollutants mainly comprise sulfide, cyanide, ammonia nitrogen, thiocyanide and the like; the organic pollutants mainly comprise coal tar substances, polycyclic aromatic compounds, heterocyclic compounds containing nitrogen, oxygen and sulfur, and the like. As the wastewater also contains various chromogenic groups and chromogenic auxiliary group substances, the chroma of the semi-coke wastewater is up to ten thousand times. Phenols, heterocyclic compounds, ammonia nitrogen and the like contained in the wastewater can cause great harm to human beings, aquatic products and crops, and the wastewater can be discharged only after the content of pollutants reaches a certain standard after being treated.
As the semi-coke industry is late, no mature semi-coke wastewater treatment process exists at home and abroad at present, and the conventional treatment method mainly refers to coking wastewater with similar water quality. Comparison of various technical indexes and operation economic indexes shows that the biological method is an ideal method with more economic coking wastewater treatment and simpler operation management. However, because the semi-coke wastewater has poor water quality and poor biodegradability, the biological treatment is not suitable for direct use.
Therefore, the semi-coke wastewater treatment system at present generally comprises a conventional two-stage treatment.
The first-stage treatment is to recover pollutants from high-concentration wastewater, and the process comprises the steps of sealing and oil-separating, dephenolizing, ammonia distilling and the like. Generally, in the closed oil separation stage, the separation of oil, water and slag can be realized, the floating oil is periodically discharged into a recovery oil tank, the oil sludge at the bottom of the tank is periodically discharged into a sludge tank, and the wastewater is sent into a dephenolization flotation machine. And (4) sending the wastewater treated by the dephenolization flotation machine into a deamination tower to perform deamination treatment on the wastewater. The wastewater after the physicochemical pretreatment hardly reaches the standard of coke quenching reuse water, the COD and ammonia nitrogen in the wastewater are still high, the BOD 5/COD is 0.10-0.16, the biochemical difficulty is still high, and the wastewater needs to be diluted in an adjusting tank and added with nutritive salt and an inhibitor, so that the biodegradability of the wastewater is further improved.
The secondary treatment is to carry out harmless treatment on the pretreated wastewater, mainly adopts an activated sludge method, and utilizes microorganisms to treat organic pollutants which are dissolved or colloidal in the wastewater.
After the wastewater is treated, certain toxic and harmful substances (cyanide, COD, ammonia nitrogen and the like) still can not reach the national allowable discharge standard, and further advanced treatment is required. However, because the cost of advanced treatment is high, and is a disadvantage for many semi-coke enterprises, semi-coke wastewater is generally used for quenching coke after secondary treatment and even simple physicochemical pretreatment, so that toxic pollutants are converted from liquid phase to gas phase, and secondary pollution is caused to the environment.
From the whole process of semi-coke wastewater treatment, the advantages of biological treatment cannot be fully exerted without an effective materialization pretreatment technology. The physicochemical pretreatment technology has become a bottleneck of semi-coke wastewater treatment to some extent.
The conventional oil removal, dephenolization and ammonia distillation pretreatment process mostly adopts a coking wastewater treatment mode, but the concentration of related pollutants in semi-coke wastewater is far greater than that of coking wastewater, so that the conventional pretreatment process has poor treatment effect, high operation cost and large operation process fluctuation, and the effluent hardly meets the water inlet requirement of a biochemical section. The existing semi-coke wastewater treatment technology can not remove the salt in the sewage, and the treated effluent can not be directly recycled. For example, the invention patent with the publication number of CN104926030A discloses a semi-coke wastewater treatment and regeneration recycling method, which comprises the steps of tar removal, dephenolization, desulfurization and the like, the process is complex, the operation stability is poor, the effluent quality fluctuation is serious, even the effluent quality can not reach the standard, the investment and operation cost is high, and the method is not beneficial to popularization.
Disclosure of Invention
The invention provides a semi-coke wastewater treatment method for solving the problem of complex semi-coke wastewater treatment process, which comprises the steps of removing a deacidification unit, a dephenolization unit and an oil removal unit, controlling the operation temperature to be 40-60 ℃ by using an evaporation concentration unit, reducing the volatilization of phenolic substances by adjusting the pH value, retaining most organic matters in concentrated solution, relieving the pressure of subsequent biochemical treatment, and effectively solving the wall attachment and scaling phenomena of oils and organic matters at the temperature.
In order to achieve the purpose, the technical scheme of the invention is as follows:
the semi-coke wastewater treatment method comprises pretreatment, biochemical treatment and advanced treatment, wherein the pretreatment comprises the following steps: the semi-coke wastewater sequentially passes through a pH adjusting unit, an evaporation concentration unit and an ammonia blowing unit to obtain pretreated wastewater; performing biochemical treatment on the pretreated wastewater to obtain biochemical treatment wastewater; the deep treatment comprises the following steps: the biochemical treatment wastewater is treated by a heterogeneous catalytic oxidation unit to obtain reuse water.
The pretreatment can remove oil, ammonia nitrogen, phenols and other pollutants in the sewage, remove sulfides, cyanides and other toxic and harmful substances which influence biochemical treatment, and reduce salt content. The biodegradability of the system is improved, and good conditions are provided for subsequent processing units. COD in the pretreated wastewater is less than 1200mg/l, ammonia nitrogen is less than 50mg/l, sulfide is less than 1mg/l, cyanide is less than 1mg/l, and chroma and suspended matters are less than 10 mg/l.
Further, the biochemical treatment adopts an A/O-MBR process. The A/O-MBR process comprises an anaerobic tank, an aerobic tank and an MBR membrane reactor which are connected in sequence, and after most of organic matters are removed by utilizing an A/O biochemical reaction, biochemical effluent can realize the direct discharge standard of industrial wastewater. Meanwhile, the MBR membrane reactor removes most SS (suspended matters in water quality) and meets the SS standard of reuse water.
Further, the pH adjusting unit is used for adjusting the pH value of the semi-coke wastewater to 11-13, preferably 13, and converting phenolic substances in the semi-coke wastewater into sodium phenolate; before the wastewater enters an evaporation concentration unit (adopting an MVR evaporator), pH adjustment is carried out, the pH is controlled to be about 13, phenolic substances in the system are converted into sodium phenolate, and meanwhile, the pH of final effluent is maintained at 9-10, so that the ammonia blowing condition is met.
The evaporation concentration unit is used for reducing COD, phenols, oils, salinity and partial ammonia nitrogen in the semi-coke wastewater;
and the ammonia blowing unit is used for reducing ammonia nitrogen in the sewage.
Further, the evaporation concentration unit consists of a double-effect evaporator, and the evaporator is a plate-type climbing-film evaporator. Waste water is heated in the I-effect heater, material liquid is subjected to the action of a circulating pump and density difference, gas-liquid two-phase flow of materials rises at a high speed between heat exchange plates, the material liquid forms a film on the plate sheets in the flowing process and exchanges heat with heating steam, when the gas-liquid two-phase flow enters a separator, the material liquid and secondary steam are subjected to gas-liquid separation in the separator, the separated material liquid is continuously subjected to circulating heating and evaporation in the I-effect heater through the circulating pump, and partial material is conveyed to the II-effect heater through pressure difference. The waste water is heated in the II-effect heater, the feed liquid is subjected to the action of a circulating pump and density difference, the gas-liquid two-phase flow of the material rises at a high speed between the heat exchange plates, the feed liquid forms a film on the plate sheets in the flowing process and exchanges heat with heating steam, when the gas-liquid two-phase flow enters the separator, the feed liquid and secondary steam are subjected to gas-liquid separation in the separator, the separated feed liquid is continuously subjected to II-effect circulating heating and evaporation through the circulating pump, and the feed liquid is conveyed out of the system through the discharging pump after the concentration of the material reaches a. The evaporation condensate is the pretreated semi-coke wastewater. Cooled and discharged after passing through a subsequent ammonia blowing unit.
Further, the ammonia blowing unit adopts a stripping tower.
And further, the method also comprises sludge treatment, wherein the sludge treatment is used for directly concentrating and dehydrating the sludge generated by biochemical treatment and then sending the sludge to a coal yard.
And further, the method also comprises accident water treatment, wherein the accident water treatment is to store the semi-coke wastewater discharged in an accident state or a maintenance state by adopting an accident pool, and the semi-coke wastewater is conveyed to the pH adjusting unit by a pump with small flow after the system is stable.
Further, the heterogeneous catalytic oxidation unit adopts a catalytic oxidation tower. The catalytic oxidation tower is internally provided with a filler, and a catalyst is attached to the surface of the filler. Ozone generated by an ozone generator is used as an oxidant, the ozone is uniformly diffused into the wastewater through a gas diffuser, a gas-liquid mixture is fully contacted with a filler, and a catalyst attached to the surface of the filler catalyzes ozone molecules to generate hydroxyl radicals. The strong oxidizing property of ozone and hydroxyl free radicals is utilized to oxidize pollutants such as organic matters, ammonia nitrogen and the like in the wastewater, so that the purpose of removing the pollutants is achieved.
The heterogeneous catalytic oxidation unit is formed by combining two stages of heterogeneous catalytic oxidation units. The two-stage catalytic oxidation unit can select different operation parameters, ozone adding amount, catalytic modes and catalyst types according to the upstream incoming water quality during design.
After the catalytic oxidation advanced treatment, the water quality of the effluent can stably reach the industrial circulating cooling water quality specification GB50050 standard.
Through the technical scheme, the invention has the beneficial effects that:
1. the method has the advantages that deacidification, dephenolization and oil removal units are reduced, the evaporation concentration unit is utilized, the operation temperature is controlled to be about 40-60 ℃, the volatilization of phenolic substances is reduced through pH adjustment, most organic substances are retained in concentrated solution, the pressure of subsequent biochemical treatment is reduced, and meanwhile, the wall attachment and scaling phenomena of oils and organic substances can be effectively avoided at the temperature.
2. The water quality COD of the pretreated wastewater effluent is less than 1200 mg/l; the ammonia nitrogen is less than 50 mg/l; most of sulfide, cyanide, chroma and suspended matters in the wastewater are removed. The effluent quality is more than 80 percent better than that of the traditional pretreatment water.
3. After the quality of the pretreated effluent is improved, a modular treatment process is adopted for subsequent biochemical treatment, and the construction scale is reduced by more than 50%.
4. The pretreated effluent basically does not contain salt, and can be directly recycled after advanced treatment, so that zero discharge is realized, and zero discharge strengthening treatment and multi-stage membrane units are reduced.
Drawings
FIG. 1 is a process flow diagram of a semi-coke wastewater treatment method of the invention.
Detailed Description
The invention is further described with reference to the following figures and detailed description:
example 1
Referring to fig. 1, the semi-coke wastewater treatment method comprises accident water treatment, pretreatment, biochemical treatment, advanced treatment and sludge treatment, wherein the accident water treatment is to store semi-coke wastewater discharged in an accident state or a maintenance state by adopting an accident pool, and when a system is stable, the semi-coke wastewater is conveyed to a pH adjusting unit at a small flow rate by a pump.
The pretreatment comprises the following steps: the semi-coke wastewater sequentially passes through a pH adjusting unit, an evaporation concentration unit and an ammonia blowing unit to obtain pretreated wastewater; performing biochemical treatment on the pretreated wastewater to obtain biochemical treatment wastewater; the deep treatment comprises the following steps: the biochemical treatment wastewater is treated by a heterogeneous catalytic oxidation unit to obtain reuse water. And (4) sludge treatment, namely directly concentrating and dehydrating the sludge generated by biochemical treatment and then sending the sludge to a coal yard.
(1) The pretreatment can remove oil, ammonia nitrogen, phenols and other pollutants in the sewage, remove sulfides, cyanides and other toxic and harmful substances which influence biochemical treatment, and reduce salt content. The biodegradability of the system is improved, and good conditions are provided for subsequent processing units. COD in the pretreated wastewater is less than 1200mg/l, ammonia nitrogen is less than 50mg/l, sulfide is less than 1mg/l, cyanide is less than 1mg/l, and chroma and suspended matters are less than 10 mg/l.
a. The pH adjusting unit is used for adjusting the pH value of the semi-coke wastewater to 13, and specifically, the pH adjusting unit adopts a homogeneous adjusting reaction tank to adjust the pH of the semi-coke wastewater and convert phenolic substances in the semi-coke wastewater into phenolic sodium salts; before the wastewater enters an evaporation concentration unit (adopting an MVR evaporator), pH adjustment is carried out, the pH is controlled to be about 13, phenolic substances in the system are converted into sodium phenolate, and meanwhile, the pH of final effluent is maintained at 9-10, so that the ammonia blowing condition is met.
b. The evaporation concentration unit is used for reducing COD, phenols, oils, salinity and partial ammonia nitrogen in the semi-coke wastewater; a large amount of organic pollutants, oil and fat substances, suspended matters, phenolic substances, sulfides, cyanides, salts and part of ammonia nitrogen in the semi-coke sewage are enriched in a pre-concentration mode through an evaporation concentration unit. And separating the enriched concentrated solution from the wastewater, wherein the amount of the concentrated solution is not more than 10% of the amount of the semi-coke wastewater, and the concentrated solution is used for resource comprehensive utilization. The COD of the semi-coke wastewater separated from the concentrated solution can be reduced to below 1500mg/l, the indexes of pollutants such as petroleum, phenols, conductivity and the like are also greatly reduced, the salt content of the wastewater is low, and the biodegradability is good. The pre-concentration separation is a key treatment unit of the zero-emission treatment technology, and the pre-concentration treatment effect is the water quality guarantee of the subsequent biochemical treatment and advanced treatment of the semi-coke wastewater.
The evaporation concentration unit consists of a double-effect evaporator, and the evaporator is a plate-type climbing-film evaporator. Waste water is heated in the I-effect heater, material liquid is subjected to the action of a circulating pump and density difference, gas-liquid two-phase flow of materials rises at a high speed between heat exchange plates, the material liquid forms a film on the plate sheets in the flowing process and exchanges heat with heating steam, when the gas-liquid two-phase flow enters a separator, the material liquid and secondary steam are subjected to gas-liquid separation in the separator, the separated material liquid is continuously subjected to circulating heating and evaporation in the I-effect heater through the circulating pump, and partial material is conveyed to the II-effect heater through pressure difference. The waste water is heated in the II-effect heater, the feed liquid is subjected to the action of a circulating pump and density difference, the gas-liquid two-phase flow of the material rises at a high speed between the heat exchange plates, the feed liquid forms a film on the plate sheets in the flowing process and exchanges heat with heating steam, when the gas-liquid two-phase flow enters the separator, the feed liquid and secondary steam are subjected to gas-liquid separation in the separator, the separated feed liquid is continuously subjected to II-effect circulating heating and evaporation through the circulating pump, and the feed liquid is conveyed out of the system through the discharging pump after the concentration of the material reaches a. The evaporation condensate is the pretreated semi-coke wastewater. Cooled and discharged after passing through a subsequent ammonia blowing unit.
c. And the ammonia blowing unit is used for reducing ammonia nitrogen in the sewage. The ammonia blowing unit adopts a stripping tower. The ammonia nitrogen is mainly ammonium ion (NH) in the wastewater4+) And free ammonia (NH)3) The state exists, and the equilibrium relationship is shown as NH3+H2O—NH4+ +OH- This relationship is influenced by the pH, which when high shifts the equilibrium to the left and the proportion of free ammonia increases. At room temperature, most of ammonia nitrogen exists in the state of ammonium ion at pH of about 7, and ammonia nitrogen exists in the state of ammonium ion at pH of about 11The ammonia separation is approximately 98%. The dissociation rate (%) of ammonia nitrogen at different pH and temperature is such that ammonia in a free state is easily released when the pH value of water is increased. If physical actions such as stirring and aeration are performed, the ammonia can be further promoted to overflow from the water. In practical engineering, a deamination tower is mostly adopted. The stripping tower is generally constructed by adopting a gas-liquid contact device, and filling materials in the tower to improve the contact area. The water after adjusting the pH value is sprinkled on the filler from the upper part of the tower to form water drops which fall down along the clearance of the filler in turn and are contacted with the compressed air from the bottom of the tower to the top by a fan in a counter-current way to finish the mass transfer process, so that the ammonia is converted from a liquid phase to a gas phase and is discharged along with the compressed air to finish the stripping process. The deamination tower has simple structure, small occupied area and stable ammonia nitrogen removal effect, and the generated by-product ammonium sulfate or ammonia water can bring certain economic benefit. The deamination process also has a certain effect of removing volatile phenol in the sewage. The ammonia nitrogen of the effluent of the pre-concentration unit is about 1000mg/l, the remaining 90% of ammonia nitrogen can be removed through deamination treatment, and the ammonia nitrogen of the effluent is 80-150 mg/l.
(2) The biochemical treatment adopts an A/O-MBR process. After most of organic matters are removed by utilizing A/O biochemical reaction, the biochemical effluent can realize the direct discharge standard of industrial wastewater. Meanwhile, the MBR membrane reactor removes most SS (suspended matters in water quality) and meets the SS standard of reuse water. The A/O-MBR process comprises an anaerobic tank, an aerobic tank and an MBR membrane reactor which are connected in sequence, wherein one part of sludge generated by the MBR membrane reactor flows back to the anaerobic tank, and the other part of sludge enters a sludge storage tank.
(3) The heterogeneous catalytic oxidation unit adopts a catalytic oxidation tower. The catalytic oxidation tower is internally provided with a filler, and a catalyst is attached to the surface of the filler. Ozone generated by an ozone generator is used as an oxidant, the ozone is uniformly diffused into the wastewater through a gas diffuser, a gas-liquid mixture is fully contacted with a filler, and a catalyst attached to the surface of the filler catalyzes ozone molecules to generate hydroxyl radicals. The strong oxidizing property of ozone and hydroxyl free radicals is utilized to oxidize pollutants such as organic matters, ammonia nitrogen and the like in the wastewater, so that the purpose of removing the pollutants is achieved.
The heterogeneous catalytic oxidation unit is formed by combining two stages of heterogeneous catalytic oxidation units. The two-stage catalytic oxidation unit can select different operation parameters, ozone adding amount, catalytic modes and catalyst types according to the upstream incoming water quality during design.
After the catalytic oxidation advanced treatment, the water quality of the effluent can stably reach the industrial circulating cooling water quality specification GB50050 standard.
(4) And the sludge treatment is used for directly concentrating and dehydrating the sludge generated in the biochemical treatment stage and then sending the sludge to a coal yard. And an excess sludge pump is arranged to send excess sludge in the biochemical treatment stage to a sludge concentration tank, the sludge discharged after concentration flows into a sludge storage tank by gravity, and a mixing stirrer is arranged in the tank. And (4) conditioning the sludge in the sludge storage tank, pumping the conditioned sludge to a screw-stacking dehydrator for dehydration, and delivering the dehydrated sludge to a coal yard for disposal. And discharging the pressure filtrate generated in the dehydration process to an anaerobic tank for retreatment. The spiral shell overlapping dehydrator is simple in structure, easy to operate, stable in effect, large in filtering driving force, low in water content of obtained filter cakes, strong in adaptability to materials and suitable for various kinds of sludge. The system has low power consumption and low operating cost. The water content of the dewatered mud cake can be reduced to 80-85%.
The on-way removal rate of the semi-coke wastewater in each treatment stage is shown in table 1.
TABLE 1 Rate table for on-way removal of semi-coke wastewater at each treatment stage
The above-mentioned embodiments are merely preferred embodiments of the present invention, which are merely illustrative and not restrictive, and it should be understood that other embodiments may be easily implemented by those skilled in the art by means of replacement or modification according to the technical contents disclosed in the specification, and therefore, all changes and modifications that come within the spirit and technical conditions of the present invention should be included in the claims of the present invention.
Claims (10)
1. The semi-coke wastewater treatment method comprises pretreatment, biochemical treatment and advanced treatment, and is characterized in that the pretreatment comprises the following steps: the semi-coke wastewater sequentially passes through a pH adjusting unit, an evaporation concentration unit and an ammonia blowing unit to obtain pretreated wastewater; performing biochemical treatment on the pretreated wastewater to obtain biochemical treatment wastewater; the deep treatment comprises the following steps: the biochemical treatment wastewater is treated by a heterogeneous catalytic oxidation unit to obtain reuse water.
2. The semi-coke wastewater treatment method according to claim 1, wherein the biochemical treatment is an A/O-MBR process.
3. The semi-coke wastewater treatment method according to claim 1, wherein the pH adjustment unit is used for adjusting the pH value of the semi-coke wastewater to 11-13 and converting phenolic substances in the semi-coke wastewater into phenolic sodium salts;
the evaporation concentration unit is used for reducing COD, phenols, oils, salinity and partial ammonia nitrogen in the semi-coke wastewater;
and the ammonia blowing unit is used for reducing ammonia nitrogen in the sewage.
4. The semi-coke wastewater treatment method according to claim 3, wherein the pH value is adjusted to 13.
5. The semi-coke wastewater treatment method according to claim 3, wherein the evaporation concentration unit is composed of a two-effect evaporator, and the evaporator is a plate-type rising-film evaporator.
6. The semi-coke wastewater treatment method according to claim 3, wherein the ammonia blowing unit adopts a stripping tower.
7. The semi-coke wastewater treatment method according to claim 1 or 3, wherein the temperature of the evaporation concentration unit is 40-60 ℃.
8. The semi-coke wastewater treatment method according to claim 1, further comprising sludge treatment, wherein the sludge treatment is used for directly concentrating and dewatering the sludge generated by biochemical treatment and then sending the sludge to a coal yard.
9. The semi-coke wastewater treatment method according to claim 1, further comprising accident water treatment, wherein the accident water treatment is to store semi-coke wastewater discharged in an accident state or a maintenance state by using an accident pond, and the semi-coke wastewater is conveyed to the pH adjusting unit by a small flow rate by using a pump after the system is stabilized.
10. The semi-coke wastewater treatment method according to claim 1, wherein the heterogeneous catalytic oxidation unit adopts a catalytic oxidation tower.
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