CN115947471A - Treatment process for standard-reaching recycling of semi-coke wastewater - Google Patents
Treatment process for standard-reaching recycling of semi-coke wastewater Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
The invention relates to the technical field of wastewater treatment, in particular to a treatment process for standard-reaching recycling of semi-coke wastewater. The treatment process for recycling the carbon wastewater after reaching the standard comprises the following steps: the semi-coke wastewater enters a gravity oil separation tank to remove heavy oil and floating oil; then adding a demulsifier, a coagulant and the like for coagulation reaction, and then further removing oil by a ceramic membrane filter. And (4) performing extraction dephenolization and deamination treatment on the effluent after coagulation treatment. The deamination effluent is adjusted to be neutral in pH and then enters a biochemical treatment system which comprises a hydrolysis acidification pool, an anoxic pool and an aerobic pool. And finally, the effluent of the biochemical system enters an ozone oxidation tower and an MBR tank for advanced treatment. The invention makes the semi-coke waste water reach the recycling standard by the combination of the process sections and the control of the operation parameters, and has relatively low cost.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a treatment process for standard-reaching reuse of semi-coke wastewater.
Background
The semi-coke industry in China develops rapidly, the annual output reaches 5000 ten thousand tons, and the annual production wastewater is 830 ten thousand tons. The semi-coke waste water is mainly from the low-temperature carbonization process, the coal gas purification and the semi-coke steam quenching process of low metamorphic coal. The carbonization furnace adopted by semi-coke enterprises mainly uses an internal heating type vertical furnace, tar and water generated by the production process are difficult to separate, the COD of the wastewater is 30000-40000 mg/L, the total oil content is 1200-2000 mg/L, the content of volatile phenol is 3000-5000 mg/L, and the ammonia nitrogen content is 2000-5000 mg/L. The pollutant composition of the semi-coke wastewater is similar to that of coking wastewater, but the mass concentration of various pollutants in the semi-coke wastewater is about 10 times higher than that of the coking wastewater. The organic matter components in the semi-coke wastewater mainly comprise phenolic substances, coal tar substances, polycyclic aromatic compounds, heterocyclic compounds containing nitrogen, oxygen and sulfur, and the like. This results in high toxicity and difficult degradation of the semi-coke wastewater, which cannot be directly treated by biological methods. At present, the main treatment process of semi-coke wastewater is a combined process of oil removal, dephenolization, ammonia removal and biochemistry. The biological toxicity of the wastewater is reduced by the phenol-removing and ammonia-removing pretreatment process, but the biodegradability of the pretreated effluent is not high, so that the effluent of the biochemical process in actual operation cannot reach the standard. The semi-coke wastewater is researched and treated by using advanced oxidation technologies such as catalytic wet oxidation, electrochemical oxidation, fenton oxidation, ozone oxidation and the like, and although good treatment effect can be ensured, the operation cost is high, and the semi-coke wastewater is difficult to bear by production enterprises.
Disclosure of Invention
In order to solve the technical problem, the invention provides a treatment process for standard-reaching reuse of semi-coke wastewater, which comprises the following steps: : the semi-coke wastewater enters a gravity oil separation tank to remove heavy oil and floating oil; then adding a demulsifier, a coagulant and the like for coagulation reaction, and then further removing oil by a ceramic membrane filter. And (4) performing extraction dephenolization and deamination treatment on the coagulation treatment effluent. The deamination effluent is adjusted to be neutral in pH and then enters a biochemical treatment system which comprises a hydrolysis acidification pool, an anoxic pool and an aerobic pool. And finally, the effluent of the biochemical system enters an ozone oxidation tower and an MBR tank for advanced treatment. The method ensures that the semi-coke wastewater reaches the recycling standard through process section combination and operation parameter control, and has relatively low cost.
Preferably, the following components: the pretreatment system comprises a gravity oil separation tank, a coagulation ceramic membrane filter, a dephenolization tower, a deamination tower, a gravity oil separation tank, a coagulation ceramic membrane filter, a dephenolization tower and a deamination tower which are sequentially communicated from front to back; the gravity oil separation tank realizes oil-water separation through the action of gravity, and removes heavy oil and light oil in the wastewater; adding a demulsifier and a coagulant into the effluent of the gravity oil separation tank to perform coagulation reaction; the ceramic membrane filter is used for filtering the coagulated wastewater; the dephenolizing tower is used for carrying out extraction dephenolizing treatment on the filtered wastewater; and (3) adjusting the pH of the wastewater after dephenolization treatment, and then introducing the wastewater into a deamination tower, wherein the deamination tower is used for removing high-concentration ammonia nitrogen to obtain effluent of the pretreatment system.
Preferably: adding demulsifier dilute sulfuric acid in the coagulation process, and controlling the pH value to be 3-6; the coagulant is PAC and the addition amount is 100-500mg/L.
Preferably: the volume ratio of extraction oil to water in the extraction dephenolization is 1:5-1:7, the extraction stage number is at least 2, and the concentration of the volatile phenol in the effluent is ensured to be less than 300mg/L.
Preferably: the ammonia-removing tower comprises an ammonia still and an air stripping tower, waste water is heated to 90 ℃ and then enters the ammonia still, and water discharged from the ammonia still enters the air stripping tower, wherein the water inlet temperature of the air stripping tower is 60-70 ℃, and the gas-liquid ratio is 1500-2500.
Preferably: the biochemical treatment system includes: a hydrolysis acidification tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank; the hydrolysis acidification tank, the aerobic tank, the anoxic tank and the secondary sedimentation tank are communicated in sequence; the effluent of the pretreatment system is firstly adjusted to be neutral in pH value and then enters a hydrolysis acidification pool, and macromolecular organic matters which are difficult to degrade are decomposed into micromolecular organic matters; the hydrolysis acidification effluent enters an anoxic tank and an aerobic tank in sequence; the waste water is subjected to mineralization reaction of organic matters and nitration reaction of ammonium radicals in the aerobic tank, the mixed solution in the aerobic tank flows back to the anoxic tank, and nitrate radicals are reduced into molecular nitrogen under the denitrification effect of heterotrophic bacteria under the anoxic condition. The secondary sedimentation tank is used for separating mud and water of the mixed liquid.
Preferably: the residence time of the hydrolytic acidification tank is 10 to 20 hours, the residence time of the anoxic tank is 10 to 20 hours, and the residence time of the aerobic tank is 10 to 20 hours; the reflux ratio of the mixed liquid in the secondary sedimentation tank is 2-3, and the reflux ratio of the sludge is 0.5-1.
Preferably: the advanced treatment system comprises a high-density sedimentation tank, an ozone oxidation tower and an MBR tank; the high-density sedimentation tank, the ozone oxidation tower and the MBR tank are sequentially communicated; the high-density sedimentation tank carries out coagulation reaction by adding a coagulant PFS and quickly realizes mud-water separation; the high-density sedimentation tank is divided into three areas, namely a coagulation area, a flocculation area and a sedimentation area. The ozone oxidation tower is used for carrying out ozone oxidation on the effluent of the high-density sedimentation tank, so that the biological interpretability is improved. Finally, performing biological degradation by using an MBR tank.
Preferably, the following components: the coagulation reaction time of the high-density sedimentation tank is 8-12min, and the sludge circulation rate is 5% -10%.
Preferably: the adding amount of ozone in the ozone oxidation tower is 100-200mg/L, and the reaction time is 30-60min; the residence time of the MBR tank is 4-8 hours.
The invention has the technical effects and advantages that: 1. the invention can be matched with each other by carrying out coagulation reaction and ceramic membrane filtration after the oil separation process section, and coordinates and promotes the removal rate of oil to be more than 97 percent.
2. The invention controls the content of phenol in the water discharged from the dephenolizing tower to be less than 300mg/L by multi-stage extraction dephenolization, and reduces the impact and influence on a subsequent biochemical treatment system.
3. In the deamination process, the ammonia nitrogen is reduced to 600mg/L by the ammonia distillation tower, and then reduced to 200mg/L by the stripping tower, so that the operating cost of deamination is reduced.
4. The invention adopts a high-density sedimentation tank to treat the effluent of the biochemical treatment system to remove macromolecular refractory organic matters. Part of sludge in the high-density sedimentation tank flows back to a flocculation zone (the high-density sedimentation tank is divided into three zones, namely a coagulation zone, a flocculation zone and a sedimentation zone) from the sedimentation zone in a central reaction cylinder so as to maintain higher sludge concentration required by flocculation, reduce the consumption of a coagulant, and have high treatment efficiency and good effluent effect.
5. The invention adopts ozone-MBR to deeply treat semi-coke wastewater. Ozone oxidation improves the biodegradability of wastewater by adding low-dose ozone, and then the wastewater enters MBR for biological treatment. The wastewater treatment reaches the recycling standard at lower cost.
Drawings
FIG. 1 is a flow chart of a treatment process for standard-reaching recycling of semi-coke wastewater provided by the invention.
Detailed Description
The invention is described in further detail below with reference to the drawings and the detailed description. The embodiments of the present invention have been presented for purposes of illustration and description, and are not intended to be exhaustive or limited to the invention in the form disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art. The embodiment was chosen and described in order to best explain the principles of the invention and the practical application, and to enable others of ordinary skill in the art to understand the invention for various embodiments with various modifications as are suited to the particular use contemplated.
Example 1
Referring to fig. 1, in this embodiment, a treatment process for standard-reaching recycling of semi-coke wastewater is provided, in this embodiment, semi-coke wastewater of a certain coal chemical industry enterprise is used, and the water quality includes: COD:35000mg/L, oil: 2000mg/L, volatile phenol: 4000mg/L, ammonia nitrogen: 5000mg/L, and the balance of water, and specific trace components are not described in detail.
The method comprises the following steps: the semi-coke wastewater is pumped into a gravity oil separation tank in a pretreatment system, the semi-coke wastewater is layered into heavy oil, light oil and wastewater under the action of gravity, and the light oil layer and the heavy oil layer on the upper layer are discharged by shunting, so that the heavy oil and the light oil of the wastewater are removed. Adding sulfuric acid as demulsifier and PAC as coagulant into the rest waste water for coagulation reaction, wherein the addition amount of PAC as coagulant is 100mg/L. And (3) filtering the coagulated wastewater by a ceramic membrane filter, and adding acid (such as hydrochloric acid) into the wastewater after filtering to control the pH value of the wastewater to be 3. The filtered wastewater is directly subjected to extraction dephenolization without adjusting the pH value, the extraction agent is selected from MIBK (methyl isobutyl ketone), the volume ratio of extracted oil to water is 1:5, and the extraction stages are 2 stages. And after dephenolization treatment, adjusting the pH of the wastewater to 9, simultaneously performing heat exchange on the wastewater to 90 ℃, and then feeding the wastewater into an ammonia still to treat the wastewater until the ammonia nitrogen concentration is about 600 mg/L. And then, the wastewater enters an air stripping tower for treatment, wherein the water inlet temperature of the air stripping tower is 60 ℃, and the gas-liquid ratio is 1500.
Finally obtaining the effluent of the pretreatment system after the treatment of the first step. Detecting the effluent quality of the pretreatment system to obtain the effluent quality of the pretreatment system: COD:4000mg/L, oil: 100mg/L, volatile phenol: 350mg/L, ammonia nitrogen: 250mg/L.
Step two: adjusting the pH value of the effluent of the pretreatment system to be neutral, entering a biochemical treatment system, and entering a hydrolysis acidification tank. In the hydrolysis acidification tank, macromolecular organic matters in the effluent of the pretreatment system are decomposed into micromolecular organic matters, the residence time of the hydrolysis acidification tank is 10 hours, and then the decomposed wastewater sequentially enters the anoxic tank and the aerobic tank. The waste water is subjected to mineralization reaction of organic matters and nitration reaction of ammonium radicals in an aerobic tank, mixed liquor in the aerobic tank flows back to an anoxic tank, nitrate radicals are reduced to molecular nitrogen under the denitrification effect of heterotrophic bacteria under the anoxic condition, the retention time of the anoxic tank is 10 hours, and the retention time of the aerobic tank is 10 hours. And (3) the treated wastewater enters a secondary sedimentation tank, the wastewater is subjected to mixed sedimentation to obtain biochemical waste liquid, the reflux ratio of mixed liquid in the secondary sedimentation tank is 2, and the reflux ratio of sludge is 0.5. Finally obtaining the biochemical waste liquid.
Treating the effluent quality through the second step: COD:800mg/L, oil: 60mg/L, volatile phenol: 100mg/L, ammonia nitrogen: 20mg/L.
Step three: the biochemical waste liquid enters a high-density sedimentation tank, wherein the adding amount of a coagulant PFS is 300mg/L for secondary coagulation, the coagulation reaction time is 8min, and the sludge circulation rate is 5 percent. And (3) enabling the wastewater to flow out of the high-density sedimentation tank and enter an ozone oxidation tower, wherein the adding amount of ozone is 100mg/L, and the reaction time is 30min. And (4) allowing the wastewater after ozone oxidation to enter an MBR tank for aerobic reaction, and staying for 4 hours. Finally, the recovery liquid is obtained.
Treating the effluent quality through the third step: COD:200mg/L, oil: 10mg/L, volatile phenol: 6mg/L, ammonia nitrogen: 20mg/L. The effluent completely meets the water quality requirements of coking production wastewater for coal washing, coke quenching, blast furnace slag flushing and the like after treatment in GB 16171-2012.
Example 2
The embodiment provides a treatment process for standard-reaching recycling of semi-coke wastewater, and the semi-coke wastewater of a certain coal chemical industry enterprise is adopted in the embodiment, and the components of the water quality of the semi-coke wastewater comprise: COD:35000mg/L, oil: 2000mg/L, volatile phenol: 4000mg/L, ammonia nitrogen: 5000mg/L, and the balance of water, and specific trace components are not described in detail.
The method comprises the following steps: the semi-coke wastewater is pumped into a gravity oil separation tank in a pretreatment system, the semi-coke wastewater is layered into heavy oil, light oil and wastewater under the action of gravity, and the light oil layer and the heavy oil layer on the upper layer are discharged by shunting, so that the heavy oil and the light oil of the wastewater are removed. Adding sulfuric acid as a demulsifier, a PAC coagulant and the like into the residual wastewater for coagulation reaction, wherein the addition amount of the PAC coagulant is 300mg/L. And (3) filtering the coagulated wastewater by a ceramic membrane filter, and adding acid (such as hydrochloric acid) into the wastewater after filtering to control the pH value of the wastewater to be 4.5. The filtered wastewater is directly subjected to extraction dephenolization without adjusting the pH value, the extraction agent is selected from MIBK (methyl isobutyl ketone), the volume ratio of extracted oil to water is 1:6, and the extraction stages are 2 stages. And after dephenolization treatment, adjusting the pH value of the wastewater to 10, simultaneously performing heat exchange on the wastewater to 90 ℃, and then feeding the wastewater into an ammonia still to treat the wastewater until the ammonia nitrogen concentration is about 600 mg/L. And then the wastewater enters an air stripping tower for treatment, wherein the water inlet temperature of the air stripping tower is 65 ℃, and the gas-liquid ratio is 2000.
And finally obtaining the effluent of the pretreatment system after the treatment of the step one. Detecting the effluent quality of the pretreatment system to obtain the effluent quality of the pretreatment system: COD:3600mg/L, oil: 50mg/L, volatile phenol: 200mg/L, ammonia nitrogen: 150mg/L.
Step two: adjusting the pH value of the effluent of the pretreatment system to be neutral, entering a biochemical treatment system, and entering a hydrolysis acidification tank. In the hydrolysis acidification tank, macromolecular organic matters in the effluent of the pretreatment system are decomposed into micromolecular organic matters, the residence time of the hydrolysis acidification tank is 16 hours, and then the decomposed wastewater sequentially enters the anoxic tank and the aerobic tank. The waste water is subjected to mineralization reaction of organic matters and nitration reaction of ammonium radicals in an aerobic tank, mixed liquor in the aerobic tank flows back to an anoxic tank, nitrate radicals are reduced to molecular nitrogen under the denitrification effect of heterotrophic bacteria under the anoxic condition, the retention time of the anoxic tank is 16 hours, and the retention time of the aerobic tank is 16 hours. And (3) the treated wastewater enters a secondary sedimentation tank, and the wastewater is mixed and precipitated to obtain biochemical waste liquid, wherein the reflux ratio of mixed liquid in the secondary sedimentation tank is 2.5, and the reflux ratio of sludge is 0.8. Finally obtaining the biochemical waste liquid.
Treating the effluent quality through the second step: COD:600mg/L, oil: 10mg/L, volatile phenol: 35mg/L, ammonia nitrogen: 5mg/L.
Step three: the biochemical waste liquid enters a high-density sedimentation tank, wherein the adding amount of a coagulant PFS is 300mg/L for secondary coagulation, the coagulation reaction time is 10min, and the sludge circulation rate is 8%. And the wastewater flows out of the high-density sedimentation tank and enters an ozone oxidation tower, the adding amount of ozone is 150mg/L, and the reaction time is 45min. And (4) allowing the wastewater after ozone oxidation to enter an MBR (membrane bioreactor) tank for aerobic reaction, and staying for 6 hours. Finally, obtaining a recovery liquid.
Treating the effluent quality through the third step: COD:80mg/L, oil: 0.5mg/L, volatile phenol: 0.2mg/L, ammonia nitrogen: none. The effluent completely meets the water quality requirements of coking production wastewater for coal washing, coke quenching, blast furnace slag flushing and the like after treatment in GB 16171-2012.
Example 3
The treatment process for standard-reaching reuse of semi-coke wastewater is provided in the embodiment, the semi-coke wastewater of a certain coal chemical industry enterprise is adopted in the embodiment, and the components of the water quality of the semi-coke wastewater comprise: COD:35000mg/L, oil: 2000mg/L, volatile phenol: 4000mg/L, ammonia nitrogen: 5000mg/L, and the balance of water, and specific trace components are not described in detail.
The method comprises the following steps: the semi-coke wastewater is pumped into a gravity oil separation tank in the pretreatment system, the semi-coke wastewater is layered into heavy oil, light oil and wastewater under the action of gravity, and the light oil layer and the heavy oil layer on the upper layer are discharged by shunting, so that the heavy oil and the light oil of the wastewater are removed. And adding demulsifier sulfuric acid, coagulant PAC and the like into the residual wastewater for coagulation reaction, wherein the addition amount of the coagulant PAC is 500mg/L. And (3) filtering the coagulated wastewater by a ceramic membrane filter, and adding acid (such as hydrochloric acid) into the wastewater after filtering to control the pH value of the wastewater to be 6. The filtered wastewater is directly subjected to extraction dephenolization treatment without adjusting the pH value, an extraction agent is MIBK (methyl isobutyl ketone), the volume ratio of extracted oil to water is 1:7, and the extraction stages are 2 stages. And after dephenolization treatment, adjusting the pH value of the wastewater to 11, simultaneously performing heat exchange on the wastewater to 90 ℃, and then feeding the wastewater into an ammonia still to treat the wastewater until the ammonia nitrogen concentration is about 600 mg/L. And then the wastewater enters an air stripping tower for treatment, wherein the water inlet temperature of the air stripping tower is 70 ℃, and the gas-liquid ratio is 2500.
And finally obtaining the effluent of the pretreatment system after the treatment of the step one. Detecting the effluent quality of the pretreatment system to obtain the effluent quality of the pretreatment system: COD:3800mg/L, oil: 100mg/L, volatile phenol: 300mg/L, ammonia nitrogen: 200mg/L.
Step two: adjusting the pH value of the effluent of the pretreatment system to be neutral, entering a biochemical treatment system, and entering a hydrolysis acidification tank. In the hydrolysis acidification tank, macromolecular organic matters in the effluent of the pretreatment system are decomposed into micromolecular organic matters, the residence time of the hydrolysis acidification tank is 20 hours, and then the decomposed wastewater sequentially enters the anoxic tank and the aerobic tank. The waste water is subjected to mineralization reaction of organic matters and nitration reaction of ammonium radicals in the aerobic tank, the mixed solution in the aerobic tank flows back to the anoxic tank, nitrate radicals are reduced to molecular nitrogen under the denitrification effect of heterotrophic bacteria under the anoxic condition, the anoxic tank stays for 20 hours, and the aerobic tank stays for 20 hours. And (3) the treated wastewater enters a secondary sedimentation tank, the wastewater is subjected to mixed sedimentation to obtain biochemical waste liquid, and the reflux ratio of mixed liquid in the secondary sedimentation tank is 3 and the reflux ratio of sludge is 1. Finally obtaining the biochemical waste liquid.
Treating the effluent quality through the second step: COD:650mg/L, oil: 12mg/L, volatile phenol: 38mg/L, ammonia nitrogen: 7mg/L.
Step three: the biochemical waste liquid enters a high-density sedimentation tank, wherein the adding amount of a coagulant PFS is 300mg/L for secondary coagulation, the coagulation reaction time is 12min, and the sludge circulation rate is 10%. And (3) enabling the wastewater to flow out of the high-density sedimentation tank and enter an ozone oxidation tower, wherein the adding amount of ozone is 200mg/L, and the reaction time is 60min. And (4) allowing the wastewater after ozone oxidation to enter an MBR (membrane bioreactor) tank for aerobic reaction, and allowing the wastewater to stay for 8 hours. Finally, the recovery liquid is obtained.
Treating the effluent quality through the third step: COD:90mg/L, oil: 2mg/L, volatile phenol: 1mg/L, ammonia nitrogen: none. The effluent completely meets the water quality requirements of coking production wastewater for coal washing, coke quenching, blast furnace slag flushing and the like after treatment in GB 16171-2012.
By analyzing the three groups of data:
1. the invention can be matched with each other by carrying out coagulation reaction and ceramic membrane filtration after the oil separation process section, and coordinates and promotes the removal rate of oil to be more than 97 percent.
2. The invention controls the content of phenol in the water discharged from the dephenolizing tower to be less than 300mg/L by multi-stage extraction dephenolization, and reduces the impact and influence on a subsequent biochemical treatment system.
3. In the deamination process, the ammonia nitrogen is reduced to 600mg/L by the ammonia distillation tower, and then reduced to 200mg/L by the stripping tower, so that the operating cost of deamination is reduced.
4. The invention adopts a high-density sedimentation tank to treat the effluent of the biochemical treatment system to remove macromolecular refractory organic matters. Part of sludge in the high-density sedimentation tank flows back to a central reaction cylinder of a flocculation tank (the high-density sedimentation tank is divided into three areas, namely a coagulation area, a flocculation area and a sedimentation area) from the sedimentation tank so as to maintain higher sludge concentration required by coagulation, reduce the consumption of a coagulant, and have high treatment efficiency and good water outlet effect.
5. The invention adopts the ozone-MBR treatment of the effluent of the high-density sedimentation tank. Ozone oxidation improves the biodegradability of wastewater by adding low-dose ozone, and then the wastewater enters MBR for biological treatment. The wastewater treatment reaches the recycling standard at lower cost.
It is to be understood that the described embodiments are merely a few embodiments of the invention, and not all embodiments. All other embodiments, which can be derived by one of ordinary skill in the art and related arts based on the embodiments of the present invention without any creative effort, shall fall within the protection scope of the present invention. Structures, devices, and methods of operation not specifically described or illustrated herein are generally practiced in the art without specific recitation or limitation.
Claims (10)
1. The standard-reaching recycling treatment process of semi-coke wastewater is characterized by comprising the following steps of: the semi-coke wastewater enters a gravity oil separation tank to remove heavy oil and floating oil; then adding a demulsifier, a coagulant and the like for coagulation reaction, and then further removing oil by a ceramic membrane filter; performing extraction dephenolization and deamination treatment on the coagulation treatment effluent; adjusting the pH of the deamination effluent to be neutral, and then feeding the deamination effluent into a biochemical treatment system, wherein the biochemical treatment system comprises a hydrolysis acidification pool, an anoxic pool and an aerobic pool; and finally, the effluent of the biochemical system enters an ozone oxidation tower and an MBR tank for advanced treatment.
2. The treatment process for standard-reaching reuse of semi-coke wastewater according to claim 1, characterized in that the pretreatment system comprises a gravity oil separation tank, a coagulation tank, a ceramic membrane filter, a dephenolizing tower, a deaminating tower, a gravity oil separation tank, a coagulation tank, a ceramic membrane filter, a dephenolizing tower and a deaminating tower which are sequentially communicated from front to back; the gravity oil separation tank realizes oil-water separation through the action of gravity, and removes heavy oil and light oil in the wastewater; adding a demulsifier and a coagulant into the effluent of the gravity oil separation tank to perform coagulation reaction; the ceramic membrane filter is used for filtering the coagulated wastewater; the dephenolizing tower is used for carrying out extraction dephenolizing treatment on the filtered wastewater; and (3) adjusting the pH of the wastewater after dephenolization treatment, and then introducing the wastewater into a deamination tower, wherein the deamination tower is used for removing high-concentration ammonia nitrogen to obtain effluent of the pretreatment system.
3. The treatment process for standard-reaching recycling of semi-coke wastewater according to claim 2, characterized in that a demulsifier dilute sulfuric acid is added in the coagulation, and the pH value is controlled to be 3-6; the coagulant is PAC and the addition amount is 100-500mg/L.
4. The treatment process for standard-reaching reuse of semi-coke wastewater according to claim 3, wherein the volume ratio of extraction oil to water in the extraction dephenolization is 1:5-1:7, the number of extraction stages is at least 2, and the concentration of volatile phenol in effluent is ensured to be less than 300mg/L.
5. The treatment process for standard-reaching reuse of semi-coke wastewater according to claim 3, characterized in that the deamination tower comprises an ammonia still and a stripping tower, the wastewater enters the ammonia still after being heated to 90 ℃, the effluent of the ammonia still enters the stripping tower, wherein the water inlet temperature of the stripping tower is 60-70 ℃, and the gas-liquid ratio is 1500-2500.
6. The treatment process for standard-reaching recycling of semi-coke wastewater according to claim 1, wherein the biochemical treatment system comprises: the biochemical treatment system includes: a hydrolysis acidification tank, an anoxic tank, an aerobic tank and a secondary sedimentation tank; the hydrolysis acidification tank, the aerobic tank, the anoxic tank and the secondary sedimentation tank are communicated in sequence; the effluent of the pretreatment system is adjusted to be neutral in pH value and enters a hydrolysis acidification tank, and macromolecular organic matters which are difficult to degrade are decomposed into micromolecular organic matters; the hydrolysis acidification effluent enters an anoxic tank and an aerobic tank in sequence; the waste water is subjected to mineralization reaction of organic matters and nitration reaction of ammonium radicals in the aerobic tank, the mixed liquor in the aerobic tank flows back to the anoxic tank, nitrate radicals are reduced to molecular nitrogen under the denitrification effect of heterotrophic bacteria under the anoxic condition, and the secondary sedimentation tank is used for separating mud and water of the mixed liquor.
7. The treatment process for standard-reaching reuse of semi-coke wastewater as claimed in claim 6, wherein the residence time of the hydrolysis acidification tank is 10-20 hours, the residence time of the anoxic tank is 10-20 hours, and the residence time of the aerobic tank is 10-20 hours; the reflux ratio of the mixed liquid in the secondary sedimentation tank is 2-3, and the reflux ratio of the sludge is 0.5-1.
8. The treatment process for standard-reaching reuse of semi-coke wastewater according to claim 1, characterized in that the advanced treatment system comprises a high-density sedimentation tank, an ozone oxidation tower and an MBR tank; the high-density sedimentation tank, the ozone oxidation tower and the MBR tank are sequentially communicated; the high-density sedimentation tank carries out coagulation reaction by adding a coagulant PFS and quickly realizes mud-water separation; the high-density sedimentation tank is divided into three areas, namely a coagulation area, a flocculation area and a sedimentation area, and the ozone oxidation tower is used for carrying out ozone oxidation on the effluent of the high-density sedimentation tank, improving the biological interpretability and finally carrying out biological degradation by using an MBR (membrane bioreactor) tank.
9. The treatment process for standard-reaching recycling of semi-coke wastewater according to claim 8, wherein the coagulation reaction time of the high-density sedimentation tank is 8-12min, and the sludge circulation rate is 5% -10%.
10. The treatment process for standard-reaching recycling of semi-coke wastewater according to claim 8, wherein the ozone adding amount of the ozone oxidation tower is 100-200mg/L, and the reaction time is 30-60min; the residence time of the MBR tank is 4-8 hours.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116553774A (en) * | 2023-05-25 | 2023-08-08 | 长江生态环保集团有限公司 | Mixed sewage treatment method for improving biodegradability and optimizing carbon source distribution |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008022561A1 (en) * | 2006-08-17 | 2008-02-28 | Dawei Zhang | A filtration and adsorption material used in water treatment and the preparation thereof |
| CN103553269A (en) * | 2013-10-31 | 2014-02-05 | 北京清大国华环保科技有限公司 | Method and device for treating and recycling semi-coke wastewater |
| CN105060628A (en) * | 2015-08-04 | 2015-11-18 | 重庆杰润科技有限公司 | Semi-coke wastewater treatment method |
| WO2016188326A1 (en) * | 2015-05-27 | 2016-12-01 | 波鹰(厦门)科技有限公司 | Semi coke wastewater treating and regenerative recycling method |
| CN107746160A (en) * | 2017-11-28 | 2018-03-02 | 北京中科康仑环境科技研究院有限公司 | It is a kind of to be used for the processing of low temperature distillation waste water and reuse method in coal |
| CN108147612A (en) * | 2016-12-05 | 2018-06-12 | 中国科学院大连化学物理研究所 | A kind of method of dry distillation of coal wastewater treatment |
-
2022
- 2022-11-01 CN CN202211357078.XA patent/CN115947471A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008022561A1 (en) * | 2006-08-17 | 2008-02-28 | Dawei Zhang | A filtration and adsorption material used in water treatment and the preparation thereof |
| CN103553269A (en) * | 2013-10-31 | 2014-02-05 | 北京清大国华环保科技有限公司 | Method and device for treating and recycling semi-coke wastewater |
| WO2016188326A1 (en) * | 2015-05-27 | 2016-12-01 | 波鹰(厦门)科技有限公司 | Semi coke wastewater treating and regenerative recycling method |
| CN105060628A (en) * | 2015-08-04 | 2015-11-18 | 重庆杰润科技有限公司 | Semi-coke wastewater treatment method |
| CN108147612A (en) * | 2016-12-05 | 2018-06-12 | 中国科学院大连化学物理研究所 | A kind of method of dry distillation of coal wastewater treatment |
| CN107746160A (en) * | 2017-11-28 | 2018-03-02 | 北京中科康仑环境科技研究院有限公司 | It is a kind of to be used for the processing of low temperature distillation waste water and reuse method in coal |
Non-Patent Citations (1)
| Title |
|---|
| 魏亮亮等: "环境工程专业毕业设计指南 以城市排水工程设计为例", 哈尔滨工业大学出版社, pages: 216 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116553774A (en) * | 2023-05-25 | 2023-08-08 | 长江生态环保集团有限公司 | Mixed sewage treatment method for improving biodegradability and optimizing carbon source distribution |
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