CN214990975U - Wastewater treatment system - Google Patents
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- CN214990975U CN214990975U CN202120608453.8U CN202120608453U CN214990975U CN 214990975 U CN214990975 U CN 214990975U CN 202120608453 U CN202120608453 U CN 202120608453U CN 214990975 U CN214990975 U CN 214990975U
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Abstract
The utility model provides a wastewater treatment system, the waste water contains oil, phenol compounds and ammonia, processing system includes gravity deoiling unit, coalescence deoiling unit, filter unit, deacidification deamination unit, extraction dephenolization unit, first absorption unit, AO biochemical treatment unit, flocculation and precipitation filter unit and second absorption unit. The wastewater treatment system of one embodiment of the utility model can recycle oil, phenol and ammonia in wastewater, and water can be recycled; meanwhile, the operation effect of the wastewater treatment system is more stable, and the treatment cost is lower.
Description
Technical Field
The utility model relates to a wastewater treatment system, in particular to a system for treating wastewater containing oil, ammonia and phenol.
Background
In the production processes of semi-coke, coking and low-temperature and low-pressure gasification of coal, a large amount of wastewater is generated, and because the production processes are coal carbonization at low temperature (about 600-800 ℃), the generated wastewater is complex in components, contains a large amount of organic pollutants such as tar, ammonia, phenols and difficultly-degradable heterocyclic compounds, is typical high-pollution and high-toxicity industrial wastewater, and has high COD concentration. For example, the COD of the semi-coke wastewater is about 30000-50000 mg/l, the ammonia nitrogen is about 1500-4000 mg/l, the volatile phenol is about 5000-7000 mg/l, the total phenol is about 6000-10000 mg/l, the petroleum is about 300-2000 mg/l, and the COD, ammonia nitrogen and phenol of the coal low-temperature low-pressure gasification wastewater are also very high.
The current wastewater treatment process mainly comprises the steps of filtering wastewater by adopting a multi-medium filter after oil separation by gravity, then evaporating ammonia, extracting and dephenolizing, and then carrying out biochemical treatment, wherein the main problems are as follows:
1. because the waste water contains more emulsified oil, has complex types, light oil and heavy oil, and has density close to that of water, the ideal separation effect is difficult to achieve by a simple gravity settling separation method, the gravity settling separation needs dozens of hours, and the oil content of the effluent is still high.
2. Because of high oil content and large amount of dust, when the phenol and ammonia in the ammonia distillation tower are recovered by steam stripping and dephenolization, the internal parts of the tower are easy to block, the tower plate is easy to coke, and the tower liquid is frequent in the operation process of the ammonia distillation tower and the like. The crude phenol product is not qualified.
3. The waste water contains high phenol, the phenol types are complex, the content of polyphenol is also higher, the phenol content in the effluent water is still higher after the extraction dephenolization treatment, about 1000mg/l, the high-concentration phenol has strong toxic action on the biochemical treatment, and the operation fluctuation of an extraction dephenolization system can cause serious influence and impact on the biochemical treatment system.
4. The waste water contains more heterocyclic compounds which are difficult to biodegrade, and even though effective biochemical treatment is carried out, the effluent water of the waste water can hardly meet the water quality index requirement of the water for quenching coke in the national standard. Let alone meet the standards for direct emissions.
5. The prior extraction dephenolization process has the defects of high equipment investment, large extractant loss, high treatment cost, large occupied area and the like.
SUMMERY OF THE UTILITY MODEL
A primary object of the present invention is to provide a wastewater treatment system, the wastewater contains oil, phenolic compounds and ammonia, the treatment system comprises:
the gravity oil removal unit is used for removing at least part of heavy oil, floating oil and suspended matters in the wastewater through standing layering treatment;
the coalescence deoiling unit is used for removing at least part of emulsified oil and suspended matters in the effluent of the gravity deoiling unit;
the filtering unit is used for filtering the effluent of the coalescence deoiling unit;
the deacidification and deamination unit is used for carrying out deacidification and deamination treatment on the effluent of the filtering unit so as to remove at least part of acidic compounds and ammonia in the effluent;
the extraction and dephenolization unit is used for carrying out extraction treatment on the effluent of the deacidification and deamination unit so as to remove at least part of phenolic compounds in the effluent;
the first adsorption unit is used for carrying out adsorption treatment on the effluent of the extraction dephenolization unit so as to remove at least part of residual phenolic compounds;
the A/O biochemical treatment unit is used for performing biochemical treatment on the effluent of the first adsorption unit;
the flocculation precipitation filtering unit is used for carrying out flocculation, precipitation and filtering treatment on the effluent of the A/O biochemical treatment unit; and
and the second adsorption unit is used for carrying out adsorption treatment on the effluent of the flocculation precipitation filtering unit so as to remove at least part of heterocyclic compounds and nitrogen-containing aromatic compounds in the effluent.
According to the utility model relates to an embodiment, gravity deoiling unit coalesce deoiling unit the filter unit deacidification deamination unit the extraction dephenolization unit first adsorb the unit AO biochemical treatment unit flocculation precipitation filter unit reaches the second adsorbs the unit and links to each other in proper order.
According to the utility model discloses an embodiment gravity deoiling unit is provided with container, oil trap and the mud groove that is used for the sedimentation separation be provided with collection device in the container that is used for the sedimentation separation.
According to an embodiment of the present invention, a coalescing separator is disposed in the coalescing oil removal unit; and/or the deacidification and deamination unit is provided with a deacidification tower and a deamination tower.
According to an embodiment of the present invention, the first adsorption unit is provided with an adsorption column filled with an adsorbent capable of adsorbing phenolic compounds.
According to an embodiment of the present invention, the second adsorption/desorption unit is provided with an adsorption column filled with an adsorbent capable of adsorbing a heterocyclic compound or a nitrogen-containing aromatic compound.
According to an embodiment of the present invention, a membrane filter is disposed at the filtering unit; and/or the extraction dephenolization unit is provided with a cooler, an extraction reactor, a phase separator and an extractant regeneration tower.
According to an embodiment of the present invention, a ceramic membrane or a metal sintered membrane is disposed in the membrane filter; and/or the extraction reactor is a fiber membrane contactor.
According to an embodiment of the present invention, the wastewater treatment system further comprises a first heating unit and/or a second heating unit, wherein the first heating unit is connected to the gravity oil removal unit and the coalescence oil removal unit respectively; the second heating unit is respectively connected with the coalescence deoiling unit and the filtering unit; and/or the presence of a gas in the gas,
according to the utility model discloses an embodiment, wastewater treatment system still includes hydrolysis acidification unit, hydrolysis acidification unit respectively with first adsorption element with the biochemical treatment unit of AO links to each other.
The wastewater treatment system of one embodiment of the utility model can recycle oil, phenol and ammonia in wastewater, and water can be recycled; meanwhile, the operation effect of the wastewater treatment system is more stable, and the treatment cost is lower.
Drawings
FIG. 1 is a schematic structural view of a wastewater treatment system according to an embodiment of the present invention.
Wherein the reference numerals are as follows:
1. a gravity oil removal unit; 2. a first heating unit; 3. a coalescent oil removal unit; 4. a second heating unit; 5. a filtration unit; 6. a deacidification deamination unit; 7. an extraction dephenolization unit; 8. a first adsorption unit; 9. a hydrolysis acidification unit; 10. an A/O biochemical treatment unit; 11. a flocculation precipitation filtration unit; 12. a second adsorption unit;
A. wastewater to be treated; B. floating oil; C. settling dregs; D. suspended matter; E. an acid gas; F. containing NH3A gas; G. crude phenol; H. residual liquid; I. sludge; J. regenerating waste liquid; l, flocculating agent; m, coagulant aid; K. and (4) treating the treated wastewater.
Detailed Description
Exemplary embodiments that embody features and advantages of the present invention will be described in detail in the following description. It is to be understood that the invention is capable of other and different embodiments and its several details are capable of modification without departing from the scope of the invention, and that the description and drawings are to be regarded as illustrative in nature and not as restrictive.
Referring to fig. 1, an embodiment of the present invention provides a wastewater treatment system for treating wastewater containing oil, phenolic compounds and ammonia, the treatment system comprising:
the gravity oil removal unit 1 is used for removing part of heavy oil, floating oil and suspended matters in the wastewater through standing treatment;
the coalescence deoiling unit 3 is used for removing part of emulsified oil and suspended matters in the effluent of the gravity deoiling unit;
the filtering unit 5 is used for filtering the effluent of the coalescence deoiling unit 3;
the deacidification and deamination unit 6 is used for carrying out deacidification and deamination treatment on the effluent of the filtering unit 3 so as to remove acidic substances and ammonia in the effluent;
the extraction dephenolization unit 7 is used for extracting the effluent of the deacidification and deamination unit 6 to remove most of phenolic compounds in the effluent;
a first adsorption unit 8 (adsorption dephenolization unit) for performing adsorption treatment on the effluent of the extraction dephenolization unit 7 to remove most of the residual phenolic compounds;
the A/O biochemical treatment unit 10 is used for performing biochemical treatment on the effluent of the first adsorption unit 8 to remove most organic matters and ammonia nitrogen in the effluent;
the flocculation precipitation filtering unit 11 is used for carrying out flocculation, precipitation and filtering treatment on the effluent of the A/O biochemical treatment unit 10; and
and the second adsorption unit 12 is used for performing adsorption treatment on the effluent of the flocculation precipitation filtering unit 11 to remove organic matters in the effluent.
In one embodiment, the wastewater may be wastewater produced during semi-coke, coking, or low temperature, low pressure gasification of coal.
In one embodiment, the gravity degreasing unit 1, the coalescence degreasing unit 3, the filtering unit 5, the deacidification and deamination unit 6, the extraction and dephenolization unit 7, the first adsorption unit 8, the A/O biochemical treatment unit 10, the flocculation precipitation filtering unit 11 and the second adsorption unit 12 are connected in sequence.
During operation, wastewater is treated by the gravity oil removal unit 1, the coalescence oil removal unit 3, the filtering unit 5, the deacidification and deamination unit 6, the extraction and dephenolization unit 7, the first adsorption unit 8, the A/O biochemical treatment unit 10, the flocculation precipitation filtering unit 11 and the second adsorption unit 12 in sequence, and the treated water can reach the recycling standard.
In one embodiment, heavy oil, oil slick and suspended matter are separated from water by gravity during the standing process of the gravity oil removal unit 1, and the separated substances are further separated from water.
In one embodiment, the gravity oil removal unit 1 is provided with a container, an oil collecting tank and a sludge discharge tank which perform sedimentation separation by using gravity; the oil collecting tank is used for containing floating oil, the sludge discharging tank is used for containing sediments, and a collecting device, such as an oil and slag scraping machine, is arranged in the container for sedimentation separation. Part of the floating oil in the wastewater has a lower specific gravity than water, and part of the suspended matter and oil have a higher specific gravity than water. During operation, the wastewater is kept still for a period of time in the container for sedimentation separation, the floating oil with smaller specific gravity than water floats to the water surface under the action of gravity, and partial suspended matters and oil with larger specific gravity than water can be settled to the bottom of the container to form floating oil B and sediment C. The floating oil B and the sediment C can be respectively collected into the oil collecting tank and the sludge discharging tank through the collecting device, so that the separation of oil, slag and water is realized.
The utility model has no special limitation to the container for settling separation of the gravity oil removal unit 1, can be a common oil separation tank in the field, and has no special limitation to the material and the structural form, for example, reinforced concrete or metal can be adopted; the device for collecting the floating oil and the sediments of the utility model is not specially limited, and can be a common oil and sediment scraping machine in the field.
In one embodiment, the standing time of the wastewater in the gravity oil removal unit 1 may be 2 to 10 hours, and further may be 5 to 8 hours, so as to separate most of the floating oil and the sediments from water, and further, the standing time is too long, so that the wastewater does not occupy too large space and increase investment.
In an embodiment, the wastewater treatment system further comprises a first heating unit 2, and the first heating unit 2 is used for heating the effluent of the gravity oil removal unit 1 so as to make the wastewater reach the temperature required by the coalescence oil removal unit 3.
In one embodiment, the first heating unit 2 may be connected to the gravity degreasing unit 1 and the coalescing degreasing unit 3, respectively.
In one embodiment, the first heating unit 2 is provided with a heater and a temperature controller to heat and control the temperature of the effluent of the gravity oil removal unit 1.
The utility model discloses heater and temperature controller to first heating element 2 do not have special limitation, can adopt the common shell and tube heat exchanger and the temperature controller in this field, also do not have special limitation to heating medium, can adopt steam, hot water or electrical heating.
In one embodiment, the temperature of the wastewater to be treated entering the coalescing oil removal unit 3 may be 10-90 ℃.
In one embodiment, the temperature of the wastewater to be treated entering the coalescing oil removal unit 3 may be 40 to 80 ℃, and further may be 50 to 70 ℃, and the higher temperature is favorable for reducing the viscosity and the fluidity of oil in the wastewater to be treated, so that the oil-water separation is more favorable.
In one embodiment, the coalescing oil removal unit 3 may be connected to the gravity oil removal unit 1 or the first heating unit 2, and a coalescing material is disposed in the coalescing oil removal unit 3 to remove a part of emulsified oil and suspended substances in the wastewater to be treated by coalescence and emulsion breaking of the coalescing material.
In one embodiment, a coalescing separator, which is a separation vessel filled with a coalescing material therein, is provided in the coalescing oil removal unit 3. When the wastewater to be treated passes through the coalescence material, because the affinity of oil and water to the surface of the coalescence material is very different, the emulsified oil drops in the wastewater can be coalesced and demulsified, and the oil phase and the water phase move upwards and downwards respectively and are separated, so that the oil content in the effluent water of the coalescence oil removal unit 3 is further reduced.
In one embodiment, the oil content of the effluent of the coalescing oil removal unit 3 is less than 300mg/l, further less than 100 mg/l.
In one embodiment, the retention time of the wastewater to be treated in the coalescer is 45 to 90 minutes.
The utility model discloses do not have special limitation to the coalescence separator of coalescence deoiling unit 3, also do not have special limitation to the material and the specification of coalescence material, can adopt common coalescer and coalescence material in this field, as long as can reach water oil separating's effect can. The coalescence separator can be one-stage or multi-stage series connection, and can also adopt different coalescence materials in each stage to meet the coalescence demulsification requirements of oil drops with different properties and particle sizes, thereby achieving the best demulsification and oil-water separation effects.
In an embodiment, the wastewater treatment system further comprises a second heating unit 4 for heating the effluent of the coalescing oil removal unit 3 to bring the wastewater to a desired temperature for the filter unit 5.
In one embodiment, the second heating unit 4 may be connected to the coalescing oil removal unit 3 and the filtering unit 5 respectively.
In one embodiment, a heater and a temperature controller are disposed in the second heating unit 4 to heat and control the temperature of the effluent of the coalescing oil removing unit 3.
In one embodiment, the temperature of the outlet water of the second heating unit 4 may be 40 to 100 ℃, further 50 to 90 ℃, and further 60 to 80 ℃.
The utility model discloses heater and temperature controller to second heating element 4 do not have special limitation, can adopt the common shell and tube heat exchanger in this field, also do not have special limitation to heating medium, can adopt steam, hot water or electrical heating.
In one embodiment, the filtering unit 5 can be connected to the coalescing degreasing unit 3 or the second heating unit 4, and a filter is provided in the filtering unit 5, under the action of which most of the suspended substances D and colloids in the wastewater to be treated are intercepted and water and oil are permeated.
In one embodiment, the content of suspended matter in the effluent of the filtration unit 5 may be below 20mg/l, further may be below 10 mg/l.
The filter of the filtering unit 5 of the present invention is not particularly limited, and a medium filter or a membrane filter commonly used in the art may be used.
In one embodiment, the filter can be one or more stages connected in series, and can also be a combination of medium filtration and membrane filtration.
In one embodiment, a membrane filter is provided in the filter unit 5. The membrane filtration belongs to absolute filtration, has high filtration precision and better turbidity removal effect, and can better meet the requirements of the subsequent deacidification deamination unit 6 and the extraction dephenolization unit 7 on the content of suspended matters in the inlet water so as to prevent the units from being blocked by dirt.
The utility model discloses there is not special restriction to the filtration membrane that filter unit 5 used, can adopt common milipore filter in this field, micro-filtration membrane or have other filtration membranes of equivalent treatment effect. The utility model discloses also not have special restriction to filtration membrane's material. In one embodiment, the filtration membrane used in the filtration unit 5 is a ceramic membrane or a metal sintered membrane.
The utility model discloses also not specially limited to the filtration mode of the membrane filter of filter unit 5, can adopt dead end filtration or cross-flow filtration. In one embodiment, cross-flow filtration is adopted, and the circulation flow rate of the cross-flow filtration may be 1 to 10 times of the filtration flow rate, and more preferably 4 to 8 times.
In one embodiment, the deacidification deamination unit 6 may be connected to the filtration unit 5. The deacidification and deamination unit 6 is provided with a deacidification tower and a deamination tower which are used for removing most of H in the effluent of the filtering unit 52S、CO2Isoacidic substance and NH3. In the deacidification tower and the deamination tower, steam is adopted to carry out steam stripping treatment on the effluent of the filtering unit 5, and most of H in the wastewater is removed in the deacidification tower and the deamination tower respectively2S、CO2Isoacidic substance and NH3(ii) a Containing H2S and CO2The acid gas E is discharged from the top of the deacidification tower,the discharged acid gas E can be continuously treated; in addition, containing NH3And (4) discharging the gas F from the top of the deamination tower, and further treating and recovering ammonia in the gas F to obtain ammonia water or liquid ammonia.
In one embodiment, the H of the effluent of the deacidification deamination unit 62The S content is less than 20mg/l, and the ammonia content is less than 200 mg/l.
The utility model discloses deacidify tower and deamination tower's structural style, tower internals kind and form and the operating parameter to deacidification deamination unit 6 do not have special restriction, as long as reach equal treatment effect can.
In one embodiment, the extractive dephenolation unit 7 may be connected to the deacidification deamination unit 6. The extraction dephenolization unit 7 is provided with a cooler, an extraction reactor, a phase separator and an extractant regeneration tower. In operation, the effluent of the deacidification and deamination unit 6 is firstly cooled to a desired temperature by a cooler and then is contacted and mixed with an extracting agent in an extraction reactor, organic matters such as phenol and oil have higher solubility in the extracting agent so as to enter the extracting agent from water, and then the mixture is stood and layered in a phase separator into an extraction phase rich in phenol and oil and a water phase less in phenol and oil. And (3) regenerating the extract phase rich in the phenol in an extractant regeneration tower through steam, evaporating the extractant from the extract phase and recycling the extractant, wherein the residual substances in the extract phase without the extractant are mainly phenol and oil and are recycled as crude phenol G.
The utility model discloses do not have special restriction to the kind of the extractant of extraction dephenolization unit 7, can adopt the common ketone in this field, ether, petroleum class compound or their mixture, as long as reach equal treatment effect can.
The utility model discloses do not have special restriction to the type of the cooler of extraction dephenolization unit 7, can adopt the common shell and tube heat exchanger in this field or plate heat exchanger, as long as reach anticipated cooling effect can. In one embodiment, the cooled wastewater has a temperature of less than 40 ℃.
The utility model discloses do not have special restriction to the structural style of extraction reactor, phase separator and extractant regenerator of extraction dephenolization unit 7, as long as reach equal treatment effect can.
In one embodiment, a fiber membrane contactor is used as an extraction reactor (extraction medium carrier), and the fiber membrane contactor and a phase separator form an integrated device to provide high-efficiency mass transfer efficiency and separation effect, reduce entrainment loss of an extracting agent, and have smaller occupied area and investment of the device. The extraction reactor and the phase separator may be connected in series in one or more stages.
In one embodiment, the content of volatile phenol in the effluent of the extraction dephenolization unit 7 is less than 200mg/l, and the content of oil is less than 30 mg/l; furthermore, the content of volatile phenol is less than 100mg/l, and the content of oil is less than 10 mg/l.
In one embodiment, the first adsorption unit 8 may be connected to the extractive dephenolation unit 7. The first adsorption unit 8 is provided with an adsorption column filled with an adsorbent with selective adsorption capacity on phenolic substances, and the phenolic substances in the effluent of the extraction dephenolization unit 7 are adsorbed on the adsorbent after flowing through the adsorption column.
In one embodiment, the volatile phenol content in the effluent of the adsorption column of the first adsorption unit 8 is less than 50mg/l, and further less than 20mg/l, so that the volatile phenol content does not harm the microorganisms of the subsequent hydrolytic acidification treatment unit 9 and the A/O biochemical treatment unit 10.
In an embodiment, the first adsorption unit 8 is further provided with a desorption system, a desorption agent is arranged in the desorption system, when the adsorbent is gradually saturated, and the content of phenol in the effluent water exceeds a design index, the desorption agent can be adopted to perform desorption regeneration on the effluent water, and the regenerated adsorbent can be put into use again.
The utility model discloses do not have special limitation to first adsorption unit 8's adsorbent, can adopt the adsorption resin that the field is common or other adsorption material that have the equivalent effect, as long as these adsorption material have selective adsorption capacity to phenols. The utility model discloses also not having special limitation to the desorbent, can adopting ketone, alcohol or salt, alkali etc. as long as use these desorbents to the adsorbent regeneration back, can resume the adsorbent adsorption efficiency can.
In one embodiment, methanol is used as a desorption agent, the desorbed solvent is subjected to solvent regeneration by a rectifying tower, the solvent is rectified to obtain methanol and a tower bottom residual solution H, the methanol is recycled, and the residual solution H mainly contains water, phenol and other organic matters and can be incinerated.
In one embodiment, the wastewater treatment system further comprises a hydrolysis acidification treatment unit 9, and the hydrolysis acidification treatment unit 9 can be respectively connected with the first adsorption unit 8 and the A/O biochemical treatment unit 10. The hydrolysis acidification treatment unit 9 is used for performing hydrolysis acidification treatment on the effluent of the first adsorption unit 8 so as to improve the biodegradability of the wastewater.
In one embodiment, the hydrolysis-acidification processing unit 9 is provided with a hydrolysis-acidification tank, so that under the action of a large amount of hydrolysis bacteria and acidification bacteria in the hydrolysis-acidification tank, insoluble organic matters in the wastewater to be processed can be hydrolyzed into soluble organic matters, and macromolecular substances which are difficult to biodegrade are converted into micromolecular substances which are easy to biodegrade, thereby improving the biodegradability of the wastewater to be processed. Meanwhile, by utilizing the metabolic characteristics of anaerobic microorganisms, soluble organic matters are decomposed, metabolized and digested by anaerobic bacteria, so that the content of the organic matters in the treated wastewater is reduced, and the COD concentration in the wastewater is reduced.
The utility model discloses whether add filler and filler form etc. and all do not have special limitation in structural style, the pond to the hydrolytic acidification pond of hydrolytic acidification processing unit 9, treat that the dwell time of processing waste water in the hydrolytic acidification pond also does not have special limitation, as long as reach equal treatment effect can.
In one embodiment, the BOD of the effluent from the hydrolysis acidification unit 95The ratio of COD/COD is greater than 0.3, and further greater than 0.5.
In one embodiment, the A/O biochemical treatment unit 10 may be connected to the hydrolytic acidification treatment unit 9. The A/O biochemical treatment unit 10 is provided with an anoxic tank, an aerobic tank, a secondary sedimentation tank, a sludge reflux pump and a digestive juice reflux pump. A stirrer is arranged in the anoxic tank, and an aeration system is arranged in the aerobic tank. In the anoxic pond, denitrifying bacteria can utilize organic matters in the waste water to be treated as carbon source to carry out large amount of NO introduced from the returned mixed liquid and the returned sludge3- -N and NO2Reduction of-N to N2Released into the air, and the dissolved organic matters are absorbed by cells to ensure that BOD in the sewage5Decrease in concentration, NO3The concentration of-N is greatly reduced. In the aerobic tank, the organic matter is biochemically degraded by aerobic microorganisms, BOD5The concentration continues to decrease; the organic nitrogen is ammoniated and then nitrated to make NH3The N concentration drops significantly, but NO is produced as a result of the nitration process3And (4) increasing the concentration of N, conveying a part of the mixed liquid of the wastewater and the microbial activated sludge in the aerobic tank to the anoxic tank by a digestive juice reflux pump for continuous treatment, conveying the other part of the mixed liquid to a secondary sedimentation tank for sedimentation separation, conveying the effluent of the secondary sedimentation tank to a subsequent flocculation precipitation filtering unit 11, conveying a part of sludge I settled at the bottom of the secondary sedimentation tank to the front-end aerobic tank by a sludge reflux pump, and discharging a part of sludge I as residual activated sludge out of the system. After the wastewater is treated by the A/O biochemical treatment unit 10, most organic matters and ammonia nitrogen in the wastewater are removed.
In one embodiment, the COD in the effluent of the A/O biochemical treatment unit 10 is less than 250mg/l and the ammonia nitrogen is less than 5 mg/l.
The form of the A/O biochemical treatment unit 10 of the present invention is not particularly limited, and the A/O process and its variants, which are common in the art, such as A2The specific operation parameters such as sludge load, retention time, sludge reflux ratio, and digester reflux ratio are not particularly limited, so long as the same treatment effect is achieved, e.g.,/O, SBR.
In one embodiment, the flocculation filtration unit 11 can be connected to the A/O biochemical treatment unit 10. The flocculation precipitation filtration unit 11 is provided with a flocculation reaction tank, a sedimentation tank and a filter. After the effluent of the A/O biochemical treatment unit 10 enters the flocculation reaction tank, under the action of the flocculating agent L and the coagulant aid M, colloids and fine suspended matters in the sewage are coagulated into floccules, and then the floccules are precipitated in the sedimentation tank, so that most of pollutants such as suspended matters, colloids, microorganism slime, turbidity and the like in the wastewater to be treated are removed. And then, the effluent of the sedimentation tank enters a filter, and pollutants such as suspended matters, colloid and the like in the water are further removed.
In one embodiment, the content of suspended matters in the effluent after being treated by the flocculation precipitation filtration unit 11 is less than 10 mg/l.
The utility model discloses there is not special restriction to the structural style of flocculation and precipitation filtration unit 11's sedimentation tank, can adopt common sedimentation tank, mechanical stirring depositing reservoir or high density depositing reservoir etc. in the field, the utility model discloses also there is not special restriction to the type of filter, can adopt common many medium filter or membrane filter etc. in the field as long as reach same treatment effect can.
In one embodiment, the second adsorption unit 12 is connected to the flocculation filtration unit 11. The second adsorption unit 12 is provided with an adsorption column filled with an adsorbent having selective adsorption capacity for heterocyclic compounds, refractory organics of nitrogen-containing aromatic hydrocarbons and the like, and after the effluent of the flocculation precipitation filtration unit 11 flows through the adsorption column, the heterocyclic compounds, refractory organics of nitrogen-containing aromatic hydrocarbons, water-soluble and polar organics, ionic micromolecular organics and the like therein are adsorbed on the adsorbent.
In one embodiment, the COD content in the effluent of the adsorption column of the second adsorption unit 12 is less than 150mg/l, the chroma is less than 40, and further the COD content is less than 80mg/l, and the chroma is less than 20.
In one embodiment, the second adsorption unit 12 is further provided with a desorption system, a desorption agent is provided in the desorption system, when the adsorbent is gradually saturated, and the content of COD in the effluent exceeds the design index, the desorption agent is used for desorption regeneration, and the regenerated adsorbent is put into use again.
The utility model discloses do not have special limitation to the adsorbent of second adsorption element 12, can adopt the common adsorption resin in this field, strong, weak alkaline resin or other adsorption material that have equivalent effect, as long as these adsorption materials have selective adsorption capacity to the micromolecular organic matter and the colourity of refractory organic matter, water-solubility and polarity organic matter, ionic state can. The utility model discloses also not having special limitation to the desorbent, can adopting ketone, alcohol or salt, alkali etc. as long as use these desorbents to the adsorbent regeneration back, can resume the adsorbent adsorption efficiency can.
The treated wastewater K discharged by the second adsorption unit 12 can reach the national specified coke quenching standard, can be directly used for coke quenching, and can also be continuously subjected to reverse osmosis membrane to further remove organic matters and salt substances in the wastewater, so that the recycled reclaimed water reaches a higher water quality standard, and near zero emission is realized. Due to the adoption of the treatment system of the embodiment of the utility model, the subsequent reverse osmosis desalination system can realize long-term stable operation, and the recovery rate of water can be higher.
The utility model discloses an embodiment's effluent disposal system is applicable in the processing of coal chemical industry waste water such as the low temperature low pressure gasification of blue charcoal, coking, coal.
The wastewater treatment system of an embodiment of the utility model can treat wastewater containing oil, ammonia and phenol, such as coal chemical industry or coking wastewater, and can recycle the oil, phenol, ammonia and the like in the wastewater, and treat the wastewater to meet the recycling standard for recycling; the device can also effectively solve the coking and dirt blocking tendency of the device in the wastewater treatment process, and improve the stability and reliability of the operation of the wastewater treatment device, thereby ensuring the long-term, stable and reliable operation of the wastewater treatment system. Meanwhile, the investment and the occupied area are less.
The following will further explain an embodiment of the wastewater treatment system according to the present invention with reference to the drawings and the specific examples.
Examples
The method comprises the following steps of: CODcr50000mg/L, BOD520000mg/L, 3000mg/L ammonia nitrogen, 6000mg/L volatile phenol, 1000mg/L petroleum compound, 100mg/L sulfide and 500mg/L suspended matter.
a. And introducing the wastewater A to be treated into a horizontal flow type oil separation tank of the gravity oil removal unit 1, and staying for 7 hours. The oil content of the effluent of the oil removal tank is 700mg/l, and the content of suspended matters is 250 mg/l.
b. The effluent of the oil separation tank is heated to 60 ℃ by steam in a first heating unit 2, and then is lifted by a pump to be sent into a coalescence deoiling system of a coalescence deoiling unit 3, wherein coalescence deoiling adopts 3 grades, the effluent oil content is 100mg/l, and the suspended matter content is 50 mg/l.
c. And heating the water discharged from the coalescence deoiling unit 3 to 80 ℃ in a second heating unit 4 by using steam, and pumping the water to a ceramic membrane filtering system of the filtering unit 5, wherein the ceramic membrane system adopts cross-flow filtration, the circulating flow of the cross-flow filtration is 6 times of the filtering flow, and the filtering flux is 500 LMH. At the moment, the water recovery rate is 95 percent, the effluent suspended substance is approximately equal to 0mg/L, and the effluent turbidity is less than 0.1 NTU.
d. And (3) sequentially introducing water produced by the ceramic membrane filtration system into a deacidification tower and a deamination tower of the deacidification and dephenolization unit 6, wherein the deacidification tower and the deamination tower are normal-pressure rectifying towers, and 1.5MPaG saturated steam is used as a heat source in a tower kettle to provide heat through a reboiler. The CO which is extracted from the top of the deacidification tower is rich in2And H2And (3) sending the acidic tail gas of the S to an incinerator, carrying out two-stage condensation and separation on an ammonia-containing gas phase extracted from the top of the deamination tower, desulfurizing, and absorbing ammonia gas by using water to obtain an ammonia water product with the ammonia content of not less than 20 wt%.
e. The water discharged from the deamination tower is lifted by a pump to enter an extraction dephenolization system of an extraction dephenolization unit 7, wherein an extracting agent is MIBK, a fiber membrane contactor is adopted by the extraction dephenolization system as a contact and mass transfer medium of wastewater and an extracting solvent, the wastewater and the solvent flow through a fiber membrane and then are kept stand and separated in a phase separator, the solvent at the upper part enters a regeneration tower for solvent regeneration, the regeneration tower is a reduced pressure rectification tower, the operation pressure is-70 KPa, and 1.5MPaG saturated steam is used as a heat source by a reboiler at the bottom of the regeneration tower. Tower bottoms at the bottom of the regeneration tower are used as crude phenol products and are cooled to 40 ℃ for recovery, wherein the phenol content is more than 83%. Waste water CODcr2568mg/l, BOD at the lower part of the phase separator of the extraction dephenolization system5624mg/L, 90mg/L of volatile phenol, 20mg/L of sulfide and 100mg/L of ammonia nitrogen.
f. The wastewater at the lower part of the phase separator of the extraction dephenolization system passes through a dephenolization resin adsorption column of a first adsorption unit 8, the flow rate of the adsorption column is 3BV/h, and the effluent CODcr1260mg/l, BOD5427mg/l, volatile phenol 13.5 mg/l. The resin saturated with adsorption was regenerated with methanol for a regeneration period of 24 hours. And rectifying the regenerated waste liquid by using a rectifying tower to obtain the methanol for recycling.
g. Introducing the effluent of the dephenolized resin adsorption column into a hydrolysis acidification pool of a hydrolysis acidification unit 9 for hydrolysis acidificationThe tank adopts a composite hydrolysis acidification reactor, namely a hydrolysis acidification reactor with a packing layer is additionally arranged in a sludge bed of an upflow hydrolysis acidification reactor. PP elastic filler is arranged in the pool to increase the contact area of microorganisms and water and maintain biomass. The retention time of the wastewater in the hydrolysis acidification tank is 20 hours, and the effluent CODcr1130mg/l, BOD5448mg/l and 120mg/l ammonia nitrogen.
h. Introducing the effluent of the hydrolysis acidification tank into an A/O biochemical treatment system of an A/O biochemical treatment unit 10, arranging a stirrer at an anoxic section, adopting a three-gallery plug-flow type aerobic aeration tank at an aerobic section, arranging a slat type microporous aerator at the bottom of the tank, wherein the residence time of the anoxic section is 18 hours, the residence time of the aerobic section is 118 hours, and the reflux ratio of the nitrifying liquid is as follows: 200% -400%; sludge reflux ratio: 50 to 100 percent. Effluent CODcr is less than 230mg/l, ammonia nitrogen is 3mg/l, phenol is 0.2mg/l, sulfide is 0.1mg/l, and petroleum compound is 0.5 mg/l.
i. Adding agents such as a coagulant PFS, a flocculant PAM and the like into the effluent of the A/O biochemical treatment unit 10, stirring for reaction, wherein the adding amount of the coagulant is 50ppm, the adding amount of the flocculant is 1.5ppm, the reaction time is 5 minutes, and then, clarifying the effluent in a high-efficiency clarifying tank. The ascending flow velocity of the inclined plate area of the clarification tank is designed according to 2.2-2.5 mm/S. And the effluent of the clarification tank enters a multi-medium filter, and filter materials adopt quartz sand and anthracite, wherein the filling height of the quartz sand is 800mm, the filling height of the anthracite is 400mm, and the filtering speed is 7 m/h. The suspended substance of the filter effluent is 5mg/L, and the CODcr is 140mg/L
j. And (3) introducing the effluent of the multi-medium filter into a de-organic resin adsorption device of the second adsorption unit 12, wherein adsorption resin is filled in the resin adsorption device, and tests show that the effluent CODcr of the resin adsorption device is 70mg/l and the suspended matters are less than 5 mg/l. Can completely meet the water quality standard of the coke quenching water. The resin saturated with adsorption was regenerated with NaCl and NaOH for a 48 hour period.
As can be seen from the above embodiments, most of the oil and suspended matters in the wastewater are removed by the gravity oil removal unit 1 and the coalescence oil removal unit 3; the residual suspended matters in the wastewater are removed through the filtering unit 5, so that the pollution and blockage of the deacidification tower and the deamination tower are prevented; while the two heating treatments in the first heating unit 2 and the second heating unit 4 create advantageous operating conditions for coalesced degreasing and membrane filtration; most of sulfide and ammonia are removed by the deacidification and deamination unit 6; most of the phenolic compounds are removed by the extraction dephenolation unit 7; most of the residual volatile phenol is removed through the first adsorption unit 8, so that the toxic action of phenol on the microorganisms of a subsequent biochemical treatment system is avoided; the biodegradability of the wastewater is improved through the hydrolysis acidification unit 9, and most of COD, ammonia nitrogen, phenol, sulfide and other pollutants in the wastewater are removed through the A/O biochemical treatment unit 10; then suspended matters and colloid in the biochemical effluent are removed through the flocculation precipitation filtering unit 11, and refractory organic matters and chromaticity in the wastewater are removed through the adsorption action of the second adsorption unit 12 for removing organic matters, so that the standard of recycling is achieved.
The utility model discloses an embodiment's effluent disposal system can make the system long-term, stable, move reliably, has apparent economic benefits and environmental benefit.
Unless otherwise defined, all terms used in the present invention have the meanings commonly understood by those skilled in the art.
The described embodiments are for illustrative purposes only and are not intended to limit the scope of the present invention, and various other substitutions, changes and modifications may be made by those skilled in the art within the scope of the present invention.
Claims (10)
1. A wastewater treatment system, said wastewater comprising oil, phenolic compounds, and ammonia, said treatment system comprising:
the gravity oil removal unit is used for removing at least part of heavy oil, floating oil and suspended matters in the wastewater through standing layering treatment;
the coalescence deoiling unit is used for removing at least part of emulsified oil and suspended matters in the effluent of the gravity deoiling unit;
the filtering unit is used for filtering the effluent of the coalescence deoiling unit;
the deacidification and deamination unit is used for carrying out deacidification and deamination treatment on the effluent of the filtering unit so as to remove at least part of acidic compounds and ammonia in the effluent;
the extraction and dephenolization unit is used for carrying out extraction treatment on the effluent of the deacidification and deamination unit so as to remove at least part of phenolic compounds in the effluent;
the first adsorption unit is used for carrying out adsorption treatment on the effluent of the extraction dephenolization unit so as to remove at least part of residual phenolic compounds;
the A/O biochemical treatment unit is used for performing biochemical treatment on the effluent of the first adsorption unit;
the flocculation precipitation filtering unit is used for carrying out flocculation, precipitation and filtering treatment on the effluent of the A/O biochemical treatment unit; and
and the second adsorption unit is used for carrying out adsorption treatment on the effluent of the flocculation precipitation filtering unit so as to remove at least part of heterocyclic compounds and nitrogen-containing aromatic compounds in the effluent.
2. The wastewater treatment system of claim 1, wherein the gravity degreasing unit, the coalescing degreasing unit, the filtering unit, the deacidification deamination unit, the extraction dephenolization unit, the first adsorption unit, the A/O biochemical treatment unit, the flocculation precipitation filtering unit, and the second adsorption unit are connected in sequence.
3. The wastewater treatment system according to claim 1, wherein a container for sedimentation separation, an oil sump and a sludge discharge tank are provided in the gravity oil removal unit, and a collection device is provided in the container for sedimentation separation.
4. The wastewater treatment system according to claim 1, wherein a coalescing separator is provided in said coalescing oil removal unit; and/or the deacidification and deamination unit is provided with a deacidification tower and a deamination tower.
5. The wastewater treatment system according to claim 1, wherein an adsorption column is provided in the first adsorption unit, and an adsorbent capable of adsorbing phenolic compounds is packed in the adsorption column.
6. The wastewater treatment system according to claim 1, wherein an adsorption column is provided in the second adsorption unit, and an adsorbent capable of adsorbing a heterocyclic compound or a nitrogen-containing aromatic hydrocarbon compound is packed in the adsorption column.
7. The wastewater treatment system according to claim 1, wherein a membrane filter is provided at the filtering unit; and/or the presence of a gas in the gas,
the extraction dephenolization unit is provided with a cooler, an extraction reactor, a phase separator and an extractant regeneration tower.
8. The wastewater treatment system according to claim 7, wherein a ceramic membrane or a metal sintered membrane is provided in the membrane filter; and/or the presence of a gas in the gas,
the extraction reactor is a fibrous membrane contactor.
9. The wastewater treatment system of claim 1, further comprising a first heating unit and/or a second heating unit, the first heating unit being connected to the gravity oil removal unit and the coalescing oil removal unit, respectively; the second heating unit is respectively connected with the coalescence deoiling unit and the filtering unit.
10. The wastewater treatment system of claim 1, further comprising a hydrolytic acidification unit, the hydrolytic acidification unit being connected to the first adsorption unit and the A/O biochemical treatment unit, respectively.
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