CN103288310B - Slack coal pressure gasification wastewater treatment method and treatment system as well as application - Google Patents

Slack coal pressure gasification wastewater treatment method and treatment system as well as application Download PDF

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Publication number
CN103288310B
CN103288310B CN201310271931.0A CN201310271931A CN103288310B CN 103288310 B CN103288310 B CN 103288310B CN 201310271931 A CN201310271931 A CN 201310271931A CN 103288310 B CN103288310 B CN 103288310B
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waste water
treatment
unit
filtrate
water
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CN103288310A (en
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安洪光
李春启
岳子明
刘俊峰
梅长松
宋学平
赵荧
李国胜
张文博
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Datang International Chemical Technology Research Institute Co Ltd
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Datang International Chemical Technology Research Institute Co Ltd
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Abstract

The invention provides a slack coal pressure gasification wastewater treatment method and treatment system as well as application. The treatment method sequentially comprises the following steps of: (1) performing coagulating sedimentation on the wastewater to obtain wastewater after the coagulating sedimentation treatment; (2) performing chemical catalysis on the wastewater obtained by the step (1) to obtain wastewater after the catalytic oxidation treatment; (3) performing aeration biofiltration on the wastewater obtained by the step (2) to obtain wastewater after the aeration biofiltration treatment; and (4) performing membrane separation on the wastewater obtained by the step (3) to obtain dischargeable/recyclable water.

Description

A kind of crushed coal pressure gasifying method of wastewater treatment and treatment system and application
Technical field
The present invention relates to a kind for the treatment of process and treatment system of waste water, be specifically related to a kind for the treatment of process of crushed coal pressure gasifying waste water, and for the system processed crushed coal pressure gasifying waste water of the method and the method or this system for the treatment of the application in crushed coal pressure gasifying waste water.
Background technology
Crushed coal pressure gasifying waste water is the coal gasification waste water that broken coal produces in pressurized gasification process.The materials such as the heterogeneous ring compound containing a large amount of ammonia nitrogen, aldehydes matter, oily substance, prussiate, mononuclear aromatics and polycyclic aromatic hydrocarbonss and nitrogenous, sulphur, oxygen in this waste water, wherein COD cr(refer to and adopt potassium bichromate (K 2cr 2o 7) chemical oxygen demand that determines as oxygenant, i.e. dichromate index) concentration is 4000 ~ 5000mg/L, unit phenol (in phenol) is 450 ~ 550mg/L, and polyphenol (in phenol) is 500 ~ 600mg/L, and ammonia nitrogen is 200 ~ 300mg/L.Crushed coal pressure gasifying waste water has that quantity discharged is large, organic concentration is high, ammonia nitrogen concentration high, is one of difficult trade effluent of generally acknowledging in the world.
At present, crushed coal pressure gasifying wastewater treatment generally adopts sequencing batch active sludge (SequencingBatch Reactor Activated Sludge Process, be called for short SBR method), anoxic/aerobic method (Anoxic/Oxic is called for short A/O method) and multistage A/O technique biologic treating technique.But, water-quality guideline after biological treatment often can not reach the emission standard of national regulation, needing after secondary or Multilevel biochemistry treatment, increase the technique such as coagulating sedimentation, quartz sand filtration makes it reach emission standard, adds investment and the running cost for the treatment of facility.
Realizing waste water recycling is reduce wastewater discharge at present, reduces environmental pollution, one of vital task fulfiling corporate environmental responsibility.Conventional waste water recycling treatment technology has electrochemical deposition, advanced oxidation, membrane sepn and absorption method etc., wherein, membrane separation technique becomes the recycling processing technique of current first-selection because having the features such as separation efficiency is high, stable, working cost is low, but due to crushed coal pressure gasifying waste water after the biochemistry-coagulating treatment of routine still containing higher concentration organism (COD crabout 200mg/L), and be macromole (being mainly benzene ring substance) hardly degraded organic substance, fouling membrane is serious, backwash is difficult, run the shortcomings such as pressure reduction rising is fast directly to adopt membrane separation technique to exist.In order to remove the organism in water, having at present and increasing activated carbon filtration to reach reduction COD before membrane sepn crobject, but be easy to make charcoal absorption saturated, there is gac and change the shortcomings such as frequent, running cost is high, backwash frequency is high.
Chinese patent CN101857331A discloses a kind of coal chemical industry wastewater zero emission treatment method and system, this invention relate to before Using Multistage Membranes is separated and uses activated coke filter bed as film pretreatment technology, make use of most of organism in activated coke absorption degradation water, to reduce the feature of the risk of fouling membrane, but ignore the shortcoming of activated coke limited sorption capacity, the backwash frequency that there is activated coke is high, change the problems such as activated coke is frequent, coke ratio is large, and a large amount of useless burnt of generation will become new secondary pollutant.
Chinese patent CN101560045A discloses a kind of coal chemical wastewater treating technique, coal chemical industrial waste water is carried out pre-treatment by air-floating apparatus by this technique, obtain pretreated waste water, Fenton class reagent is joined in pretreated waste water and carries out secondary treatment, waste water after secondary treatment is by activated sludge aeration pond, in aeration tank, add active carbon powder carry out advanced treatment, waste water after advanced treatment is carried out Ultra filtration membrane, reuse water after Ultra filtration membrane obtains the reuse water after reverse osmosis by reverse osmosis membrane, namely the process to waste water is completed after reuse water after reverse osmosis is carried out evaporative crystallization.In this treatment process, make use of the adsorption of activity charcoal powder, the Adsorption of Organic in water is fallen thus reaches and reduce COD crobject, but owing to containing a large amount of viscosity mud in aeration tank, to stick on active carbon powder, limit activated carbon adsorptive capacity, thus be easy to cause effluent quality unstable, organism in water outlet is simultaneously still larger molecular organics, when entering in ultrafiltration system, dirt will block up ultra-filtration membrane and affect work-ing life and the operation stability of ultra-filtration membrane.
Therefore, also need at present to find a kind of technical feasibility and can realize long-time continuous stable run complete membrane technology.
Summary of the invention
Therefore, the object of the invention is to overcome the problems referred to above of the prior art and defect, provide a kind of simple to operate, stable, with low cost, crushed coal pressure gasifying method of wastewater treatment that processing efficiency is higher and corresponding treatment system, phenomenon is blocked up in the dirt significantly reducing membranous system, thus achieves qualified discharge and/or the reuse of waste water.
The invention provides a kind of crushed coal pressure gasifying method of wastewater treatment, described treatment process sequentially comprises:
(1) waste water is carried out coagulating sedimentation, obtain the waste water after coagulating kinetics;
(2) waste water that above-mentioned steps (1) obtains is carried out chemical catalysis, obtain the waste water after catalytic oxidation treatment;
(3) waste water that above-mentioned steps (2) obtains is carried out biological aerated filter, obtain the waste water after biological aerated filter process; Preferably, described biological aerated filter mainly refers to and utilizes BAF (Biological Aerated Filter) to process waste water;
(4) waste water that above-mentioned steps (3) obtains is carried out membrane sepn, obtain discharging/reuse water.
Preferably, described step (1) comprising: in waste water, add flocculation agent react, and precipitation, gets supernatant liquid, obtain the waste water after described coagulating kinetics.Most suspended substances in waste water, colloid and partial organic substances can be separated by flocculation, precipitating action, get the waste water of supernatant liquid as subsequent disposal, throw out then can be discharged by the mud discharging mouth of bottom.In addition, before waste water is passed into coagulating sedimentation unit, first can carry out conventional pre-treatment, SBR technique, A/O technique and/or the biological treatment of multistage A/O technique as required, become bio-chemical effluent, then carry out the process in the present invention.
More preferably, described step (2) comprising: in the waste water that step (1) obtains, add strong oxidizer react, obtain the waste water after described catalytic oxidation treatment.Use strong oxidizer, as chlorine, hypochlorite, potassium permanganate, ozone etc., the organism of difficult degradation in water, macromolecule oxidation operation can be removed or be oxidized to the small-molecular-weight organism of readily biodegradable, thus improve the biodegradability of waste water, reduce the molecular weight entering membrane sepn step simultaneously, contribute to the cost reducing membrane separation.
Again preferably, described step (3) comprising: waste water step (2) obtained interacts with the filtrate being loaded with microorganism in BAF, and by continuing aeration effect, obtains the waste water after described biological aerated filter process.Filtrate wherein can be used for the organism in absorption and filtered wastewater, passes through the microbial process on filtrate hole and surface, by its oxidative degradation simultaneously.The microorganism such as nitrifier, carbonization bacterium that this microorganism can be commonly used for this area.
According to method of the present invention, wherein, in step (1), described flocculation agent can select polymerize aluminum chloride (PAC).Preferably, the dosage of described flocculation agent can be 350 ~ 400mg/L(i.e. often liter of dosage that need process in waste water), can 350mg/L be preferably.More preferably, adding the reaction times after described flocculation agent can be 30 ~ 60min, can be preferably 30min, and sedimentation time can be 3 ~ 5h, can be preferably 4h.By selecting suitable added amount of chemical and operational condition, the organic matter removal effect in water can be made to reach optimum level, such as, can make COD crclearance reaches about 50%.
According to method of the present invention, wherein, in step (2), described strong oxidizer is ozone.Preferably, the dosage of ozone is 25 ~ 100mg/L(i.e. often liter of dosage that need process in waste water), can 50 ~ 75mg/L be preferably, be more preferably 75mg/L.Further preferably, the reaction times adding ozone can be 30 ~ 90min, can be preferably 30min.Ozone has stronger oxidation capacity to various organic group and oxidizing reaction is rapid, can not produce secondary pollution simultaneously.Contriver finds, if the dosage of ozone is lower than range of choice of the present invention, then be difficult to the organism of difficult degradation, larger molecular organics oxygenolysis, thus the removal efficiency of follow-up biological aerated filter and the operating flux of membrane sepn can be affected, if but dosage is higher than scope of the present invention, then can cause investment and the waste of running cost, be unfavorable for the industrialization promotion for the treatment of process.
According to method of the present invention, wherein, in step (2), also supersound process can be carried out to waste water.Preferably, described supersound process can be carried out adding while strong oxidizer carries out reacting.More preferably, the ultrasonic frequency of supersound process can be 20 ~ 40kHz, can be preferably 25 ~ 35kHz.By hyperacoustic cavatition, particulate in liquid can be made to produce strenuous vibration, then produce little cavity at liquid internal, the chemical reaction between solute dissolves and solute can be accelerated, thus can Reaction time shorten, improve reaction efficiency.
According to method of the present invention, wherein, in step (3), described filtrate can be activated coke filtrate.Activated coke filtrate has larger specific surface area, and central hole structure is flourishing, has good adsorption, and the microorganism in hole and on surface can be utilized to be degraded by adsorbed oxidation operation to the organic pollutant in water.Preferably, the particle diameter of described activated coke filtrate is 3 ~ 5mm, and mean pore size is 4 ~ 16nm.More preferably, the pack density of described filtrate is 0.5 ~ 0.6g/cm 3.Further preferably, the empty bed residence time of described biological aerated filter unit is 6 ~ 8h, can be preferably 8h.
According to method of the present invention, wherein, in step (4), described membrane sepn comprises uf processing and reverse-osmosis treated.
Preferably, described uf processing can adopt external pressure type ultra-filtration membrane to carry out.More preferably, the material of ultra-filtration membrane can be PVDF, and filtering accuracy can be 0.03 micron, and operating pressure can be 0.08 ~ 0.20MPa, and filtration flux can be 20 ~ 60L/m 2h, preferably, filtration flux is 25 ~ 45L/m 2h, more can be preferably 40L/m 2h.By the membrane sepn effect of uf processing, bacterium remaining in water, suspended substance, colloid and small portion inorganics etc. can be retained.In treatment process of the present invention, the cycle of ultra-filtration membrane normal backwash is 20 ~ 60 minutes, such as every 30 minutes, 40 minutes, 50 minutes or backwash in 60 minutes are once, the backwash time can be 120 ~ 180 seconds/time, can be preferably 150 seconds/time, the cycle that chemistry strengthens backwash then can extend to 24 hours, namely only needs every day once chemistry to strengthen backwash, it can be 10 ~ 30min that chemistry strengthens the backwash time, can be preferably 15min.The conventional chemical agent in this area can be adopted to carry out backwash, hydrochloric acid, clorox, sodium hydroxide etc. can be included but not limited to.
Preferably, described reverse-osmosis treated can adopt pollution-resistant reverse osmosis membrane to carry out.By the membrane sepn effect of reverse-osmosis treated, can by inorganic salts separating substances in water out.The water purification produced after being separated can reuse be circulating water system moisturizing or the chemical feed water (i.e. reuse water) as boiler shop, also can qualifiedly discharge.The dense water produced can be used for grey field in factory and sprays.This resistance to crocking reverse osmosis membrane can be BW30FR-400/34i etc., also can add Scale inhibitors (such as nail (unit of length) section PC191) is 2 ~ 8mg/L(i.e. often liter of dosage that need process in waste water simultaneously), 2mg/L can be preferably, reductive agent (such as sodium bisulfite) is 3 ~ 10mg/L, 6mg/L can be preferably, non oxidizing bactericide (such as nail (unit of length) section OSM965) is 8 ~ 10mg/L, can 10mg/L be preferably, etc.
According to method of the present invention, wherein, before the method is also included in step (4), multi-medium filtering is carried out to the waste water that step (3) obtains.Preferably, the filtrate in described multi-medium filtering step comprises hard coal and quartz sand.The material such as macrobead thing, suspended substance, colloid remaining in water can be retained removal, to alleviate the operating pressure of subsequent film separating treatment by this multi-medium filtering process further.
According to method of the present invention, wherein, the COD of the waste water of coagulating sedimentation is carried out crconcentration can be 300 ~ 400mg/L, and unit phenol (in phenol) can be 50 ~ 80mg/L, and polyphenol (in phenol) can be 60 ~ 110mg/L, and ammonia nitrogen can be≤15mg/L.
Present invention also offers the treatment system of a kind of crushed coal pressure gasifying waste water for treatment process of the present invention, this system comprises the coagulating sedimentation unit, chemical catalysis unit, biological aerated filter unit and the film separation unit that sequentially connect.Preferably, described film separation unit can comprise ultra filtration unit and reverse osmosis units.More preferably, multi-medium filtering unit can also be provided with between described biological aerated filter unit and film separation unit.
According to system of the present invention, wherein, described chemical catalysis unit can be provided with device for absorbing tail gas.Preferably, carbon leaching material is filled with in described device for absorbing tail gas.This device for absorbing tail gas can adopt tower structure, filling carbon leaching material in tower, for strong oxidizer remaining in planar water as ozone, avoids having a negative impact to links such as follow-up biological aerated filters.More preferably, the filling ratio of described carbon leaching material can be 30 ~ 40%v/v(volume percent), can 30%v/v be preferably.
The working temperature for the treatment of process of the present invention or treatment system can be 18 ~ 30 DEG C, can be preferably 25 DEG C.
Present invention also offers treatment process of the present invention or the application for the treatment of system in process crushed coal pressure gasifying waste water.
Treatment process of the present invention and system thereof have but are not limited to following beneficial effect:
Even if 1. crushed coal pressure gasifying waste water still has a large amount of difficult biochemical larger molecular organics after routine biochemistry process.For this feature, present invention employs chemical catalysis and react the technique combined with biological aerated filter, be first the small-molecule substance of readily biodegradable by the larger molecular organics oxygenolysis in waste water, improve the biodegradability of waste water, then utilize follow-up biological aerated filter process effectively to be decomposed by remaining organism, water outlet COD can be made crreach below 60mg/L, and have simple to operate, running cost is low, the advantage such as stable.
2. the present invention is by the optimal design-aside to treatment scheme, substantially increases operating flux and the matting cycle of membranous system in ultra filtration unit and reverse osmosis units, thus reduces equipment investment cost and running cost.Meanwhile, owing to significantly improving the matting cycle of membranous system, extend the work-ing life of membranous system, improve membrane separation efficiency.
3. contriver also finds, if be combined strong oxidizer ozone and supersound process in chemical catalysis step, greatly can reduce the chemical feeding quantity of ozone, further reduces water outlet COD simultaneously crconcentration.This may be accelerate the dispersion of ozone in waste water, Dissolution and dissociation due to ultrasonic, thus produces a large amount of free radical, greatly enhances the oxidation efficiency of ozone.And ultrasonicly itself also the macromole of part difficult degradation can be decomposed into small molecules, there is certain synergy.This discovery significantly improves the processing efficiency of follow-up biological aerated filter, then contributes to the operating flux improving ultrafiltration and reverse osmosis units, promotes the raising of membrane sepn efficiency.
4. in addition, the present invention has also selected activated coke as the filtrate of biological aerated filter.Compared with conventional haydite, select activated coke significantly can reduce the water outlet COD of biological aerated filter cr, and the frequent backwash that the system pressure difference of subsequent film separating unit can not be caused to rise rapidly and cause.When contriver also finds to use mean pore size to be the activated coke of 4 ~ 16nm, better effect can be obtained.
Accompanying drawing explanation
Below, describe embodiment of the present invention in detail by reference to the accompanying drawings, wherein:
Fig. 1 shows the schematic diagram of a kind of embodiment of crushed coal pressure gasifying Waste Water Treatment of the present invention.
Embodiment
Further illustrate the present invention below by specific embodiment, but should be understood to, these embodiments are only used for the use specifically described more in detail, and should not be construed as limiting the present invention in any form.
General description is carried out to the material used in the present invention's test and test method in this part.Although for realizing many materials that the object of the invention uses and working method is well known in the art, the present invention still describes in detail as far as possible at this.It will be apparent to those skilled in the art that within a context, if not specified, material therefor of the present invention and working method are well known in the art.
embodiment 1
The present embodiment is for illustration of crushed coal pressure gasifying method of wastewater treatment of the present invention and treatment system thereof.
Crushed coal pressure gasifying Waste Water Treatment as shown in Figure 1, described treatment system comprises the coagulating sedimentation unit, chemical catalysis unit, biological aerated filter unit, multi-medium filtering unit, ultra filtration unit and the reverse osmosis units that sequentially connect.In reality is built, existing equipment and the technology with above-mentioned functions can be selected, such as coagulating sedimentation unit can be coagulation-settling tank, chemical catalysis unit can be chemical catalysis reaction tank, biological aerated filter unit can be BAF, multi-medium filtering unit can be more medium filter, etc.Aforesaid device and structures connect successively by pipeline.
Can be provided with device for absorbing tail gas in chemical catalysis unit, wherein be filled with carbon leaching material, filling ratio can be 30 ~ 40%v/v.
The technical data of this treatment system can be set as follows (working temperature for the treatment of system is about 25 DEG C):
(1) coagulating sedimentation unit
Reaction times: 30 minutes
Sedimentation time: 4 hours
Coagulating agent: polymerize aluminum chloride (PAC), dosage: 350 milligrams/often liter waste water
(2) chemical catalysis unit
Oxygenant: ozone (O 3), dosage: 75 milligrams/often liter waste water
Reaction times: 30 minutes
pH:7~8.5
The device for absorbing tail gas residence time: 25 minutes
Activated carbon particle size: 1 ~ 3mm
Pack density: 0.45-0.55g/cm 3
Packing fraction: 30%(volume ratio)
Device for absorbing tail gas hydraulic load: 10m/h
(3) biological aerated filter unit
Filtrate: activated coke, particle diameter: 3 ~ 5mm, mean pore size: 4 ~ 16nm
Pack density: 0.5 ~ 0.6g/cm 3
The empty bed residence time: 8 hours
Filtering velocity: 4 ~ 10m/h
Backwash water filtering velocity: 20 ~ 60m/h
Backwash air filter speed: 20 ~ 60m/h
The backwash time: 30 ~ 40 minutes
(3) multi-medium filtering unit
Anthracite granule size: 1.2 ~ 1.8mm
Hard coal loading height: 800mm
Quartz sand particle size: 0.5 ~ 1.2mm
Quartz sand loading height: 400mm
Hydraulic load: 10m/h
Backwash water filtering velocity: 20 ~ 50m/h
Backwash gas intensity: 12 ~ 18L/sm 2
The backwash time: 5 ~ 10 minutes
(4) ultra filtration unit
Filtered version: grossflow filtration
Ultra-filtration membrane material: PVDF material
Filtering accuracy: 0.03 micron
Operating pressure: 0.08 ~ 0.20MPa
Filtration flux: 40L/m 2h
The backwash cycle: backwash in every 30 minutes once
The backwash time: 150 seconds/time
Backwash water flux: 90 ~ 120L/m 2h
Chemistry is strengthened washing the cycle: one day
Chemistry is strengthened washing the time: 15 minutes
Chemistry strengthens wash agent concentration: 300 ~ 500mg/L clorox
(5) reverse osmosis units
Reverse osmosis membrane: pollution-resistant film BW30FR-400/34i(is purchased from Dow Chemical)
Operating pressure: 0.8 ~ 2MPa
Permeant flux: 18L/m 2h
Scale inhibitors (nail (unit of length) section PC191, purchased from American Nalco Chemical Co): 2 milligrams/often liter waste water
Reductive agent (NaHSO 3): 6 milligrams/often liter waste water
Non oxidizing bactericide (nail (unit of length) section OSM965, purchased from American Nalco Chemical Co): 10 milligrams/often liter waste water
The rate of recovery: 75%
Ratio of desalinization: > 95%
The coagulating agent used in said process, sterilant, reductive agent can be all the medicaments used in conventional water treatment process.
Pending crushed coal pressure gasifying waste water is bio-chemical effluent, water yield 600m 3/ h, waste water quality: pH value: 7 ~ 8.5, COD cr: 300 ~ 400mg/L, TDS:2000 ~ 2500mg/L, SS:30 ~ 50mg/L, unit phenol (in phenol): 50 ~ 80mg/L, polyphenol (in phenol): 60 ~ 110mg/L, ammonia nitrogen :≤15mg/L.
Waste water delivers to coagulating sedimentation unit through force (forcing) pump, the effect such as utilize the electrical counteract of coagulating agent (as PAC), adsorption bridging and net to catch, and is removed by the materials such as the organism in water, suspended substance, after coagulation and precipitation, and water outlet COD cr≤ 200mg/L, SS≤15mg/L.
Waste water after coagulating sedimentation pumps in chemical catalysis unit, the larger molecular organics of the organism in water especially containing phenyl ring class directly can be degraded remove or be converted into small organic molecule by the strong oxidizing property of ozone.After catalyzed oxidation, water outlet COD cr≤ 180mg/L.
Biological aerated filter unit is pumped into through the reacted waste water of chemical catalysis, because chemical catalysis reaction makes the material oxidized point of larger molecular organics especially containing phenyl ring class take off or be decomposed into small-molecule substance, these small-molecule substances can be removed by microorganism absorption degradation, after BAF, water outlet COD cr≤ 60mg/L, SS≤10mg/L.
Waste water after biological aerated filter enters into ultra filtration unit, through the membrane sepn effect of ultra filtration unit, can remove the materials such as the bacterium in water, colloid and suspended substance, effluent quality COD after ultrafiltration cr≤ 50mg/L, turbidity≤0.1NTU, SDI 15≤ 4.
Waste water after ultrafiltration enters into reverse osmosis units, through the effect of reverse osmosis membrane, macromolecule contaminant in water and partial solubility solids content is separated in concentrated solution, the product water COD of reverse osmosis units cr≤ 20mg/L, TDS≤75mg/L, can meet the requirement of reuse.The dense water that reverse osmosis units produces can be used for grey field and sprays.
Effluent quality after treated system process: pH value: 6.5 ~ 7.5, COD cr≤ 20mg/L, TDS≤75mg/L, unit phenol (in phenol) :≤1mg/L, polyphenol (in phenol) :≤1mg/L, ammonia nitrogen :≤1mg/L.This result illustrates that native system is to COD cr, the larger molecular organics that especially difficulty such as unit phenol and polyphenol is decomposed has significant reducing effect.
embodiment 2
The present embodiment is for illustration of the screening of the present invention to ozone dosage.
Contriver finds that the dosage of ozone can affect the treatment effect of waste water.Therefore, inventors have investigated the impact of ozone on process results of different dosage.The operation steps of the present embodiment and other parameters substantially the same manner as Example 1, unlike the dosage of ozone in chemical catalysis unit.Testing data is as shown in table 1 below.
The dosage of table 1 ozone is on the impact of water treatment effect
Note:
*: refer to that ultra filtration unit pressure reduction rises fast, need frequent backwash and cleaning, and the cleaning interval is short;
*: on the basis of ozone dosage, adds supersound process (ultrasonic frequency: 25 ~ 35kHz).
The above results illustrate when ozone dosage 25mg/L and above time, obviously can improve operating flux and the backwash cycle of film separation unit (as ultra filtration unit).Although and the COD of chemical catalysis also can be increased more than the dosage of 100mg/L crclearance, but high cost, economy is poor.In addition, contriver finds, after introducing supersound process, even if the dosage of ozone is lower, also can obtain extraordinary COD crremoval effect.
embodiment 3
The present embodiment is for illustration of the screening of the present invention to the filtrate of biological aerated filter.
Contriver is investigated different filtrates in biological aerated filter unit to the impact for the treatment of effect.Equally, the operation steps of the present embodiment and other parameters substantially the same manner as Example 1, unlike the kind of filtrate in biological aerated filter unit.Testing data is as shown in table 2 below.
Table 2 filtrate kind is on the impact of water treatment effect
Note:
*: mainly refer to that particle diameter is 3 ~ 5mm, mean pore size is the activated coke of 4 ~ 16nm;
*: refer to that ultrafiltration system pressure reduction rises fast, need frequent backwash and cleaning, and the cleaning interval is short.
The above results shows, select activated coke as filtrate (carrier) at biological aerated filter unit, than using haydite and gac, there is better CODcr removal effect, and can ensure that film separation unit (as ultra filtration unit) has larger operating flux and longer backwash cycle, make system cloud gray model more stable, efficiency is higher.
Although present invention has been description to a certain degree, significantly, under the condition not departing from the spirit and scope of the present invention, can carry out the suitable change of each condition.Be appreciated that and the invention is not restricted to described embodiment, and be attributed to the scope of claim, it comprises the equivalent replacement of described each factor.

Claims (16)

1. a crushed coal pressure gasifying method of wastewater treatment, is characterized in that, described treatment process sequentially comprises:
(1) waste water is carried out coagulating sedimentation, obtain the waste water after coagulating kinetics;
(2) waste water that above-mentioned steps (1) obtains is carried out chemical catalysis, obtain the waste water after catalytic oxidation treatment;
(3) waste water that above-mentioned steps (2) obtains is carried out biological aerated filter, obtain the waste water after biological aerated filter process;
(4) waste water that above-mentioned steps (3) obtains is carried out membrane sepn, obtain discharging/reuse water;
Described step (1) comprising: in waste water, add flocculation agent react, and precipitation, gets supernatant liquid, obtain the waste water after described coagulating kinetics; Described flocculation agent is polymerize aluminum chloride, and its dosage is 350 ~ 400mg/L;
Described step (2) comprising: in the waste water that step (1) obtains, add strong oxidizer react, obtain the waste water after described catalytic oxidation treatment; Described strong oxidizer is ozone, and the dosage of described ozone is 50 ~ 75mg/L, and the reaction times adding ozone is 30 ~ 90min; Carry out supersound process adding while strong oxidizer carries out reacting, the ultrasonic frequency of described supersound process is 25 ~ 35kHz;
Described step (3) comprising: waste water step (2) obtained interacts with the filtrate being loaded with microorganism in BAF, and by continuing aeration effect, obtain the waste water after described biological aerated filter process, described filtrate is activated coke filtrate, the particle diameter of described activated coke filtrate is 3 ~ 5mm, mean pore size is 4 ~ 16nm, and the pack density of described filtrate is 0.5 ~ 0.6g/cm 3, the empty bed residence time of described BAF is 6 ~ 8h.
2. method according to claim 1, is characterized in that, in step (1), adding the reaction times after described flocculation agent is 30 ~ 60min, and sedimentation time is 3 ~ 5h.
3. method according to claim 1 and 2, is characterized in that, in step (4), described membrane sepn comprises uf processing and reverse-osmosis treated.
4. method according to claim 3, is characterized in that, described uf processing adopts external pressure type ultra-filtration membrane to carry out.
5. method according to claim 4, is characterized in that, the material of described ultra-filtration membrane is PVDF, and filtering accuracy is 0.03 micron, and operating pressure is 0.08 ~ 0.20MPa, and filtration flux is 20 ~ 60L/m 2h.
6. method according to claim 4, is characterized in that, the filtration flux of described ultra-filtration membrane is 25 ~ 45L/m 2h.
7. method according to claim 3, is characterized in that, described reverse-osmosis treated adopts pollution-resistant reverse osmosis membrane to carry out.
8. method according to claim 1 and 2, is characterized in that, before the method is also included in step (4), carries out multi-medium filtering to the waste water that step (3) obtains.
9. method according to claim 8, is characterized in that, the filtrate adopted in described multi-medium filtering comprises hard coal and quartz sand.
10., for a crushed coal pressure gasifying Waste Water Treatment for method according to any one of claim 1 to 9, it is characterized in that, this system comprises the coagulating sedimentation unit, chemical catalysis unit, biological aerated filter unit and the film separation unit that sequentially connect.
11. systems according to claim 10, is characterized in that, described film separation unit comprises ultra filtration unit and reverse osmosis units.
12. systems according to claim 10 or 11, is characterized in that, be also provided with multi-medium filtering unit between described biological aerated filter unit and film separation unit.
13. systems according to claim 10 or 11, it is characterized in that, described chemical catalysis unit is provided with device for absorbing tail gas.
14. systems according to claim 13, is characterized in that, are filled with carbon leaching material in described device for absorbing tail gas.
15. systems according to claim 14, is characterized in that, the filling ratio of described carbon leaching material is 30 ~ 40%v/v.
16. methods according to any one of claim 1 to 9 or the application of the system according to any one of claim 10 to 15 in process crushed coal pressure gasifying waste water.
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