CN103288309B - Coal gasification wastewater zero-emission treatment method, and application thereof - Google Patents
Coal gasification wastewater zero-emission treatment method, and application thereof Download PDFInfo
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Abstract
The invention provides a coal gasification wastewater zero-emission treatment method, a treatment system and an application thereof. The treatment system provided by the invention can respectively perform biochemical treatment, desalting and concentrated saline treatment on coal gasification wastewater through a biochemical treatment unit, a desalting unit and a concentrated saline treatment unit, clear water produced by each step can be reused, the produced high-salinity concentrated water can enter the next step for treatment, evaporation is finally performed through an evaporation unit, the clear water produced after evaporation can be used for water supply of a boiler, and the produced concentrated water can be used for flushing ash and slag. The treatment system provided by the invention can realize wastewater zero-emission treatment so as to achieve the purpose of saving water resources.
Description
Technical field
The invention belongs to technical field of sewage.Particularly, the present invention relates to a kind of coal gasification waste water treatment technology, particularly a kind for the treatment of process of coal gasification waste water zero release, treatment system and application thereof.
Background technology
In the waste water producing in Coal Gasification Technology process, contain the heterogeneous ring compound of a large amount of ammonia nitrogens, aldehydes matter, mononuclear aromatics and polycyclic aromatic hydrocarbons and nitrogenous, sulphur, oxygen, also have part oils and prussiate, COD
cr(adopt potassium bichromate (K
2cr
2o
7) chemical oxygen demand that determines as oxygenant) dense.Coal gasification waste water has the features such as wastewater discharge is large, Persistent organic pollutants concentration is high, intractability is large, is one of difficult trade effluent of generally acknowledging.
For the processing of current coal gasification waste water, be conventionally divided into coagulation, second-stage treatment and advanced treatment.Coagulation is pre-treatment, payes attention to the recovery of valuable material, comprises the unit such as absorption, precipitation, extraction, stripping; Second-stage treatment is mainly biochemical treatment, biochemical processing process is the core of whole coal gasification waste water processing, biochemical processing process mainly contains activated sludge process, anoxic/aerobic method (is Anacrobic/Oxic, be called for short AO method), sequencing batch active sludge (be Sequencing Batch Reactor Activated Sludge Process, be called for short SBR method) and combination process thereof etc.; The common method of advanced treatment is Fenton reagent method, Ozonation, flocculent precipitation, membrane treatment process etc.But adopt above-mentioned biochemical processing process to carry out biochemical treatment, owing to containing a large amount of hard-degraded substances such as phenyl ring and heterocyclic in water, can cause bio-chemical effluent COD
crdense.And after biochemical treatment, adopt the above-mentioned techniques such as activated carbon filter process, Ozonation, flocculent precipitation to carry out advanced treatment, because the suspended substance in water, colloid and organic concentration are still very high, thereby make running cost high, and effluent quality is still very high.Therefore, mainly taking qualified discharge as main, can not realize the cyclically utilizing of waste water for the processing of such waste water.
At present, the coal gasification waste water treatment technology that can realize reuse has been reported.For example, Chinese patent CN101857331B discloses a kind of coal chemical industry wastewater zero emission treatment method and system, and it has mainly utilized activated coke filter bed, adsorbs by activated coke, the most of organism of absorption degradation, has reduced the follow-up membrane treatment process film Pollution risk that enters.But the adsorptive power of activated coke is limited, not only cause backwash frequency high, become new secondary pollutant but also produce a large amount of useless Jiao.This invention does not consider that coal gas waste has the advantages that the water yield is large yet, adopt the waste water water yield producing after membrane sepn still very large, can only there is part waste water to go desulphurization system, also have greatly and do not process, also caused the running cost of production technique high simultaneously, and the defect of fluctuation of service.Chinese patent CN101560045A discloses a kind of coal chemical wastewater treating technique, this technique be mainly before biochemical treatment, to adopt Fenton reagent and ozone catalytic agent, utilize the redoxomorphism of Fenton reagent and ozone catalytic agent, phenols in waste water, the degraded of polycyclic aromatic hydrocarbons substance oxidation are removed, but owing to thering is high organism, high chroma, high suspended matter feature through the pretreated water outlet of air supporting, and the organism in water had both contained the macromole such as phenols, polycyclic aromatic hydrocarbons hardly degraded organic substance, also contain a large amount of small molecules easily biodegradable organicses.Therefore, disturbed by high chroma, high suspended matter, small organic molecule, adopt and before pre-treatment, use Fenton reagent and ozone catalytic agent, can not play good removal hardly degraded organic substance effect, and add a large amount of Fenton reagents and can increase a large amount of salts substances, especially the sulfate radical content in water increases, and can directly affect the operation of subsequent film treatment process.And because ozone has germicidal action, the water outlet after ozonize can directly be killed the microorganism in follow-up active sludge aeration tank owing to containing remaining ozone, thereby has also limited biological treatment ability.Meanwhile, the shortcoming that coal gasification waste water water production rate is large is not considered in the same existence of this invention, causes and directly adopts evaporative crystallization processing can cause cost of investment large reverse osmosis waste water, and running cost is also high, has limited the extensive popularization of technique.
Summary of the invention
For above-mentioned technological deficiency, an object of the present invention is to provide a kind of coal gasification waste water Zero discharge treatment method, another object of the present invention is to provide a kind of coal gasification waste water zero-discharge treatment system, and a further object of the present invention is to provide the purposes of a kind of above-mentioned treatment process and treatment system.Treatment process of the present invention and treatment system have taken into full account the large problem of coal gasification waste water quantity discharged, and the thinking that has adopted the water yield to successively decrease step by step reaches the object of saving water resource.
Except as otherwise noted, term " desalination " refers to the processing that the dissolved solid in coal gasification waste water is removed in the present invention.
Except as otherwise noted, term " strong brine " refers to by desalination and processes the waste water producing after the solid substance dissolving in coal gasification waste water is concentrated in the present invention.
Except as otherwise noted, term " the dense water of high salt " refers to by strong brine and processes the waste water producing after the dissolved solid in strong brine is further concentrated in the present invention.
Except as otherwise noted, the waste water producing when term " backwash water " refers in the second ultrafiltration system, BAF, more medium filter, filtration with manganese sand device and the first ultrafiltration system operational process regularly backwash in the present invention.
On the one hand, the invention provides a kind for the treatment of process of coal gasification waste water zero release, the method comprises the following steps:
(1) coal gasification waste water is carried out to biochemical treatment, obtain the waste water after biochemical treatment;
(2) waste water obtaining in step (1) is carried out to desalination, obtain desalination strong brine after treatment and water purification;
(3) strong brine obtaining in step (2) is carried out to strong brine processing, obtain the strong brine dense water of high salt after treatment and water purification; Preferably, described strong brine processing is carried out in strong brine processing unit, and more preferably, described strong brine processing unit comprises the lime settling pond, more medium filter, the first ultrafiltration system, nanofiltration system and the first reverse osmosis system that are communicated with successively;
(4) the dense water of high salt obtaining in step (3) is evaporated, obtain dense water and water purification after evaporation process.
According to method of the present invention, the biochemical treatment described in step (1) is preferably carried out in biochemical treatment unit, and more preferably, described biochemical treatment unit comprises the anaerobic pond, anoxic pond, Aerobic Pond and the settling tank that are communicated with successively; Further preferably, hydraulic detention time in described anaerobic pond is 18～24 hours, more preferably, hydraulic detention time in described anoxic pond is 12～24 hours, again preferably, hydraulic detention time in described Aerobic Pond is 40～72 hours, and most preferably, the hydraulic detention time in described settling tank is 4～8 hours; Further preferably, the sludge concentration in described Aerobic Pond is 3～4g/L, more preferably, oxyty in described Aerobic Pond is 2～3mg/L, more preferably, the nitrification liquid reflux ratio in described Aerobic Pond is 50～100%, most preferably, the return sludge ratio in described settling tank is 100～200%.
According to method of the present invention, desalination described in step (2) preferably carries out in desalination unit, more preferably, described desalination unit comprises the coagulative precipitation tank that adds coagulating agent, the ozone oxidation reaction device that adds ozone, BAF, the second ultrafiltration system and the second reverse osmosis system that are communicated with successively, again preferably, described coagulating agent is one or more in polymerize aluminum chloride, poly-ferric chloride and Tai-Ace S 150, and most preferably, described coagulating agent is polymerize aluminum chloride; Further preferably, the dosage of described coagulating agent is 350～400mg/L, and more preferably, the dosage of described ozone is 80～120mg/L, and most preferably, the filtrate in described BAF is ceramic grain filter; Still more preferably, described the second ultrafiltration system is immersion ultrafiltration system, and more preferably, described the second ultrafiltration system comprises self-cleaning filter, more preferably, the filtration flux of described the second ultrafiltration system is 10～50L/m
2h, most preferably, the filtration flux of described the second ultrafiltration system is 20～40L/m
2h; Again further preferably, the reverse osmosis membrane in described the second reverse osmosis system is pollution-resistant reverse osmosis membrane, and more preferably, the rate of recovery of described the second reverse osmosis system is 65～75%; Again further preferably, hydraulic detention time in described coagulative precipitation tank is 3.5～6 hours, and more preferably, the hydraulic detention time in described ozone oxidation reaction device is 1～2 hour, most preferably, the empty bed residence time in described BAF is 6～8 hours.
According to method of the present invention, in step (3), preferably, in described lime settling pond, add the unslaked lime that bodied ferric sulfate that dosage is 100～300mg/L and dosage are 150～250mg/L, more preferably, the filtering velocity of described more medium filter is 8～15m/h; Further preferably, the filtration flux of described the first ultrafiltration system is 15～45L/m
2h, is preferably 25～30L/m
2h, more preferably, the rate of recovery of described the first reverse osmosis system is 70～80%, more preferably, the pH value of the water inlet of described reverse osmosis system is 9～10, most preferably, the rate of recovery of described nanofiltration system is 70～80%.
In a preferred embodiment of the method for the invention, described strong brine processing unit also comprises filtration with manganese sand device, and preferably, described filtration with manganese sand device is communicated between described more medium filter and the first ultrafiltration system, more preferably, the filtering velocity of described filtration with manganese sand device is 8～10m/h.
According to method of the present invention, the evaporation described in step (4) is carried out in vaporizer, and preferably, the rate of recovery of described evaporation is greater than 90%.
In another preferred embodiment of the method for the invention, described method can also comprise step (1 ') before in step (1): coal gasification waste water is carried out to pre-treatment, preferably, described pre-treatment is carried out in pretreatment unit, and more preferably, described pretreatment unit comprises equalizing tank, again preferably, in described equalizing tank, be provided with whipping appts, most preferably, the hydraulic detention time in described equalizing tank is 12～24 hours.
In above-mentioned preferred embodiment, can first coal gasification waste water be passed into equalizing tank, in equalizing tank, be provided with agitator, pass through mechanical agitation, the water quality that guarantee enters biochemical treatment unit is even, stable, water outlet in described equalizing tank enters anoxic pond by pipeline enter the anaerobic pond of biochemical treatment unit by pipeline after more successively, Aerobic Pond, water outlet in Aerobic Pond is back to anoxic pond according to certain nitrification liquid reflux ratio, rest part enters settling tank, by biological respinse, the most organic pollutants in waste water are removed by microbial process absorption degradation.
On the other hand, the present invention also provides a kind for the treatment of system of coal gasification waste water zero release, this system comprises: biochemical treatment unit, desalination unit, strong brine processing unit and evaporation element, preferably, described biochemical treatment unit comprises the anaerobic pond being communicated with successively, anoxic pond, Aerobic Pond and settling tank, more preferably, described desalination unit comprises the coagulative precipitation tank being communicated with successively, ozone oxidation reaction device, BAF, the second ultrafiltration system and the second reverse osmosis system, most preferably, described strong brine processing unit comprises the lime settling pond being communicated with successively, more medium filter, the first ultrafiltration system, nanofiltration system and the first reverse osmosis system, further preferably, described the second ultrafiltration system is immersion ultrafiltration system, and more preferably, described the second ultrafiltration system comprises self-cleaning filter, and most preferably, described evaporation element comprises vaporizer.
In a preferred embodiment of system of the present invention, described system also comprises pretreatment unit, preferably, described pretreatment unit is communicated with biochemical treatment unit, and more preferably, described pretreatment unit comprises equalizing tank, most preferably, in described equalizing tank, be provided with whipping appts.
In another preferred embodiment for the treatment of system of the present invention, described strong brine processing unit also comprises filtration with manganese sand device, and described filtration with manganese sand device is communicated between more medium filter and the first ultrafiltration system.
On the one hand, the present invention also provides treatment process of the present invention and the application for the treatment of system in gas treatment waste water again.
Below by a preferred embodiment of the present invention, the present invention is made to further description:
Coal gasification waste water is passed in the equalizing tank that inside is provided with whipping appts and carries out pre-treatment, by the mechanical agitation of whipping appts, make water quality evenly, stable;
Then the water outlet in equalizing tank delivers into anaerobic pond, anoxic pond, the Aerobic Pond of biochemical treatment unit successively by pipeline, water outlet in Aerobic Pond is back to anoxic pond by certain nitrification liquid reflux ratio, rest part enters settling tank, in biochemical treatment unit, by biological respinse, the most organic pollutants in waste water is removed by microbial process absorption degradation; Water outlet in settling tank is back to anoxic pond by certain return sludge ratio, and rest part enters desalination unit;
Desalination unit is for by the inorganic salts separating substances of the waste water after described biochemical treatment out, and the water purification of generation can reuse, collects the strong brine producing, for next processing unit; In the coagulative precipitation tank of desalination unit, remove suspended substance and the partial organic substances in water by coagulation; Water outlet in coagulative precipitation tank delivers into ozone oxidation reaction device by pipeline, by the hardly degraded organic substance in waste water under oxygenant effect, by complete oxidation or change the small organic molecule of readily biodegradable into; Water outlet in ozone oxidation reaction device enters in BAF, utilize ozone catalytic agent strong oxidizing property feature, hard-degraded substance in water after biochemical processing process is oxidized to the material of easy degraded, utilize filtration and the microbial process of BAF, the removal of further organism in waste water being degraded, has reduced to large extent and has entered organic loading in film system; In BAF, water outlet delivers into the second ultrafiltration system by pipeline, the second ultrafiltration system comprises self-cleaning filter, for the treatment of the large particulate matter in water inlet, prevention damages ultra-filtration membrane, the effect of ultrafiltration is to hold back the materials such as bacterium in waste water, colloid, suspended substance, water is produced in ultrafiltration can reuse, also can directly enter the second reverse osmosis system and carry out desalination, the water purification that the second reverse osmosis system produces can reuse, the backwash water of the backwash water of the second ultrafiltration system and BAF can also be returned to coagulative precipitation tank and again process;
The strong brine again the second reverse osmosis system being produced delivers into strong brine processing unit by pipeline, for the strong brine of described desalination unit is further processed, the water purification obtaining after processing can reuse, collects the dense water of high salt producing, for next processing unit; First strong brine enters lime settling pond, under the unslaked lime, flocculation agent (as polyiron sulfate), coagulant aids (as polyacrylamide) acting in conjunction that add, can not only remove hardness, basicity and organism, suspended substance in water, can also play germicidal action; Water outlet in lime settling pond enters into more medium filter, further removes the material such as suspended substance and part heavy metal in water; Water outlet in more medium filter enters into filtration with manganese sand device or directly enters into the first ultrafiltration system, nanofiltration system and the first reverse osmosis system, and adopting filtration with manganese sand device is in order to remove the iron in waste water, and the water purification that the first reverse osmosis system produces can reuse; The backwash water of more medium filter, filtration with manganese sand device and/or the first ultrafiltration system can also be returned to lime settling pond and again process, the dense water of high salt that nanofiltration system is produced passes into evaporation element;
Finally the water outlet in strong brine processing unit (being the dense water of high salt) is delivered into evaporation element, by vaporizer, the material such as salt, organism in dense high salt water is further concentrated, water purification after evaporation can be used as boiler feedwater, and the dense water that evaporation obtains can be for rushing grey flushing cinder.
Compared with prior art, at least there is following beneficial effect in the present invention:
(1) treatment process of the present invention has not only been avoided the secondary pollutant that uses Fenton reagent and ozone catalytic agent and activated coke filter bed to produce, and can also realize the zero release of coal gasification waste water, thereby reach the object of saving water resource;
(3) the present invention, by coal gasification waste water stepwise disposal, has reduced the water yield that enters evaporation process, and then has reduced cost of investment and the running cost of evaporation process, particularly in the present invention, effectively reduce the calcium in the waste water that enters the first reverse osmosis system, the fouling tendency divalent ions such as magnesium, for follow-up reverse osmosis treatment system has reduced inorganic salt fouling risk, and in feed water by reverse osmosis system, regulate water inlet pH value to 9～10, it is moved in alkaline environment, reduce the Pollution risk of organism to reverse osmosis membrane in water, greatly improve the operation stability of reverse osmosis system, significantly improved the rate of recovery of reverse osmosis system simultaneously, the rate of recovery can reach this rate of recovery of 70～80%(even unexpectedly can be higher than the rate of recovery of the second reverse osmosis system), reduce significantly the water yield that enters evaporation process,
(3) technological operation of the present invention is simple, convenient management, and running cost is low.
Brief description of the drawings
Below, describe by reference to the accompanying drawings embodiment of the present invention in detail, wherein:
Fig. 1 adopts treatment system of the present invention to carry out the schematic flow sheet of an embodiment of coal gasification waste water zero discharge treatment;
Fig. 2 adopts the biochemical treatment unit for the treatment of system of the present invention to carry out the schematic flow sheet of an embodiment of biochemical treatment;
Fig. 3 adopts the desalination unit for the treatment of system of the present invention to carry out the schematic flow sheet of an embodiment of desalination processing;
Fig. 4 adopts the strong brine processing unit for the treatment of system of the present invention to carry out the schematic flow sheet of an embodiment of strong brine processing;
Fig. 5 adopts the strong brine processing unit for the treatment of system of the present invention to carry out the schematic flow sheet of another embodiment of strong brine processing;
Fig. 6 adopts treatment system of the present invention to carry out the schematic flow sheet of another embodiment of coal gasification waste water zero discharge treatment;
Fig. 7 adopts the pretreatment unit for the treatment of system of the present invention to carry out the schematic flow sheet of pretreated another embodiment.
description of reference numerals:
1-coal gasification waste water, 2-biochemical treatment unit, 3-desalination unit, 4-strong brine processing unit, 5-evaporation element, the dense water of 6-, 7, 8, 9-water purification, 10-equalizing tank, 11-anaerobic pond, 12-anoxic pond, 13-Aerobic Pond, 14-settling tank, 15-waste water, 16-coagulative precipitation tank, 17-ozone oxidation reaction device, 18-BAF, 19-the second ultrafiltration system, 20-the second reverse osmosis system, 21, 22, 30, 31, 34-backwash water, 23-strong brine, 24-lime settling pond, 25-more medium filter, 26-the first ultrafiltration system, 27-nanofiltration system, 28-the first reverse osmosis system, 29, the dense water of the high salt of 34-, 32-pretreatment unit, 33-filtration with manganese sand device.
Embodiment
Below in conjunction with embodiment, the present invention is described in further detail, the embodiment providing is only in order to illustrate the present invention, instead of in order to limit the scope of the invention.
embodiment 1
As shown in Figure 1, treatment system of the present invention comprises biochemical treatment unit (2), desalination unit (3), strong brine processing unit (4) and the evaporation element (5) that contains vaporizer.
As shown in Figure 2, described biochemical treatment unit (2) comprise the anaerobic pond (11), anoxic pond (12), Aerobic Pond (13) and the settling tank (14) that are communicated with successively.
As shown in Figure 3, described desalination unit (3) comprises the coagulative precipitation tank that adds coagulating agent (16) being communicated with successively, (for example add the ozone oxidation reaction device (17) of ozone, inner circular tower structure ozone oxidation reaction device of filling 30% active carbon filler), BAF (18) (for example inner BAF that is filled with ceramic grain filter), the second ultrafiltration system (19) (for example comprises self-cleaning filter, ultra-filtration membrane can adopt the immersion ultrafiltration system (GE Zeed500d) of PVDF material) and the second reverse osmosis system (20) (for example adopting the reverse osmosis membrane of the wide runner film of resistance to crocking (BW30FR～400/34i)).
As shown in Figure 4, described strong brine processing unit (4) comprises that (for example ultra-filtration membrane can adopt external-compression type ultrafiltration (as Tao Shi SFP2860) to lime settling pond (24), more medium filter (25), filtration with manganese sand device (33), the first ultrafiltration system (26) being communicated with successively, PVDF material), nanofiltration system (27) (for example, nanofiltration membrane model can for DURASLICK NF8040) and the first reverse osmosis system (28) (reverse osmosis membrane can adopt the wide runner film of resistance to crocking (BW30FR～400/34i)).
In the time that the treatment system that adopts the present embodiment is carried out coal gasification waste water (1) zero discharge treatment, treatment process can be carried out as follows:
A. coal gasification waste water (1) first enters after anaerobic pond (11), anoxic pond (12), Aerobic Pond (13), settling tank (14) successively by pipeline, the waste water (15) producing enters desalination unit (3) successively by pipeline, the water outlet of Aerobic Pond (13) is back to anoxic pond (12) according to certain nitrification liquid reflux ratio, and the water outlet of settling tank (14) is back to anoxic pond (12) according to certain return sludge ratio;
B. in desalination unit (3), waste water (15) enters coagulative precipitation tank (16), ozone oxidation reaction device (17), BAF (18), the second ultrafiltration system (19), the second reverse osmosis system (20) successively, the water purification (7) producing is exported reuse by pipeline, the backwash water (21) that the backwash water (22) that the second ultrafiltration system (19) produces and BAF (18) produce is delivered to coagulative precipitation tank (16) ingress by pipeline and carries out re-treatment, and the strong brine (23) of generation enters strong brine processing unit (4);
C. in strong brine processing unit (4), strong brine (23) enters lime settling pond (24) successively by pipeline, more medium filter (25), filtration with manganese sand device (33), the first ultrafiltration system (26), nanofiltration system (27), the first reverse osmosis system (28), the backwash water (31) that the first ultrafiltration system (26) produces, the backwash water (30) that the backwash water (34) that filtration with manganese sand device (33) produces and more medium filter (25) produce is delivered to lime settling pond (24) front end by pipeline, again process, the water purification (8) producing is transmitted back to use by pipeline, the dense water of high salt (29) that the dense water of high salt (34) that nanofiltration system produces and the first reverse osmosis system produce enters evaporation element (5),
D. in evaporation element (5), the dense water of high salt (29) and the dense water of high salt (34) are directly delivered in vaporizer by pipeline, by the evaporation concentration effect of vaporizer, and the water purification of generation (9) reuse, the dense water (6) of generation can be used for rushing grey flushing cinder.
In the time that the treatment process that adopts the present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can adopt following parameter to carry out:
Hydraulic detention time in anaerobic pond (11): 24h,
Hydraulic detention time in anoxic pond (12): 24h,
Hydraulic detention time in Aerobic Pond (13): 72h, sludge concentration: 4g/L, oxyty: 2g/L, water inlet pH value: 7～8, nitrification liquid reflux ratio: 100%,
Hydraulic detention time in settling tank (14): 8h, return sludge ratio: 200%,
Hydraulic detention time in coagulative precipitation tank (16): 6h, the dosage of coagulant polymeric aluminium chloride: 400mg/L,
Hydraulic detention time in ozone oxidation reaction device (17): 2h, ozone dosage: 120mg/L,
The empty bed residence time: 8h in BAF (18),
The filtration flux of the second ultrafiltration system (19): 30L/ (m
2.h), the water purification rate of recovery of the second ultrafiltration system: 90%,
The water purification rate of recovery of the second reverse osmosis system (20): 75%,
Hydraulic detention time in lime settling pond (24): 2h, the dosage of bodied ferric sulfate: 150mg/L, the dosage of unslaked lime: 200mg/L, controls water outlet pH value in 10.3 left and right,
The water inlet of more medium filter (25) is by salt acid for adjusting pH to 7～8, and filtering velocity is 10m/h, and upper strata is 1～2mm hard coal, and lower floor is 0.8～1.2mm quartz sand,
The filtering velocity of filtration with manganese sand device (33): 10m/h,
The filtration flux of the first ultrafiltration system (26): 30L/ (m
2.h), the water purification rate of recovery of the first ultrafiltration system: 80%,
Nanofiltration system (27) rate of recovery: 80%,
The water inlet pH value of the first reverse osmosis system (28) is controlled at 10.0 left and right, the water purification rate of recovery of the first reverse osmosis system: 80%,
The evaporation water purification rate of recovery: 90%.
The effluent quality analytical data in different treatment stage in table 1 embodiment 1
Note: system total yield refers to obtained total water purification amount and the ratio of total inflow
embodiment 2
As the replacement of strong brine processing unit described in embodiment 1 (4), the present invention can also adopt strong brine processing unit (4) as shown in Figure 5 to carry out strong brine processing.
As shown in Figure 5, this strong brine processing unit (4) has omitted the filtration with manganese sand device (33) being communicated between more medium filter (25) and the first ultrafiltration system (26).
In the time adopting the treatment system of the present embodiment to carry out coal gasification waste water (1) zero discharge treatment, can be undertaken by the step a in embodiment 1, b and d.As shown in Figure 5, in the time of implementation step c, the water outlet of more medium filter (25) directly can be passed into the first ultrafiltration system (26).
In the time that the treatment process that adopts the present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can adopt following parameter to carry out:
Hydraulic detention time in anaerobic pond (11): 18h,
Hydraulic detention time in anoxic pond (12): 12h,
Hydraulic detention time in Aerobic Pond (13): 40h, sludge concentration: 4g/L, oxyty: 2g/L, water inlet pH value: 7～8, nitrification liquid reflux ratio: 50%,
Hydraulic detention time in settling tank (14): 4h, return sludge ratio: 100%,
Hydraulic detention time in coagulative precipitation tank (16): 3.5h, the dosage of coagulant polymeric iron(ic) chloride: 350mg/L,
Hydraulic detention time in ozone oxidation reaction device (17): 2h, ozone dosage: 80mg/L,
The empty bed residence time: 7h in BAF (18),
The filtration flux of the second ultrafiltration system (19): 10L/ (m
2.h), the water purification rate of recovery of the second ultrafiltration system: 90%,
The water purification rate of recovery of the second reverse osmosis system (20): 65%,
Hydraulic detention time in lime settling pond (24): 2h, the dosage of bodied ferric sulfate: 100mg/L, the dosage of unslaked lime: 200mg/L, controls water outlet pH value in 10.3 left and right,
The water inlet of more medium filter (25) is by salt acid for adjusting pH to 7～8, and filtering velocity is 8m/h, and upper strata is 1～2mm hard coal, and lower floor is 0.8～1.2mm quartz sand,
The filtration flux of the first ultrafiltration system (26): 15L/ (m
2.h), the water purification rate of recovery of the first ultrafiltration system: 80%,
Nanofiltration system (27) rate of recovery: 70%,
The water inlet pH value of the first reverse osmosis system (28) is controlled at 9.0 left and right, the water purification rate of recovery of the first reverse osmosis system: 70%,
The evaporation water purification rate of recovery: 90%.
The effluent quality analytical data in different treatment stage in table 2 embodiment 2
Note: system total yield refers to obtained water purification amount and the ratio of total inflow.
embodiment 3
As shown in Figure 6, the present invention can also adopt pretreatment unit (32) to carry out pre-treatment to coal gasification waste water (1).
As shown in Figure 7, described pretreatment unit (32) comprises that the inside being communicated with anaerobic pond (11) is provided with the equalizing tank (10) of whipping appts.
In the time adopting the treatment system of the present embodiment to carry out coal gasification waste water (1) zero discharge treatment, can be undertaken by the step b in embodiment 2, c and d.As shown in Figure 7, in the time of implementation step a, coal gasification waste water (1) first need to be passed into equalizing tank (10) and pass into again anaerobic pond (11).
In the time that the treatment process that adopts the present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can adopt following parameter to carry out:
Hydraulic detention time in equalizing tank (10): 20h,
Hydraulic detention time in anaerobic pond (11): 20h,
Hydraulic detention time in anoxic pond (12): 18h,
Hydraulic detention time in Aerobic Pond (13): 60h, sludge concentration: 3g/L, oxyty: 3g/L, water inlet pH value: 7～8, nitrification liquid reflux ratio: 80%,
Hydraulic detention time in settling tank (14): 7h, return sludge ratio: 150%,
Hydraulic detention time in coagulative precipitation tank (16): 5h, the dosage of aluminum sulfate coagulant: 380mg/L,
Hydraulic detention time in ozone oxidation reaction device (17): 1h, ozone dosage: 100mg/L,
The empty bed residence time: 6h in BAF (18),
The filtration flux of the second ultrafiltration system (19): 50L/ (m
2.h), the water purification rate of recovery of the second ultrafiltration system: 90%,
The water purification rate of recovery of the second reverse osmosis system (20): 70%,
Hydraulic detention time in lime settling pond (24): 2h, the dosage of bodied ferric sulfate: 300mg/L, the dosage of unslaked lime: 200mg/L, controls water outlet pH value in 10.3 left and right,
The water inlet of more medium filter (25) is by salt acid for adjusting pH to 7～8, and filtering velocity is 15m/h, and upper strata is 1～2mm hard coal, and lower floor is 0.8～1.2mm quartz sand,
The filtration flux of the first ultrafiltration system (26): 45L/ (m
2.h), the water purification rate of recovery of the first ultrafiltration system: 80%,
Nanofiltration system (27) rate of recovery: 75%,
The water inlet pH value of the first reverse osmosis system (28) is controlled at 9.5 left and right, the water purification rate of recovery of the first reverse osmosis system: 75%,
The evaporation water purification rate of recovery: 90%.
The effluent quality analytical data in different treatment stage in table 3 embodiment 3
Note: system total yield refers to obtained water purification amount and the ratio of total inflow.
Although the present invention describes in detail; but should be appreciated that foregoing description is not in order to limit the present invention, without departing from the spirit and scope of the present invention; any amendment of doing, be equal to replacement, improvement etc., within protection scope of the present invention all should be included in.
Claims (6)
1. a treatment process for coal gasification waste water zero release, the method comprises the following steps:
(1) coal gasification waste water is carried out to biochemical treatment, obtain the waste water after biochemical treatment;
(2) waste water obtaining in step (1) is carried out to desalination, obtain strong brine and water purification after desalination;
(3) strong brine obtaining in step (2) is carried out to strong brine processing, obtain the strong brine dense water of high salt after treatment and water purification, described strong brine processing is carried out in strong brine processing unit, and described strong brine processing unit comprises the lime settling pond, more medium filter, the first ultrafiltration system, nanofiltration system and the first reverse osmosis system that are communicated with successively;
(4) the dense water of high salt obtaining in step (3) is evaporated, obtain dense water and water purification after evaporation process;
Wherein,
Biochemical treatment described in step (1) is carried out in biochemical treatment unit, described biochemical treatment unit comprises the anaerobic pond, anoxic pond, Aerobic Pond and the settling tank that are communicated with successively, hydraulic detention time in described anaerobic pond is 18～24 hours, hydraulic detention time in described anoxic pond is 12～24 hours, hydraulic detention time in described Aerobic Pond is 40～72 hours, and the hydraulic detention time in described settling tank is 4～8 hours; Sludge concentration in described Aerobic Pond is 3～4g/L, and the oxyty in described Aerobic Pond is 2～3mg/L, and the nitrification liquid reflux ratio in described Aerobic Pond is 50～100%, and the return sludge ratio in described Aerobic Pond is 100～200%;
Desalination described in step (2) carries out in desalination unit, described desalination unit comprises the coagulative precipitation tank that adds coagulating agent, the ozone oxidation reaction device that adds ozone, BAF, the second ultrafiltration system and the second reverse osmosis system that are communicated with successively, described coagulating agent is one or more in polymerize aluminum chloride, poly-ferric chloride and Tai-Ace S 150, the dosage of described coagulating agent is 350～400mg/L, the dosage of described ozone is 80～120mg/L, and the filtrate in described BAF is ceramic grain filter; Described the second ultrafiltration system is immersion ultrafiltration system, and described the second ultrafiltration system comprises self-cleaning filter, and the filtration flux of described the second ultrafiltration system is 10～50L/m
2h; Reverse osmosis membrane in described the second reverse osmosis system is anti-soil type reverse osmosis membrane, and the rate of recovery of described the second reverse osmosis system is 65～75%;
In step (3), in described lime settling pond, add the unslaked lime that bodied ferric sulfate that dosage is 100～300mg/L and dosage are 150～250mg/L, the filtering velocity of described more medium filter is 8～15m/h; The filtration flux of described the first ultrafiltration system is 15～45L/m
2h, the rate of recovery of described the first reverse osmosis system is 70～80%, and the pH value of the water inlet of described the first reverse osmosis system is 9～10, and the rate of recovery of described nanofiltration system is 70～80%;
Evaporation described in step (4) is carried out in evaporation element, and described evaporation element comprises vaporizer, and the rate of recovery of described evaporation is greater than 90%;
Described method can also comprise step (1 ') before in step (1): coal gasification waste water is carried out to pre-treatment, described pre-treatment is carried out in pretreatment unit, described pretreatment unit comprises equalizing tank, in described equalizing tank, be provided with whipping appts, the hydraulic detention time in described equalizing tank is 12～24h.
2. treatment process according to claim 1, is characterized in that, the filtration flux of described the second ultrafiltration system is 20～40L/m
2h.
3. treatment process according to claim 1, it is characterized in that, hydraulic detention time in described coagulative precipitation tank is 3.5～6 hours, and the hydraulic detention time in described ozone oxidation reaction device is 1～2 hour, and the empty bed residence time in described BAF is 6～8 hours.
4. according to the treatment process described in any one in claims 1 to 3, it is characterized in that, the filtration flux of described the first ultrafiltration system is 25～30L/m
2h.
5. according to the treatment process described in any one in claims 1 to 3, it is characterized in that, described strong brine processing unit also comprises filtration with manganese sand device, and described filtration with manganese sand device is communicated between described more medium filter and the first ultrafiltration system, and the filtering velocity of described filtration with manganese sand device is 8～10m/h.
6. the application in gas treatment waste water according to the treatment process described in any one in claim 1 to 5.
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