CN103288309A - Coal gasification wastewater zero-emission treatment method, treatment system and application thereof - Google Patents
Coal gasification wastewater zero-emission treatment method, treatment system and application thereof Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Separation Using Semi-Permeable Membranes (AREA)
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
The heterogeneous ring compound that contains a large amount of ammonia nitrogens, aldehydes matter, mononuclear aromatics and polycyclic aromatic hydrocarbons and nitrogenous, sulphur, oxygen in the waste water that produces in the Coal Gasification Technology process also has part oils and prussiate, COD
Cr(namely adopt potassium bichromate (K
2Cr
2O
7) chemical oxygen demand that determines as oxygenant) dense.Characteristics such as coal gasification waste water has that wastewater discharge is big, Persistent organic pollutants concentration height, intractability are big are one of difficult trade effluents of generally acknowledging.
For the processing of present coal gasification waste water, be divided into one-level processing, second-stage treatment and advanced treatment usually.It is pre-treatment that one-level is handled, and payes attention to the recovery of valuable material, comprises unit such as absorption, precipitation, extraction, stripping; Second-stage treatment mainly is biochemical treatment, biochemical processing process is the core that whole coal gasification waste water is handled, biochemical processing process mainly contains activated sludge process, anoxic/aerobic method (is Anacrobic/Oxic, abbreviation AO method), sequencing batch active sludge (be Sequencing Batch Reactor Activated Sludge Process, be called for short the SBR method) and combination process thereof etc.; The common method of advanced treatment is Fenton reagent method, ozone oxidation method, flocculent precipitation, membrane treatment process etc.But adopt above-mentioned biochemical processing process to carry out biochemical treatment, owing to contain hard-degraded substances such as a large amount of phenyl ring and heterocyclic in the water, can cause bio-chemical effluent COD
CrDense.And after the biochemical treatment, adopt above-mentioned technologies such as activated carbon filter process, ozone oxidation method, flocculent precipitation to carry out advanced treatment, because suspended substance, colloid and organic concentration in the water are still very high, thereby make the running cost height, and effluent quality is still very high.Therefore, mainly based on qualified discharge, can not realize the cyclically utilizing of waste water at the processing of such waste water.
At present, can realize the existing report of coal gasification waste water treatment technology of reuse.For example, Chinese patent CN101857331B discloses a kind of coal chemical industry wastewater zero emission treatment method and system, and it has mainly utilized the 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, has not only caused the backwash frequency height, becomes new secondary pollutant but also produce a large amount of useless Jiao.This invention does not consider that coal gas waste has the big characteristics of the water yield yet, adopt the waste water water yield that produces behind the membrane sepn still very big, can only have part waste water to go desulphurization system, also have greatly and do not handle, also caused simultaneously the running cost height of production technique, and the defective of fluctuation of service.Chinese patent CN101560045A discloses a kind of coal chemical industrial waste water treatment process, this technology mainly be before biochemical treatment, to adopt Fenton reagent and ozone catalytic agent, utilize the redoxomorphism of Fenton reagent and ozone catalytic agent, phenols in the waste water, the oxidative degradation of polycyclic aromatic hydrocarbons material are removed, but owing to have high organism, high chroma, high suspended matter characteristics through the pretreated water outlet of air supporting, and the organism in the water had both contained macromole hardly degraded organic substances such as phenols, polycyclic aromatic hydrocarbons, also contained a large amount of small molecules easily biodegradable organicses.Therefore, disturbed by high chroma, high suspended matter, small organic molecule, Fenton reagent and ozone catalytic agent are used in employing before pre-treatment, 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 the water increases, and can directly influence the operation of subsequent film treatment process.And because ozone has germicidal action, the water outlet after the ozonize can directly be killed microorganism in the follow-up active sludge aeration tank owing to contain remaining ozone, thereby has also limited the biological treatment ability.Simultaneously, this invents the shortcoming that same existence does not consider that the coal gasification waste water water production rate is big, causes directly to adopt the evaporative crystallization processing can cause cost of investment big reverse osmosis waste water, and running cost is also high, has limited the extensive popularization of technology.
Summary of the invention
At 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 provides a kind of coal gasification waste water zero discharge treatment system, and a further object of the present invention provides 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 big 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 purpose of conserve water resource.
Except as otherwise noted, term " desalination " refers to processing that the dissolved solid in the coal gasification waste water is removed in the present invention.
Except as otherwise noted, term " strong brine " refers to that handling the solid substance that will dissolve in the coal gasification waste water by desalination concentrates the waste water that the back produces in the present invention.
Except as otherwise noted, term " the dense water of high salt " refers to handle the waste water that the dissolved solid in the strong brine is further concentrated the back generation by strong brine in the present invention.
The waste water that produces when except as otherwise noted, term " backwash water " refers in second ultrafiltration system, BAF, more medium filter, filtration with manganese sand device and the first ultrafiltration system operational process backwash regularly 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, this method may further comprise the steps:
(1) coal gasification waste water is carried out biochemical treatment, obtain the waste water after the biochemical treatment;
(2) waste water that obtains in the step (1) is carried out desalination, obtain strong brine and water purification after desalination is handled;
(3) strong brine that obtains in the step (2) is carried out strong brine and handle, obtain the dense water of high salt and water purification after strong brine is handled; Preferably, described strong brine is handled and is carried out in the strong brine processing unit, and more preferably, described strong brine processing unit comprises lime settling pond, more medium filter, first ultrafiltration system, nanofiltration system and first reverse osmosis system that is communicated with successively;
(4) the dense water of high salt that obtains in the step (3) is evaporated, obtain dense water and water purification after the evaporation process.
According to method of the present invention, the biochemical treatment described in the step (1) is preferably carried out in the biochemical treatment unit, and more preferably, described biochemical treatment unit comprises anaerobic pond, anoxic pond, Aerobic Pond and the settling tank that is communicated with successively; Further preferably, hydraulic detention time in the described anaerobic pond is 18～24 hours, more preferably, hydraulic detention time in the described anoxic pond is 12～24 hours, again preferably, hydraulic detention time in the described Aerobic Pond is 40～72 hours, and most preferably, the hydraulic detention time in the described settling tank is 4～8 hours; Further preferably, the sludge concentration in the described Aerobic Pond is 3～4g/L, more preferably, oxyty in the described Aerobic Pond is 2～3mg/L, and more preferably, the nitrification liquid reflux ratio in the described Aerobic Pond is 50～100%, most preferably, the return sludge ratio in the described settling tank is 100～200%.
According to method of the present invention, desalination described in the step (2) preferably carries out in the 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, second ultrafiltration system and second reverse osmosis system that is communicated with successively, again preferably, described coagulating agent is one or more in polymerize aluminum chloride, poly-ferric chloride and the 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 the described BAF is ceramic grain filter; Still more preferably, described second ultrafiltration system is the immersion ultrafiltration system, and more preferably, described second ultrafiltration system comprises self-cleaning filter, and more preferably, the filtration flux of described second ultrafiltration system is 10～50L/m
2H, most preferably, the filtration flux of described second ultrafiltration system is 20～40L/m
2H; Again further preferably, the reverse osmosis membrane in described second reverse osmosis system is antipollution type reverse osmosis membrane, and more preferably, the rate of recovery of described second reverse osmosis system is 65～75%; Again further preferably, hydraulic detention time in the described coagulative precipitation tank is 3.5～6 hours, and more preferably, the hydraulic detention time in the described ozone oxidation reaction device is 1～2 hour, most preferably, the empty bed residence time in the described BAF is 6～8 hours.
According to method of the present invention, in step (3), preferably, adding bodied ferric sulfate and the dosage that dosage is 100～300mg/L in the described lime settling pond is the unslaked lime of 150～250mg/L, more preferably, the filtering velocity of described more medium filter is 8～15m/h; Further preferably, the filtration flux of described first ultrafiltration system is 15～45L/m
2H is preferably 25～30L/m
2H, more preferably, the rate of recovery of described first reverse osmosis system is 70～80%, and more preferably, the pH value of the water inlet of described reverse osmosis system is 9～10, and 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 the filtration with manganese sand device, and preferably, described filtration with manganese sand device is communicated between described more medium filter and 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 the 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 pre-treatment, preferably, described pre-treatment is carried out in pretreatment unit, and more preferably, described pretreatment unit comprises equalizing tank, again preferably, be provided with whipping appts in the described equalizing tank, most preferably, the hydraulic detention time in the described equalizing tank is 12～24 hours.
In above-mentioned preferred embodiment, can earlier coal gasification waste water be fed equalizing tank, be provided with agitator in the equalizing tank, pass through mechanical agitation, the water quality that assurance enters the biochemical treatment unit is even, stable, water outlet in the described equalizing tank enters anoxic pond, Aerobic Pond by pipeline enter the anaerobic pond of biochemical treatment unit by pipeline after more successively, water outlet in the 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 the waste water is removed by the 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: the biochemical treatment unit, the desalination unit, strong brine processing unit and evaporation element, preferably, described biochemical treatment unit comprises the anaerobic pond that is communicated with successively, anoxic pond, Aerobic Pond and settling tank, more preferably, described desalination unit comprises the coagulative precipitation tank that is communicated with successively, the ozone oxidation reaction device, BAF, second ultrafiltration system and second reverse osmosis system, most preferably, described strong brine processing unit comprises the lime settling pond that is communicated with successively, more medium filter, first ultrafiltration system, nanofiltration system and first reverse osmosis system; Further preferably, described second ultrafiltration system is the immersion ultrafiltration system, and more preferably, described 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 the biochemical treatment unit, and more preferably, described pretreatment unit comprises equalizing tank, most preferably, be provided with whipping appts in the described equalizing tank.
In another preferred embodiment for the treatment of system of the present invention, described strong brine processing unit also comprises the filtration with manganese sand device, and described filtration with manganese sand device is communicated between more medium filter and first ultrafiltration system.
Again on the one hand, the present invention also provides treatment process of the present invention and the application for the treatment of system in handling coal gasification waste water.
Below by a preferred embodiment of the present invention the present invention is made and to further describe:
Coal gasification waste water fed in the inner equalizing tank that is provided with whipping appts carries out pre-treatment, by the mechanical agitation of whipping appts, make water quality evenly, stable;
Water outlet in the equalizing tank delivers into anaerobic pond, anoxic pond, the Aerobic Pond of biochemical treatment unit successively by pipeline then, water outlet in the Aerobic Pond is back to anoxic pond by certain nitrification liquid reflux ratio, rest part enters settling tank, by biological respinse the most organic pollutants in the waste water is removed by the microbial process absorption degradation in the biochemical treatment unit; Water outlet in the settling tank is back to anoxic pond by certain return sludge ratio, and rest part enters the desalination unit;
The desalination unit is used for the inorganic salts separating substances of the waste water after the described biochemical treatment is come out, but the strong brine that produces is collected in the water purification reuse of generation, is used for next processing unit; In the coagulative precipitation tank of desalination unit, by suspended substance and the partial organic substances in the coagulation removal water; Water outlet in the coagulative precipitation tank enters the ozone oxidation reaction device by pipe-line transportation, with the hardly degraded organic substance in the waste water under the oxygenant effect, by complete oxidation or change the small organic molecule of readily biodegradable into; Water outlet in the ozone oxidation reaction device enters in the BAF, utilize ozone catalytic agent strong oxidizing property characteristics, hard-degraded substance in the water behind the 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 the waste water being degraded has reduced entering organic loading in the film system to large extent; Water outlet enters second ultrafiltration system by pipe-line transportation in the BAF, second ultrafiltration system comprises self-cleaning filter, for the treatment of the large particulate matter in the water inlet, prevention damages ultra-filtration membrane, the effect of ultrafiltration is to hold back materials such as bacterium in the waste water, colloid, suspended substance, but the water reuse is produced in ultrafiltration, also can directly enter second reverse osmosis system and carry out desalination, the water purification that second reverse osmosis system produces can reuse, the backwash water of the backwash water of second ultrafiltration system and BAF can also be returned coagulative precipitation tank and handle again;
The strong brine that second reverse osmosis system is produced enters the strong brine processing unit by pipe-line transportation again, be used for the strong brine of described desalination unit is further handled, but the dense water of high salt that produces is collected in the water purification reuse that obtains after the processing, is used for next processing unit; Strong brine at first enters the lime settling pond, under the unslaked lime by adding, flocculation agent (as polyiron sulfate), coagulant aids (as the polyacrylamide) acting in conjunction, can not only remove hardness, basicity and organism, suspended substance in the water, can also play germicidal action; Water outlet in the lime settling pond enters into more medium filter, further removes materials such as suspended substance in the water and part heavy metal; Water outlet in the more medium filter enters into the filtration with manganese sand device or directly enters into first ultrafiltration system, nanofiltration system and first reverse osmosis system, and adopting the filtration with manganese sand device is in order to remove the iron in the waste water, but the water purification reuse that first reverse osmosis system produces; The backwash water of more medium filter, filtration with manganese sand device and/or first ultrafiltration system can also be returned the lime settling pond and handle again, the dense water of high salt that nanofiltration system is produced feeds evaporation element;
At last the water outlet in the strong brine processing unit (being the dense water of high salt) is delivered into evaporation element, by vaporizer materials such as the salt in the dense water of high salt, organism are further concentrated, water purification after the evaporation can be used as boiler feedwater, and the dense water that evaporation obtains can be used for towards grey flushing cinder.
Compared with prior art, there is following beneficial effect at least 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 purpose of conserve water resource;
(3) the present invention has reduced the water yield that enters evaporation process by coal gasification waste water is handled step by step, and then has reduced cost of investment and the running cost of evaporation process; Particularly in the present invention, reduced the calcium in the waste water that enters first reverse osmosis system effectively, fouling tendency divalent ions such as magnesium, for follow-up reverse osmosis treatment system has reduced inorganic salt fouling risk, and in the feed water by reverse osmosis system, regulate water inlet pH value to 9～10, it is moved in alkaline environment, reduced in the water organism to the Pollution risk of reverse osmosis membrane, improved the operation stability of reverse osmosis system greatly, 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 second reverse osmosis system), reduced the water yield that enters evaporation process significantly;
(3) technological operation of the present invention is simple, convenient management, and running cost is low.
Description of drawings
Below, describe embodiment of the present invention by reference to the accompanying drawings in detail, wherein:
Fig. 1 carries out the schematic flow sheet of an embodiment of coal gasification waste water zero discharge treatment for adopting treatment system of the present invention;
Fig. 2 carries out the schematic flow sheet of an embodiment of biochemical treatment for the biochemical treatment unit that adopts treatment system of the present invention;
Fig. 3 carries out the schematic flow sheet of an embodiment of desalination processing for the desalination unit that adopts treatment system of the present invention;
Fig. 4 carries out the schematic flow sheet of an embodiment of strong brine processing for the strong brine processing unit that adopts treatment system of the present invention;
Fig. 5 carries out the schematic flow sheet of another embodiment of strong brine processing for the strong brine processing unit that adopts treatment system of the present invention;
Fig. 6 carries out the schematic flow sheet of another embodiment of coal gasification waste water zero discharge treatment for adopting treatment system of the present invention;
Fig. 7 carries out the schematic flow sheet of pretreated another embodiment for the pretreatment unit that adopts treatment system of the present invention.
Description of reference numerals:
The 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, the 9-water purification, 10-equalizing tank, 11-anaerobic pond, the 12-anoxic pond, 13-Aerobic Pond, 14-settling tank, 15-waste water, 16-coagulative precipitation tank, 17-ozone oxidation reaction device, the 18-BAF, 19-second ultrafiltration system, 20-second reverse osmosis system, 21,22,30,31, the 34-backwash water, 23-strong brine, 24-lime settling pond, the 25-more medium filter, 26-first ultrafiltration system, 27-nanofiltration system, 28-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 further described in detail, the embodiment that provides is only in order to illustrate the present invention, rather than in order to limit the scope of the invention.
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 contains the evaporation element (5) of vaporizer.
As shown in Figure 2, described biochemical treatment unit (2) comprises anaerobic pond (11), anoxic pond (12), Aerobic Pond (13) and the settling tank (14) that is communicated with successively.
As shown in Figure 3, described desalination unit (3) comprises the coagulative precipitation tank that adds coagulating agent (16) that is communicated with successively, add the ozone oxidation reaction device (17) (for example, inner circular tower structure ozone oxidation reaction device of filling 30% active carbon filler) of ozone, BAF (18) (for example inner BAF that is filled with ceramic grain filter), 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 second reverse osmosis system (20) (for example adopt the wide runner film of resistance to crocking (BW30FR～400/34i) reverse osmosis membrane).
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), first ultrafiltration system (26) that is communicated with successively, the PVDF material), (reverse osmosis membrane can adopt the wide runner film of resistance to crocking (BW30FR～400/34i)) for nanofiltration system (27) (for example, the nanofiltration membrane model can be DURASLICK NF8040) and first reverse osmosis system (28).
When the treatment system that adopts present embodiment was carried out coal gasification waste water (1) zero discharge treatment, treatment process can be carried out as follows:
A. after coal gasification waste water (1) at first enters anaerobic pond (11), anoxic pond (12), Aerobic Pond (13), settling tank (14) successively by pipeline, the waste water (15) that produces 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), second ultrafiltration system (19), second reverse osmosis system (20) successively, the water purification (7) that produces is by pipeline output reuse, the backwash water (21) that the backwash water (22) that second ultrafiltration system (19) produces and BAF (18) produce is carried out re-treatment by pipe-line transportation to coagulative precipitation tank (16) ingress, and the strong brine of generation (23) 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), first ultrafiltration system (26), nanofiltration system (27), first reverse osmosis system (28), the backwash water (31) that first ultrafiltration system (26) produces, the backwash water (30) of the backwash water (34) that filtration with manganese sand device (33) produces and more medium filter (25) generation by pipe-line transportation to lime settling pond (24) front end, again handle, the water purification (8) that produces is by the pipe-line transportation reuse, and the dense water of high salt (29) that the dense water of high salt (34) that nanofiltration system produces and 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) directly by pipe-line transportation to vaporizer, by the evaporation concentration effect of vaporizer, the water purification of generation (9) reuse, the dense water (6) of generation can be used for towards grey flushing cinder.
When the treatment process that adopts present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can adopt following parameter to carry out:
Hydraulic detention time in the anaerobic pond (11): 24h,
Hydraulic detention time in the anoxic pond (12): 24h,
Hydraulic detention time in the Aerobic Pond (13): 72h, sludge concentration: 4g/L, oxyty: 2g/L, water inlet pH value: 7～8, the nitrification liquid reflux ratio: 100%,
Hydraulic detention time in the settling tank (14): 8h, return sludge ratio: 200%,
Hydraulic detention time in the coagulative precipitation tank (16): 6h, the dosage of coagulant polymeric aluminium chloride: 400mg/L,
Hydraulic detention time in the ozone oxidation reaction device (17): 2h, ozone dosage: 120mg/L,
The empty bed residence time: 8h in the BAF (18),
The filtration flux of second ultrafiltration system (19): 30L/ (m
2.h), the water purification rate of recovery of second ultrafiltration system: 90%,
The water purification rate of recovery of second reverse osmosis system (20): 75%,
Hydraulic detention time in the 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 about 10.3,
The water inlet of more medium filter (25) is regulated pH to 7～8 by hydrochloric acid, and filtering velocity is 10m/h, and the 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 first ultrafiltration system (26): 30L/ (m
2.h), the water purification rate of recovery of first ultrafiltration system: 80%,
Nanofiltration system (27) rate of recovery: 80%,
The water inlet pH value of first reverse osmosis system (28) is controlled about 10.0, the water purification rate of recovery of first reverse osmosis system: 80%,
The evaporation water purification rate of recovery: 90%.
The effluent quality analytical data in different treatment stage among table 1 embodiment 1
Annotate: system's total yield refers to the ratio of resulting total water purification amount and total inflow
As the replacement of strong brine processing unit described in the embodiment 1 (4), the present invention can also adopt strong brine processing unit (4) as shown in Figure 5 to carry out the strong brine processing.
As shown in Figure 5, this strong brine processing unit (4) has omitted the filtration with manganese sand device (33) that is communicated between more medium filter (25) and first ultrafiltration system (26).
When the treatment system that adopts present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can be undertaken by the step a among the embodiment 1, b and d.As shown in Figure 5, when implementation step c, the water outlet of more medium filter (25) directly can be fed first ultrafiltration system (26).
When the treatment process that adopts present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can adopt following parameter to carry out:
Hydraulic detention time in the anaerobic pond (11): 18h,
Hydraulic detention time in the anoxic pond (12): 12h,
Hydraulic detention time in the Aerobic Pond (13): 40h, sludge concentration: 4g/L, oxyty: 2g/L, water inlet pH value: 7～8, the nitrification liquid reflux ratio: 50%,
Hydraulic detention time in the settling tank (14): 4h, return sludge ratio: 100%,
Hydraulic detention time in the coagulative precipitation tank (16): 3.5h, the dosage of coagulant polymeric iron(ic) chloride: 350mg/L,
Hydraulic detention time in the ozone oxidation reaction device (17): 2h, ozone dosage: 80mg/L,
The empty bed residence time: 7h in the BAF (18),
The filtration flux of second ultrafiltration system (19): 10L/ (m
2.h), the water purification rate of recovery of second ultrafiltration system: 90%,
The water purification rate of recovery of second reverse osmosis system (20): 65%,
Hydraulic detention time in the 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 about 10.3,
The water inlet of more medium filter (25) is regulated pH to 7～8 by hydrochloric acid, and filtering velocity is 8m/h, and the upper strata is 1～2mm hard coal, and lower floor is 0.8～1.2mm quartz sand,
The filtration flux of first ultrafiltration system (26): 15L/ (m
2.h), the water purification rate of recovery of first ultrafiltration system: 80%,
Nanofiltration system (27) rate of recovery: 70%,
The water inlet pH value of first reverse osmosis system (28) is controlled about 9.0, the water purification rate of recovery of first reverse osmosis system: 70%,
The evaporation water purification rate of recovery: 90%.
The effluent quality analytical data in different treatment stage among table 2 embodiment 2
Annotate: system's total yield refers to the ratio of resulting water purification amount and total inflow.
As shown in Figure 6, the present invention can also adopt pretreatment unit (32) that coal gasification waste water (1) is carried out pre-treatment.
As shown in Figure 7, described pretreatment unit (32) comprises that the inside that is communicated with anaerobic pond (11) is provided with the equalizing tank (10) of whipping appts.
When the treatment system that adopts present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can be undertaken by the step b among the embodiment 2, c and d.As shown in Figure 7, when implementation step a, coal gasification waste water (1) at first need be fed equalizing tank (10) and feed anaerobic pond (11) again.
When the treatment process that adopts present embodiment is carried out coal gasification waste water (1) zero discharge treatment, can adopt following parameter to carry out:
Hydraulic detention time in the equalizing tank (10): 20h,
Hydraulic detention time in the anaerobic pond (11): 20h,
Hydraulic detention time in the anoxic pond (12): 18h,
Hydraulic detention time in the Aerobic Pond (13): 60h, sludge concentration: 3g/L, oxyty: 3g/L, water inlet pH value: 7～8, the nitrification liquid reflux ratio: 80%,
Hydraulic detention time in the settling tank (14): 7h, return sludge ratio: 150%,
Hydraulic detention time in the coagulative precipitation tank (16): 5h, the dosage of aluminum sulfate coagulant: 380mg/L,
Hydraulic detention time in the ozone oxidation reaction device (17): 1h, ozone dosage: 100mg/L,
The empty bed residence time: 6h in the BAF (18),
The filtration flux of second ultrafiltration system (19): 50L/ (m
2.h), the water purification rate of recovery of second ultrafiltration system: 90%,
The water purification rate of recovery of second reverse osmosis system (20): 70%,
Hydraulic detention time in the 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 about 10.3,
The water inlet of more medium filter (25) is regulated pH to 7～8 by hydrochloric acid, and filtering velocity is 15m/h, and the upper strata is 1～2mm hard coal, and lower floor is 0.8～1.2mm quartz sand,
The filtration flux of first ultrafiltration system (26): 45L/ (m
2.h), the water purification rate of recovery of first ultrafiltration system: 80%,
Nanofiltration system (27) rate of recovery: 75%,
The water inlet pH value of first reverse osmosis system (28) is controlled about 9.5, the water purification rate of recovery of first reverse osmosis system: 75%,
The evaporation water purification rate of recovery: 90%.
The effluent quality analytical data in different treatment stage among table 3 embodiment 3
Annotate: system's total yield refers to the ratio of resulting water purification amount and 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, under the situation that does not break away from the spirit and scope of the present invention; any modification of doing, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. the treatment process of a coal gasification waste water zero release, this method may further comprise the steps:
(1) coal gasification waste water is carried out biochemical treatment, obtain the waste water after the biochemical treatment;
(2) waste water that obtains in the step (1) is carried out desalination, obtain strong brine and water purification behind the desalination;
(3) strong brine that obtains in the step (2) is carried out strong brine and handle, obtain the dense water of high salt and water purification after strong brine is handled; Preferably, described strong brine is handled and is carried out in the strong brine processing unit, and more preferably, described strong brine processing unit comprises lime settling pond, more medium filter, first ultrafiltration system, nanofiltration system and first reverse osmosis system that is communicated with successively;
(4) the dense water of high salt that obtains in the step (3) is evaporated, obtain dense water and water purification after the evaporation process.
2. treatment process according to claim 1, it is characterized in that, biochemical treatment described in the step (1) is carried out in the biochemical treatment unit, preferably, described biochemical treatment unit comprises the anaerobic pond that is communicated with successively, anoxic pond, Aerobic Pond and settling tank, more preferably, hydraulic detention time in the described anaerobic pond is 18～24 hours, again preferably, hydraulic detention time in the described anoxic pond is 12～24 hours, and again preferably, the hydraulic detention time in the described Aerobic Pond is 40～72 hours, most preferably, the hydraulic detention time in the described settling tank is 4～8 hours; Further preferably, the sludge concentration in the described Aerobic Pond is 3～4g/L, more preferably, oxyty in the described Aerobic Pond is 2～3mg/L, and more preferably, the nitrification liquid reflux ratio in the described Aerobic Pond is 50～100%, most preferably, the return sludge ratio in the described Aerobic Pond is 100～200%.
3. treatment process according to claim 1 and 2, it is characterized in that, desalination described in the step (2) carries out in the desalination unit, preferably, described desalination unit comprises the coagulative precipitation tank that adds coagulating agent, the ozone oxidation reaction device that adds ozone, BAF, second ultrafiltration system and second reverse osmosis system that is communicated with successively, more preferably, described coagulating agent is one or more in polymerize aluminum chloride, poly-ferric chloride and the Tai-Ace S 150, again 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 the described BAF is ceramic grain filter; Still more preferably, described second ultrafiltration system is the immersion ultrafiltration system, and more preferably, described second ultrafiltration system comprises self-cleaning filter, and more preferably, the filtration flux of described second ultrafiltration system is 10～50L/m
2H, most preferably, the filtration flux of described second ultrafiltration system is 20～40L/m
2H; Again further preferably, the reverse osmosis membrane in described second reverse osmosis system is anti-soil type reverse osmosis membrane, and more preferably, the rate of recovery of described second reverse osmosis system is 65～75%; Again further preferably, hydraulic detention time in the described coagulative precipitation tank is 3.5～6 hours, and more preferably, the hydraulic detention time in the described ozone oxidation reaction device is 1～2 hour, most preferably, the empty bed residence time in the described BAF is 6～8 hours.
4. according to each described treatment process in the claim 1 to 3, it is characterized in that, in step (3), adding bodied ferric sulfate and the dosage that dosage is 100～300mg/L in the described lime settling pond is the unslaked lime of 150～250mg/L, preferably, the filtering velocity of described more medium filter is 8～15m/h; Further preferably, the filtration flux of described first ultrafiltration system is 15～45L/m
2H is preferably 25～30L/m
2H, more preferably, the rate of recovery of described first reverse osmosis system is 70～80%, and more preferably, the pH value of the water inlet of described first reverse osmosis system is 9～10, and most preferably, the rate of recovery of described nanofiltration system is 70～80%.
5. according to each described treatment process in the claim 1 to 4, it is characterized in that, described strong brine processing unit also comprises the filtration with manganese sand device, preferably, described filtration with manganese sand device is communicated between described more medium filter and first ultrafiltration system, more preferably, the filtering velocity of described filtration with manganese sand device is 8～10m/h.
6. according to each described treatment process in the claim 1 to 5, it is characterized in that the evaporation described in the step (4) is carried out in evaporation element, preferably described evaporation element comprises vaporizer, and more preferably, the rate of recovery of described evaporation is greater than 90%.
7. according to each described treatment process in the claim 1 to 6, it is characterized in that, described method can also comprise step (1 ') before in step (1): coal gasification waste water is carried out pre-treatment, and preferably, described pre-treatment is carried out in pretreatment unit, more preferably, described pretreatment unit comprises equalizing tank, more preferably, is provided with whipping appts in the described equalizing tank, most preferably, the hydraulic detention time in the described equalizing tank is 12～24h.
8. treatment system of utilizing the coal gasification waste water zero release of each described treatment process in the claim 1 to 7, it is characterized in that, described system comprises the biochemical treatment unit that is communicated with successively, the desalination unit, strong brine processing unit and evaporation element, preferably, described biochemical treatment unit comprises the anaerobic pond that is communicated with successively, anoxic pond, Aerobic Pond and settling tank, more preferably, described desalination unit comprises the coagulative precipitation tank that is communicated with successively, the ozone oxidation reaction device, BAF, second ultrafiltration system and second reverse osmosis system, most preferably, described strong brine processing unit comprises the lime settling pond that is communicated with successively, more medium filter, first ultrafiltration system, nanofiltration system and first reverse osmosis system; Further preferably, described second ultrafiltration system is the immersion ultrafiltration system, and more preferably, described second ultrafiltration system comprises self-cleaning filter, and most preferably, described evaporation element comprises vaporizer.
9. treatment system according to claim 8, it is characterized in that, described treatment system also comprises pretreatment unit, preferably, described pretreatment unit is communicated with the biochemical treatment unit, and more preferably, described pretreatment unit comprises equalizing tank, most preferably, be provided with whipping appts in the described equalizing tank; Further preferably, described strong brine processing unit also comprises the filtration with manganese sand device, and more preferably, described filtration with manganese sand device is communicated between more medium filter and first ultrafiltration system.
10. one kind according to the application of each described treatment system in each described treatment process or the claim 8 to 9 in the claim 1 to 7 in handling coal gasification waste water.
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