CN105016577A - Advanced treatment system for process sewage and advanced treatment method for sewage - Google Patents
Advanced treatment system for process sewage and advanced treatment method for sewage Download PDFInfo
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- CN105016577A CN105016577A CN201510402187.2A CN201510402187A CN105016577A CN 105016577 A CN105016577 A CN 105016577A CN 201510402187 A CN201510402187 A CN 201510402187A CN 105016577 A CN105016577 A CN 105016577A
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Abstract
The invention discloses an advanced treatment system for process sewage and an advanced treatment method for sewage. The treatment system comprises a pretreatment unit, a biochemical treatment unit, an aftertreatment strengthening unit and a sewage reusing unit, wherein the pretreatment unit, the biochemical treatment unit and the aftertreatment strengthening unit are sequentially connected; the pretreatment unit comprises a regulating and homogenizing pot, an oil separating sedimentation tank and an air flotation tank which are sequentially connected in order, and a process sewage inlet pipe is connected to the regulating and homogenizing pot; the biochemical treatment unit comprises an acidifying and hydrolyzing tank, a first-class biochemical tank, a medium sedimentation tank, a second-class biochemical tank and a secondary sedimentation tank which are sequentially connected in order, and the acidifying and hydrolyzing tank is connected with a water outlet end of the air flotation tank in the pretreatment unit; the aftertreatment strengthening unit comprises a coagulation air flotation tank, an ozone contact tank, a biological aerated filter, a first-class filtration and adsorption tank, a second-class filtration and adsorption tank and a monitoring tank which are sequentially connected. The treatment system can treat the process sewage more comprehensively and effectively, so that the treated effluent realizes zero drainage and reaches the water quality standard of reused water, and secondary pollution is avoided.
Description
Technical field
The invention belongs to field of waste water treatment, be specifically related to a kind of process spent water advanced treatment system and advanced treatment method for sewage water.
Background technology
Process spent water is mainly lurgi process coal gasification wastewater, this part coal gasification wastewater CODcr concentration is high, belong to organic sewage, containing ammonia nitrogen and phenol, have certain colourity, have following features: in (1) sewage, organic concentration is high, CODcr is 3500mg/L, B/C value about 0.33, can adopt biochemical processing process; (2) contain hardly degraded organic substance in sewage if unit phenol, polyphenol etc. are containing phenyl ring and heterocyclic material, have certain bio-toxicity, these materials decompose more difficult under aerobic environment, need open loop and degraded under anaerobism/oxygen environment of holding concurrently; (3) ammonia nitrogen in sewage concentration is high, and intractability is comparatively large, needs the treatment process selecting nitrification and denitrification ability all very strong; (4) contain oil slick, dispersed oil, emulsification oils in sewage and dissolve oily substance, the main ingredient of dissolving oil is the aromatics of phenol; Oil in water emulsion needs to adopt air supporting mode to be removed, and deliquescent phenol type substances needs to be removed by method that is biochemical, absorption; (5) containing toxicity inhibition material, the toxicity inhibition material such as phenol, polyphenol, ammonia nitrogen in sewage, needs the poison resistance being improved microorganism by domestication, needs to select suitable technique to improve system impact resistance; (6) impact of abnormal sewage discharge, when art production process goes wrong, can cause the abnormal sewage discharge that Pollutant levels are high, this sewage directly can not enter biochemical treatment system, needs to arrange the measures such as accident adjustment; (7) Colority of Sewage Water is higher, containing some with colour developing group material; (8) hardness in sewage, soluble solid content are high, can not meet circulating cooling make-up water water quality requirement, need whole desalination.And the salinity in Sewage treatment systems is mainly from process spent water, sewage treatment process adds the salt that medicament produces, and therefore, from the angle of reuse water, needs the sewage after to biochemical sewage process to carry out desalination.
Though there is the system to lurgi gasifier processing wastewater advanced treatment in prior art, but the sewage feature of above-mentioned proposition is not all comprehensively processed, therefore, for guaranteeing process spent water process effluent quality, those skilled in the art need badly provides one more comprehensive, the system for the treatment of process sewage effectively, makes the water outlet after process realize zero release and reaches quality of reused water standard, avoids the process spent water advanced treatment system and the method that cause secondary pollution.
In prior art, coal gasification wastewater adopts biochemical treatment CODcr clearance about about 90%, water outlet CODcr is about 250mg/L, aftertreatment strengthening unit adopts single treatment process all cannot meet effluent index requirement, therefore, consider each cell process processing efficiency, accomplish economical rationality, the present embodiment aftertreatment strengthening unit adopts coagulation air-float, ozone+BAF (BAF), two-stage filtration adsorption treatment process, the CODcr clearance of each unit is: coagulation air-float 20%, ozone+BAF 30%, the single-stage CODcr clearance about 40% of Filtration Adsorption.The CODcr amount of two-stage filtration Adsorption is 91mg/L.During actual motion, can the flexible operations such as parallel connection, series connection, bypass segment water be adopted to control effluent quality according to water quality situation.
The each cell processing efficiency of table 1. sewage disposal
Note: the sulfide 1) entering biochemical device controls at below 20mg/L.
2) contain 100mg/L organonitrogen in wastewater influent, in biological process, organonitrogen will change into ammonia nitrogen.
Summary of the invention
The present invention is in order to overcome above-mentioned the deficiencies in the prior art, provide one more comprehensive, the system and method for the treatment of process sewage effectively, makes the water outlet after process realize zero release and reaches quality of reused water standard, avoids the process spent water advanced treatment system causing secondary pollution.The present invention is directed to process spent water to select to remove CODcr, BOD
5, ammonia nitrogen etc. is the biochemical processing process of main body, select with oil removing, decolour for the pretreatment technology of main purpose, select to turn materially main aftertreatment reinforcing process, effectively purified the saline sewage produced in process spent water and process spent water treating processes.
For achieving the above object, present invention employs following technical scheme:
A kind of process spent water advanced treatment system, this treatment system comprises: the pretreatment unit be connected in turn, biochemical treatment unit and aftertreatment strengthening unit; This treatment system also comprises reusing sewage unit; Wherein,
Described pretreatment unit comprises successively along the homogeneous tank of adjustment connected, oil partiting precipitation pool and air flotation pool, and the homogeneous tank of described adjustment is connected with process spent water water inlet pipe;
Described biochemical treatment unit comprises successively along the acidizing hydrolyzation tank connected, one-level biochemistry pool, medium sediment pool, secondary biochemical pond and second pond, wherein, described one-level biochemistry pool and medium sediment pool, secondary biochemical pond and second pond are equipped with the circulating line forming internal recycle liquid and reflux, and the feed-water end of described acidizing hydrolyzation tank is connected with the water side of air flotation pool in described pretreatment unit;
Described aftertreatment strengthening unit comprises successively along the coagulation floatation, ozone contact tank, BAF, single filter adsorption tank, cascade filtration adsorption tank, the monitoring pool that connect.
Preferably, this treatment system also comprises sludge treating block, and described sludge treating block comprises contaminated-oil basin, also comprises successively along the sludge sump connected, dewatered sludge pond, belt type dewaterer; Wherein, described contaminated-oil basin is connected with regulating the oil discharge outlet of homogeneous tank, oil partiting precipitation pool and air flotation pool, and described sludge sump is connected with the mud discharging mouth regulated bottom homogeneous tank, oil partiting precipitation pool, air flotation pool and acidizing hydrolyzation tank.
Further, described sludge treating block also comprises the sludge reflux pumping plant forming sludge reflux with one-level biochemistry pool, medium sediment pool, and forms the sludge reflux pumping plant of sludge reflux with secondary biochemical pond, second pond.
Further, described one-level biochemistry pool adopts the blast aeration formula oxidation ditch process of complete hybrid pond type, and secondary biochemical pond adopts Prepositive denitrification A/O technique.
Preferably, the homogeneous tank of described adjustment is also provided with accident equalizing tank, is provided with guarantee in described accident equalizing tank and enters the mixed uniformly diving mixer of various sewage in equalizing tank.
Preferably, described oil partiting precipitation pool is set to rectangular sedimentation tank, is provided with frizing mud scraper in settling tank.
Preferably, described reusing sewage unit comprises the biochemical sewage reuse unit, saline sewage reuse unit and the multiple-effect evaporation unit that integrally form running balance each other.
Further, described biochemical sewage reuse unit comprises successively along the settling pond, walnut shell filter, gas-water backwash filtration, ultra-filtration equipment, the first-stage reverse osmosis membrane stack that connect; The lime that the water entered wherein is softened is added in settling pond; First-stage reverse osmosis membrane stack is entered after the product water of ultra-filtration equipment adds reductive agent and Scale inhibitors; The product water of described first-stage reverse osmosis membrane stack enters reuse pool, dense water reverse osmosis membrane stack is entered after the dense water of first-stage reverse osmosis membrane stack adds Scale inhibitors, the product water of dense water reverse osmosis membrane stack enters reuse pool, and the dense water of dense water reverse osmosis membrane stack then enters multiple-effect evaporation unit; The backwash water of described walnut shell filter, gas-water backwash filtration, ultra-filtration equipment enters wastewater disposal basin, the matting water of ultra-filtration equipment, first-stage reverse osmosis membrane stack and dense water reverse osmosis membrane stack enters wastewater disposal basin, and the waste water in wastewater disposal basin is promoted to biochemical treatment unit through pump;
Described saline sewage reuse unit comprises successively along the homogeneous tank, settling pond, gas-water backwash filtration, ultra-filtration equipment, the first-stage reverse osmosis membrane stack that connect; The lime that the water entered wherein is softened is added in settling pond; First-stage reverse osmosis membrane stack is entered after the product water of ultra-filtration equipment adds reductive agent and Scale inhibitors; The product water of described first-stage reverse osmosis membrane stack enters reuse pool, dense water reverse osmosis membrane stack is entered after the dense water of first-stage reverse osmosis membrane stack adds Scale inhibitors, the product water of dense water reverse osmosis membrane stack enters reuse pool, and the dense water of dense water reverse osmosis membrane stack then enters multiple-effect evaporation unit; The backwash water of described gas-water backwash filtration, ultra-filtration equipment is back in homogeneous tank through wastewater disposal basin; The matting water of described ultra-filtration equipment, first-stage reverse osmosis membrane stack and dense water reverse osmosis membrane stack is promoted to process spent water biochemical treatment unit through pump;
Described multiple-effect evaporation unit adopts quadruple effect falling liquid film following current vaporizer to carry out evaporative condenser to material.
Preferably, outer circulation anaerobic system is also provided with between described acidizing hydrolyzation tank and one-level biochemistry pool.
Present invention also offers a kind of process spent water deep treatment method, adopt treatment system of the present invention, concrete steps are as follows:
Pre-treatment: make process spent water flow into the homogeneous tank of adjustment of pretreatment unit, carries out oil removal, air supporting, de-oiling decolouring desliming process successively; Enter accident equalizing tank deposit when process drain to exceed on Con trolling index switching in limited time;
Biochemical treatment: the interfluent biochemical treatment unit of air supporting water outlet, carries out acidification hydrolization, the biochemical anoxic of one-level and oxygen consumption, secondary biochemical anoxic and oxygen consumption process successively;
Aftertreatment: the water outlet after biochemical treatment enters described aftertreatment strengthening unit and carries out coagulation air-float, ozone contact, biological aerated filter, single filter absorption, cascade filtration adsorption treatment successively, and is monitored in real time reprocessed water outlet by monitoring pool;
Reusing sewage: biochemical sewage reuse, saline sewage reuse and multiple-effect evaporation process are carried out in the water outlet of aftertreatment strengthening unit successively.
Beneficial effect of the present invention is:
1), the present invention forms tertiary treatment structure by pretreatment unit, biochemical treatment unit and the aftertreatment strengthening unit be connected in turn, and to the sewage after process, according to the reuse requirement of different sewage, carry out biochemical sewage Treatment for Reuse, saline sewage Treatment for Reuse and multiple-effect evaporation process, finally make the water outlet after process realize zero release and reach quality of reused water standard, avoiding causing secondary pollution.
Method provided by the invention is more comprehensive, and the system for the treatment of process sewage effectively, has stronger suitability.
2), namely the present invention's the first step in biochemical treatment unit introduce acidification hydrolization technique, and acidification hydrolization technique is that coked waste water adopts one of more technique, can improve biochemical sewage performance, improves BOD
5/ CODcr ratio, solve some aerobic can not biochemical organic final removal problem.In acidification reaction process, larger molecular organics matter structure in sewage changes, change the component in sewage, make some single aerobic nondegradable organic substance, at this, inter-molecular linkage fracture occur, transform, the processes such as hydroxylation, the change of wastewater composition structure is conducive to the process of subsequent technique, improves wastewater treatment efficiency.
3), in addition, the present invention have also been introduced outer circulation (EC) anaerobic system in biochemical treatment unit, and outer circulation (EC) anaerobic system in the present invention is arranged between acidizing hydrolyzation tank and one-level biochemistry pool.Outer circulation (EC) anaerobic system can complete anaerobic co-metabolism process, while improving phenol recovery ammonia waste water quality, realizes the transition process of the organic carboxylation of part and benzoylation, avoids polyphenol to the conversion of quinones substance.Outer circulation (EC) anaerobic system also utilizes anaerobic bacterium that part phenol recovery ammonia Wastewater Pollutant is changed into methane, part hardly degraded organic substance is converted into easily biodegradable organics simultaneously, and reduce intractability for follow-up aerobe technique and alleviate operation burden, be the main process of pollutant removal in whole technique.
4) the aftertreatment strengthening unit, in the present invention adopts the tertiary treatment of flocculation-air floating, ozone oxidation+BAF (BAF), Filtration Adsorption technical process.This operational path removes colourity and difficult degradation CODcr by flocculation-air floating, oxidation, Filtration Adsorption, improves biochemical sewage performance, removed the NH in sewage by BAF further by ozone modification
3-N, CODcr, remove CODcr, the SS in water by adsorption filtration, effectively meet subsequent disposal requirement, further ensure treatment effect.
5), sewage disposal biochemical system produces in the present invention mud main flocculation sediment mud, biological excess sludge, adopt current domestic conventional belt filter press, have equipment and run ripe, power consumption is lower, and the advantage such as can domesticize, and is convenient to practical application.
Accompanying drawing explanation
Fig. 1 is structure schematic diagram of the present invention.
Fig. 2 is the structure schematic diagram of reusing sewage unit of the present invention.
Fig. 3 is the structure schematic diagram of biochemical reusing sewage unit.
Fig. 4 is the structure schematic diagram of saline sewage reuse unit.
Fig. 5 is the structure schematic diagram of multiple-effect evaporation unit.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is clearly and completely described.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
As shown in Figure 1, a kind of process spent water advanced treatment system and advanced treatment method for sewage water, this treatment system comprises: the pretreatment unit be connected in turn, biochemical treatment unit and aftertreatment strengthening unit; This treatment system also comprises reusing sewage unit; Wherein,
Described pretreatment unit comprises successively along the homogeneous tank of adjustment connected, oil partiting precipitation pool and air flotation pool, and the homogeneous tank of described adjustment is connected with process spent water water inlet pipe;
Described biochemical treatment unit comprises successively along the acidizing hydrolyzation tank connected, one-level biochemistry pool, medium sediment pool, secondary biochemical pond and second pond, wherein, described one-level biochemistry pool and medium sediment pool, secondary biochemical pond and second pond are equipped with the circulating line forming internal recycle liquid and reflux, and described acidizing hydrolyzation tank is connected with the water side of air flotation pool in described pretreatment unit;
Described aftertreatment strengthening unit comprises successively along the coagulation floatation, ozone contact tank, BAF, single filter adsorption tank, cascade filtration adsorption tank, the monitoring pool that connect.
This treatment system also comprises sludge treating block, and described sludge treating block comprises successively along the contaminated-oil basin connected, sludge sump, dewatered sludge pond, belt type dewaterer; Wherein, described contaminated-oil basin is connected with regulating the oil discharge outlet of homogeneous tank, oil partiting precipitation pool and air flotation pool, and described sludge sump is connected with the mud discharging mouth regulated bottom homogeneous tank, oil partiting precipitation pool, air flotation pool and acidizing hydrolyzation tank.
Described sludge treating block also comprises the sludge reflux pumping plant forming sludge reflux with one-level biochemistry pool, medium sediment pool, and forms the sludge reflux pumping plant of sludge reflux with secondary biochemical pond, second pond.Described one-level biochemistry pool adopts the blast aeration formula oxidation ditch process of complete hybrid pond type, and secondary biochemical pond adopts Prepositive denitrification A/O technique.
The homogeneous tank of described adjustment is also provided with accident equalizing tank, is provided with guarantee in described accident equalizing tank and enters the mixed uniformly diving mixer of various sewage in equalizing tank.
Described oil partiting precipitation pool is set to rectangular sedimentation tank, is provided with frizing mud scraper in settling tank.
As shown in Figure 2, this treatment system also comprises reusing sewage unit, and described reusing sewage unit comprises the biochemical sewage reuse unit, saline sewage reuse unit and the multiple-effect evaporation unit that integrally form running balance each other.In Fig. 2, data unit is m
3/ h, for having carried out the water yield data after balancing to the actual amount of water between sewage disposal and the inner each device of reclamation set.
As shown in Figure 3, described biochemical sewage reuse unit comprises successively along the settling pond, walnut shell filter, gas-water backwash filtration, ultra-filtration equipment, first-stage reverse osmosis membrane stack, the reuse pool that connect, also comprises wastewater disposal basin and reverse osmosis membrane stack; Wherein, the backwash water of walnut shell filter, gas-water backwash filtration, ultra-filtration equipment is all communicated with wastewater disposal basin, the matting water of ultra-filtration equipment, reverse osmosis membrane stack flows into wastewater disposal basin, wastewater disposal basin through waste water pump uniform lift to the pond of the middle biochemical treatment unit of process spent water biochemical treatment apparatus.The product water of reuse pool is delivered to outside battery limit (BL) through desalination water pump lifting, finally delivers to circulation water station.The dense water that dense water reverse osmosis produces is promoted between multiple-effect evaporation through pump and carries out evaporative crystallization process.
As shown in Figure 4, saline sewage reuse unit comprises successively along the homogeneous tank, settling pond, gas-water backwash filtration, ultra-filtration equipment, first-stage reverse osmosis membrane stack, the reuse pool that connect, also comprises wastewater disposal basin and reverse osmosis membrane stack; Wherein, the backwash water of gas-water backwash filtration, ultra-filtration equipment is back in homogeneous tank through wastewater disposal basin, the matting water of ultra-filtration equipment, first-stage reverse osmosis membrane stack and dense water reverse osmosis membrane stack through waste water pump uniform lift to the pond of the middle biochemical treatment unit of process spent water biochemical treatment apparatus.The product water of reuse pool is delivered to outside battery limit (BL) through desalination water pump lifting, finally delivers to circulation water station.The dense water that dense water reverse osmosis produces is promoted between multiple-effect evaporation through pump and carries out evaporative crystallization process.
As shown in Figure 5, multiple-effect evaporation unit adopts quadruple effect falling liquid film following current vaporizer to carry out evaporative condenser to material, and first material is through level Four preheating before entering vaporizer, and temperature material being entered an effect heating chamber is increased to close to bubble point.Then material is delivered to an effect heating chamber by feeding pump, material after heating enters an effect separate chamber and carries out vapor-liquid separation, feed liquid loops back an effect heating chamber by an effect discharging pump part, another part enters two effect heating chambers, material is successively after four-effect evaporation, and concentrated solution is discharged through quadruple effect discharging pump.
Separator solution out enters phlegma storage tank, and vaporizer raffinate delivers to evaporation pond.The condensing hot air furnace that condensation obtains, delivers to full factory condensate system.
The present invention can also be provided with outer circulation anaerobic system between described acidizing hydrolyzation tank and one-level biochemistry pool.
Below by embodiment, working process of the present invention is elaborated.
Embodiment 1
The water inlet source of native system is divided into two portions, and first part is process spent water; Second section is saline sewage.Process spent water is mainly lurgi process coal gasification wastewater, this device to sanitary sewage, ground flushing water and early-stage rainwater with lurgi process coal gasification wastewater merging treatment.
Composition graphs 1, the treating processes of native system to sewage is as follows: the production waste got rid of from process unit district phenol recycle-water tower bottom enters the homogeneous tank of sewage, sewage carries out oil removal in tank, water quantity and quality regulates, play the effect of even water quantity and quality, ensure that sewage enters the relatively stable of biological treatment and subsequent processing units water quality and the water yield.
In Coal Chemical Industry production process, process drain exceeds the situation of normal index is inevitable, therefore arranges equalizing tank when designing.Deposit when the pollutents such as CODcr, oil, ammonia nitrogen in water to exceed on Con trolling index the changeable equalizing tank that enters in limited time, after water water quality is normal, equalizing tank water pump low discharge is squeezed into the homogeneous tank of sewage.When water is uneven, the water yield of the homogeneous tank of sewage can flow into sewage equalizing tank.Diving mixer is established to ensure the various sewage Homogeneous phase mixing entered in equalizing tank in equalizing tank.
The water outlet of homogeneous tank flows into oil partiting precipitation pool, and oil partiting precipitation pool is flat flow, establishes frizing mud scraper in pond.The oil slick of oil partiting precipitation pool enters contaminated-oil basin, and pool bottom sludge enters sludge sump, finally delivers between sludge dewatering.By oil partiting precipitation pool process, most oils, suspended matter and small part CODcr, colourity can be removed, alleviate the processing load of subsequent biochemical system.
Containing oil in water emulsion in oil partiting precipitation pool water outlet, certain influence can be caused to the film device of subsequent processing units particularly desalting system if do not remove, in flow process, air-floating apparatus is set.The water outlet of oil partiting precipitation pool enters air flotation pool, and the hybrid reaction in reaction tank with the flocculation agent added and coagulant aids, removes oil in water emulsion by air supporting.
The interfluent biochemical treatment unit of air supporting water outlet, first enters acidizing hydrolyzation tank; The sanitary sewage of plant area, biochemical sewage reclaiming system backwash water, other factory effluent, bottom surface wash-down water and early-stage rainwater also enter acidizing hydrolyzation tank, and acidification hydrolization technique can improve biochemical sewage performance, improve BOD
5/ CODcr ratio, particularly, in acidification reaction process, larger molecular organics matter structure in sewage changes, and changes the component in sewage, makes some single aerobic nondegradable organic substance, at this, inter-molecular linkage fracture occur, transform, the processes such as hydroxylation, the change of wastewater composition structure is conducive to the process of subsequent technique, improves wastewater treatment efficiency.
Acidizing hydrolyzation tank water outlet enters one-level biochemistry pool (i.e. one-level A/O pond is blast aeration formula oxidation ditch process in the present invention), and biological decarbonization, denitrification reaction occur in A/O pond.One-level A/O establishes in pond internal recycle liquid system for mixed-liquor return.In A/O pond, sewage enters anoxic section and aerobic section successively, makes full use of the feature of anoxic biology and aerobe, sewage is purified.One-level A/O pond required air is provided by gas blower.
The water outlet of one-level A/O pond enters intermediate sedimentation pond, and after carrying out mud-water separation, water outlet enters secondary A/O pond.The returned sluge pump reflux of medium sediment pool precipitation is to front end, one-level A/O pond, and excess sludge pump is promoted to the sludge sump between dosing dehydration.
The water outlet in intermediate sedimentation pond enters secondary biochemical pond (i.e. secondary A/O pond), in A/O pond, biological decarbonization, denitrification reaction occurs further, removes CODcr further.Secondary A/O establishes in pond internal recycle liquid system, for mixed-liquor return.
Secondary A/O pond water outlet enters second pond mud-water separation, and the returned sluge pump reflux of sedimentation in secondary sedimentation tank is to the front end of secondary A/O, and excess sludge pump is promoted to the sludge sump between dosing dehydration.
Secondary clarifier effluent enters coagulation reaction tank, mixes with the flocculation agent added and coagulant aids, and the sewage through coagulating enters air-floating apparatus.The object adding flocculation agent removes organic pollutant, colourity and suspended substance further, reduces ozone usage.
The water outlet of coagulation, air-floating apparatus enters ozone contact Buffer Pool, and sewage removes colourity further under ozonization, simultaneously to the modification of sewage ozone, is conducive to the removal efficiency improving follow-up BAF.For prevent the residual ozone of non-complete reaction to downstream BAF system produce toxic action, design consider increase Buffer Pool, by self decay and extend the reaction times reach eliminate its to downstream microorganism poison effect.Ozone contact tank is enclosed construction, and Chi Ding establishes ozone tail gas to destroy system.
Sewage enters BAF after ozonize; Through the sewage that ozone is modified, biochemical property improves, after BAF process, and COD, NH
3-N can reduce further.The oxygen that BAF needs is supplied by gas blower, and BAF establishes gas recoil, water back-purge system.Recoil sewage enters recoil sewage lagoon, by the intermediate pool (not shown in FIG.) being pumped to acidizing hydrolyzation tank front end.
BAF water outlet is promoted to single filter adsorption tank, and Filtration Adsorption pond is filled with the sorbent material with adsorption function, and the organism in sewage and colourity are removed further, adsorbs saturated sorbent material and is regenerated between regeneration by hydraulic hoist.If the water outlet in primary adsorption pond can reach into reclamation set index, be then directly switch into technique reuse water device, if the water outlet that primary adsorption goes out can not meet, then the water outlet of single filter adsorption tank flowed into cascade filtration adsorption tank.Cascade filtration adsorption tank is filled with sorbent material equally.
In the process of sewage disposal, in native system, the treating processes of sludge treating block is as follows:
Come the homogeneous tank of inherent regulation, oil partiting precipitation pool, the base sludge mud of flocculation sedimentation tank and biochemical excess sludge and enter sludge sump, after belt processed, mud cake outward transport is disposed.
Shown in composition graphs 3, the treating processes of native system mesophytization reusing sewage unit is as follows: first biochemical sewage water outlet after biochemical device process enters settling pond, feeding lime in settling pond, carries out softening removal to the carbonate in water and bicarbonate hardness.The supernatant liquor of settling pond flows into priming reservoir, is promoted to walnut shell filter through pump, and removing may containing a small amount of oil in water, and walnut shell filter arranges timing backwash.The water outlet gravity flow of walnut shell filter enters gas-water backwash filtration, gas-water backwash filtration adopts homogeneous filtering material, the pollutents such as the particle in trap water, suspended substance, colloid, reduces pollution index, make water quality meet the requirement entering ultra-filtration equipment, gas-water backwash filtration timing adopts water, gas backwash.The water outlet of gas-water backwash filtration flows into product pond, filter tank, promote through ultrafiltration service pump, first through self-cleaning filter, the particle that may remain in water, suspended substance are retained, play security personnel's effect, through self-cleaning filter laggard enter ultra-filtration equipment, ultra-filtration equipment achieves the biological pollutant, particulate matter, colloid, turbidity, bacterium etc. removed in waste water, meets the influent quality requirement of reverse osmosis system.
The product water of ultra-filtration equipment enters ultrafiltration and produces pond, promotes through RO1 service pump, and the outlet of RO1 service pump arranges line mixer, reductive agent and Scale inhibitors is added to it, oxygenant in reductive water, avoids its injury reverse osmosis membrane, and adding Scale inhibitors is avoid salt in water at film surface scale; Water after dosing enters first-stage reverse osmosis membrane stack after RO1 high-pressure pump and cartridge filter, and first-stage reverse osmosis membrane stack product water enters product pond, dense water enters the dense pond of RO1, and the reverse osmosis water rate of recovery is 75%, and ratio of desalinization is greater than 97%; The water in the dense pond of RO1 adds Scale inhibitors after RO2 service pump promotes, avoid the salt after concentrating in water at film surface scale, after RO2 high-pressure pump and cartridge filter, enter dense water reverse osmosis membrane stack again, the product water of dense water reverse osmosis membrane stack enters product pond, dense water enters the dense pond of RO2; The reverse osmosis water rate of recovery is 50%, and ratio of desalinization is greater than 97%.
The backwash water of walnut shell filter, filter tank, ultra-filtration equipment enters wastewater disposal basin, and the matting water of the membrane stack such as ultrafiltration and reverse osmosis flows into wastewater disposal basin, wastewater disposal basin through waste water pump uniform lift to the intermediate pool of process spent water biochemical treatment apparatus.The product water in product pond is delivered to outside battery limit (BL) through desalination water pump lifting, finally delivers to circulation water station.The dense water that dense water reverse osmosis produces is promoted between multiple-effect evaporation through pump and carries out evaporative crystallization process.
Shown in composition graphs 4, in native system, the treating processes of saline sewage reuse unit is as follows: first the saline sewage that circulation water station, power plant and Desultwater Station are discharged enters the homogeneous tank of within battery limit, mixes with the backwash water such as ultrafiltration, filtration.Homogeneous tank water outlet enters settling pond, feeding lime in settling pond, softens the carbonate in water and bicarbonate hardness, removes the hardness in water, supernatant liquor after clarification flows into priming reservoir, be promoted to filter tank through pump, filter tank adopts homogeneous filtering material, air-water backwashing form, the pollutents such as the particle in trap water, suspended substance, colloid, reduce pollution index, make water quality meet the requirement entering ultra-filtration equipment, filter tank timing adopts water, gas backwash.Filter tank water outlet flows into product pond, filter tank, promote through ultrafiltration service pump, first through self-cleaning filter, the particle that may remain in water, suspended substance are retained, play security personnel's effect, through self-cleaning filter laggard enter ultra-filtration equipment, ultra-filtration equipment achieves the biological pollutant, particulate matter, colloid, turbidity, bacterium etc. removed in waste water, meets the influent quality requirement of reverse osmosis system.
The product water of ultra-filtration equipment enters ultrafiltration and produces pond, promotes through RO1 service pump, and the outlet of RO1 service pump arranges line mixer, reductive agent and Scale inhibitors is added to it, oxygenant in reductive water, avoids its injury reverse osmosis membrane, and adding Scale inhibitors is avoid salt in water at film surface scale; Water after dosing enters first-stage reverse osmosis membrane stack after RO1 high-pressure pump and cartridge filter, and the product water of first-stage reverse osmosis membrane stack enters product pond, dense water enters the dense pond of RO1; The primary reverse osmosis water rate of recovery is 75%, and ratio of desalinization is greater than 97%.
The water in the dense pond of RO1 adds Scale inhibitors after RO2 service pump promotes, avoid the salt after concentrating in water at film surface scale, after RO2 high-pressure pump and cartridge filter, enter dense water reverse osmosis membrane stack again, dense water reverse osmosis membrane stack produces that water enters product pond, dense water enters the dense pond of RO2; The reverse osmosis water rate of recovery is 50%, and ratio of desalinization is greater than 97%.
The backwash water of filter tank, ultra-filtration equipment enters wastewater disposal basin, and the matting water of the membrane stack such as ultrafiltration and reverse osmosis flows into wastewater disposal basin, is promoted to the intermediate pool of process spent water biochemical treatment apparatus through waste water pump.The product water in product pond is delivered to outside battery limit (BL) through desalination water pump lifting, finally delivers to circulation water station.The dense water that dense water reverse osmosis produces is promoted between multiple-effect evaporation through pump and carries out evaporative crystallization process.
In addition, should be noted that, sewage regulating tank in Sewage treatment systems, oil partiting precipitation pool, equalizing tank, acidizing hydrolyzation tank, between dosing dehydration, the waste gas that sludge sump etc. produce collects through covered and enclosed collection device, by centrifugal blower, airduct is delivered to emission-control equipment and is processed, waste gas first carries out adding wet treatment through advection humidifying apparatus, then bacteria bed is entered, pass through gas-liquid, liquid-solid mass transfer by multiple-microorganism in bacteria bed to hydrocarbons micro-in gas, ammonia, hydrogen sulfide and other odor causing substances absorb, decompose, generate simple, harmless, odorless material, after process, gas reaches secondary standard and " urban wastewater treatment firm pollutant emission standard " GB18918-2002 Zhong Chang circle (buffer zone edge) the exhaust gas emission secondary standard of factory's circle concentration limit of the malodorant that the People's Republic of China's " emission standard for odor pollutants " GB14554-93 specifies.
Embodiment 2
As follows system process is carried out to sewage in factory.
1) pre-treatment: make process spent water flow into the homogeneous tank of adjustment of pretreatment unit, carries out oil removal, air supporting, de-oiling decolouring desliming process successively; Enter accident equalizing tank deposit when process drain to exceed on Con trolling index switching in limited time;
2) biochemical treatment: the interfluent biochemical treatment unit of air supporting water outlet, carries out acidification hydrolization, outer circulation anaerobism, the biochemical anoxic of one-level and oxygen consumption, secondary biochemical anoxic and oxygen consumption process successively;
3) aftertreatment: the water outlet after biochemical treatment enters described aftertreatment strengthening unit and carries out coagulation air-float, ozone contact, biological aerated filter, single filter absorption, cascade filtration adsorption treatment successively, and is monitored in real time reprocessed water outlet by monitoring pool;
4) reusing sewage: biochemical sewage reuse, saline sewage reuse and multiple-effect evaporation process are carried out in the water outlet of aftertreatment strengthening unit successively, obtain reuse water.
The detailed process of above-mentioned treatment step is identical with embodiment 1, repeats no more herein.
Require emphasis and be pointed out that; embodiment 2 also add outer circulation anaerobic treatment process between the acidizing hydrolyzation tank and one-level biochemistry pool of embodiment 1; described outer circulation anaerobic system is to while improving phenol recovery ammonia waste water quality; realize the transition process of the organic carboxylation of part and benzoylation, avoid polyphenol to the conversion of quinones substance.Outer circulation anaerobism also utilizes anaerobic bacterium that part phenol recovery ammonia Wastewater Pollutant is changed into methane, part hardly degraded organic substance is converted into easily biodegradable organics simultaneously, and reduce intractability for follow-up aerobe technique and alleviate operation burden, thus have than embodiment 1 better wastewater treatment efficiency.
Claims (10)
1. a process spent water advanced treatment system, is characterized in that, this treatment system comprises: the pretreatment unit be connected in turn, biochemical treatment unit and aftertreatment strengthening unit; This treatment system also comprises reusing sewage unit; Wherein,
Described pretreatment unit comprises successively along the homogeneous tank of adjustment connected, oil partiting precipitation pool and air flotation pool, and the homogeneous tank of described adjustment is connected with process spent water water inlet pipe;
Described biochemical treatment unit comprises successively along the acidizing hydrolyzation tank connected, one-level biochemistry pool, medium sediment pool, secondary biochemical pond and second pond, wherein, described one-level biochemistry pool and medium sediment pool, secondary biochemical pond and second pond are equipped with the circulating line forming internal recycle liquid and reflux, and the feed-water end of described acidizing hydrolyzation tank is connected with the water side of air flotation pool in described pretreatment unit;
Described aftertreatment strengthening unit comprises successively along the coagulation floatation, ozone contact tank, BAF, single filter adsorption tank, cascade filtration adsorption tank, the monitoring pool that connect.
2. a kind of process spent water advanced treatment system according to claim 1, it is characterized in that: this treatment system also comprises sludge treating block, described sludge treating block comprises contaminated-oil basin, also comprises successively along the sludge sump connected, dewatered sludge pond, belt type dewaterer; Wherein, described contaminated-oil basin is connected with regulating the oil discharge outlet of homogeneous tank, oil partiting precipitation pool and air flotation pool, and described sludge sump is connected with the mud discharging mouth regulated bottom homogeneous tank, oil partiting precipitation pool, air flotation pool and acidizing hydrolyzation tank.
3. a kind of process spent water advanced treatment system according to claim 2, it is characterized in that: described sludge treating block also comprises the sludge reflux pumping plant forming sludge reflux with one-level biochemistry pool, medium sediment pool, and forms the sludge reflux pumping plant of sludge reflux with secondary biochemical pond, second pond.
4. a kind of process spent water advanced treatment system according to claim 3, is characterized in that: described one-level biochemistry pool adopts the blast aeration formula oxidation ditch process of complete hybrid pond type, and secondary biochemical pond adopts Prepositive denitrification A/O technique.
5. a kind of process spent water advanced treatment system according to claim 1, is characterized in that: the homogeneous tank of described adjustment is also provided with accident equalizing tank, is provided with guarantee and enters the mixed uniformly diving mixer of various sewage in equalizing tank in described accident equalizing tank.
6. a kind of process spent water advanced treatment system according to claim 1, is characterized in that: described oil partiting precipitation pool is set to rectangular sedimentation tank, is provided with frizing mud scraper in settling tank.
7. a kind of process spent water advanced treatment system according to claim 1, is characterized in that: described reusing sewage unit comprises the biochemical sewage reuse unit, saline sewage reuse unit and the multiple-effect evaporation unit that integrally form running balance each other.
8. a kind of process spent water advanced treatment system according to claim 7, is characterized in that:
Described biochemical sewage reuse unit comprises successively along the settling pond, walnut shell filter, gas-water backwash filtration, ultra-filtration equipment, the first-stage reverse osmosis membrane stack that connect; The lime that the water entered wherein is softened is added in settling pond; First-stage reverse osmosis membrane stack is entered after the product water of ultra-filtration equipment adds reductive agent and Scale inhibitors; The product water of described first-stage reverse osmosis membrane stack enters reuse pool, dense water reverse osmosis membrane stack is entered after the dense water of first-stage reverse osmosis membrane stack adds Scale inhibitors, the product water of dense water reverse osmosis membrane stack enters reuse pool, and the dense water of dense water reverse osmosis membrane stack then enters multiple-effect evaporation unit; The backwash water of described walnut shell filter, gas-water backwash filtration, ultra-filtration equipment enters wastewater disposal basin, the matting water of ultra-filtration equipment, first-stage reverse osmosis membrane stack and dense water reverse osmosis membrane stack enters wastewater disposal basin, and the waste water in wastewater disposal basin is promoted to biochemical treatment unit through pump;
Described saline sewage reuse unit comprises successively along the homogeneous tank, settling pond, gas-water backwash filtration, ultra-filtration equipment, the first-stage reverse osmosis membrane stack that connect; The lime that the water entered wherein is softened is added in settling pond; First-stage reverse osmosis membrane stack is entered after the product water of ultra-filtration equipment adds reductive agent and Scale inhibitors; The product water of described first-stage reverse osmosis membrane stack enters reuse pool, dense water reverse osmosis membrane stack is entered after the dense water of first-stage reverse osmosis membrane stack adds Scale inhibitors, the product water of dense water reverse osmosis membrane stack enters reuse pool, and the dense water of dense water reverse osmosis membrane stack then enters multiple-effect evaporation unit; The backwash water of described gas-water backwash filtration, ultra-filtration equipment is back in homogeneous tank through wastewater disposal basin; The matting water of described ultra-filtration equipment, first-stage reverse osmosis membrane stack and dense water reverse osmosis membrane stack is promoted to process spent water biochemical treatment unit through pump;
Described multiple-effect evaporation unit adopts quadruple effect falling liquid film following current vaporizer to carry out evaporative condenser to material.
9. a kind of process spent water advanced treatment system according to any one of claim 1 ~ 8, is characterized in that: be also provided with outer circulation anaerobic system between described acidizing hydrolyzation tank and one-level biochemistry pool.
10., according to an advanced treatment method for sewage water for any one of claim 1 ~ 8 process spent water advanced treatment system, it is characterized in that comprising the steps:
Pre-treatment: make process spent water flow into the homogeneous tank of adjustment of pretreatment unit, carries out oil removal, air supporting, de-oiling decolouring desliming process successively; Enter accident equalizing tank deposit when process drain to exceed on Con trolling index switching in limited time;
Biochemical treatment: the interfluent biochemical treatment unit of air supporting water outlet, carries out acidification hydrolization, the biochemical anoxic of one-level and oxygen consumption, secondary biochemical anoxic and oxygen consumption process successively;
Aftertreatment: the water outlet after biochemical treatment enters described aftertreatment strengthening unit and carries out coagulation air-float, ozone contact, biological aerated filter, single filter absorption, cascade filtration adsorption treatment successively, and is monitored in real time reprocessed water outlet by monitoring pool;
Reusing sewage: biochemical sewage reuse, saline sewage reuse and multiple-effect evaporation process are carried out in the water outlet of aftertreatment strengthening unit successively.
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106186580A (en) * | 2016-08-31 | 2016-12-07 | 武汉东川自来水科技开发有限公司 | A kind of emulsion sewage disposal system and processing method |
| CN106186533A (en) * | 2016-08-08 | 2016-12-07 | 北京润宇环保工程有限公司 | Processing equipment and percolation liquid treatment method for waste landfill site leachate |
| CN106517676A (en) * | 2016-12-28 | 2017-03-22 | 北京清大国华环境股份有限公司 | Biomass gasification wastewater treatment method and device |
| CN106946417A (en) * | 2017-05-10 | 2017-07-14 | 神华集团有限责任公司 | Sewage-treatment plant |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786773A (en) * | 2010-03-24 | 2010-07-28 | 哈尔滨工业大学 | Biological treatment process for coal gas wastewater of Lurgi gasifier |
| JP2014237110A (en) * | 2013-06-10 | 2014-12-18 | りんかい日産建設株式会社 | System and method for muddy water treatment |
-
2015
- 2015-07-08 CN CN201510402187.2A patent/CN105016577A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101786773A (en) * | 2010-03-24 | 2010-07-28 | 哈尔滨工业大学 | Biological treatment process for coal gas wastewater of Lurgi gasifier |
| JP2014237110A (en) * | 2013-06-10 | 2014-12-18 | りんかい日産建設株式会社 | System and method for muddy water treatment |
Non-Patent Citations (1)
| Title |
|---|
| 周跃 等: "煤化工废水"零排放"技术进展", 《煤炭加工与综合利用》 * |
Cited By (14)
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| CN106946417A (en) * | 2017-05-10 | 2017-07-14 | 神华集团有限责任公司 | Sewage-treatment plant |
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| CN108341550A (en) * | 2018-02-27 | 2018-07-31 | 河南君和环保科技有限公司 | A kind of snack food production waste water integrated treatment process |
| CN108996808A (en) * | 2018-07-02 | 2018-12-14 | 山西太钢不锈钢股份有限公司 | The biochemical combined treatment process and equipment of steel and iron industry concentrated water difficult to degrade |
| CN110078318A (en) * | 2019-06-10 | 2019-08-02 | 苏州中色德源环保科技有限公司 | A kind of chemical industry for making chlorine and alkali mother liquor water process and reclaiming system |
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