CN102485670B - Processing method of citric acid production wastewater - Google Patents
Processing method of citric acid production wastewater Download PDFInfo
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- CN102485670B CN102485670B CN2010105797445A CN201010579744A CN102485670B CN 102485670 B CN102485670 B CN 102485670B CN 2010105797445 A CN2010105797445 A CN 2010105797445A CN 201010579744 A CN201010579744 A CN 201010579744A CN 102485670 B CN102485670 B CN 102485670B
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Abstract
The invention relates to a processing method of citric acid production wastewater. The method comprises steps that: under an anaerobic condition, citric acid production wastewater contacts anaerobic particle sludge; under an aerobic condition, the citric acid production wastewater obtained in the previous step then contacts aerobic sludge; sludge-water separation is carried out, such that solid sludge and processed wastewater are obtained. The method is characterized in that: before the citric acid production wastewater contacts the anaerobic particle sludge, the citric acid production wastewater contacts an alkaline calcium salt precipitating agent and tail water reflux. The tail water reflux is the processed wastewater. With the method provided by the invention, processing efficiency of the citric acid production wastewater can be improved, the energy consumption can be reduced, the cost can be reduced, and an anaerobic section biogas yield can be improved.
Description
Technical field
The present invention relates to a kind for the treatment of process of citric acid production wastewater.
Background technology
The production of citric acid is undertaken by zymotechnique, and the high-concentration waste water produced in the citric acid production process mainly comes self-neutralization, affination and ion-exchanger conditioning workshop section, and wherein ion exchange waste water pollutes maximum.The waste water of its discharge is containing the biodegradable organic of high density, and these organism are main mainly with carbohydrate and degraded product thereof.Contain a large amount of SO in the ion exchanged water of citric acid production discharge and β-amylose waste water
4 2-, SO
3 2-, Cl
-, Na
+, NH
4 +, CN
-, and the higher Ca of concentration
2+, Al
3+, Fe
3+, Mg
2+, K
+deng metal ion, adopt the Anaerobic cultural methods (as UASB, EGSB, MIC etc.) of suspended sludge type can be because granule sludge be not easy to form, or the reason such as very easily easily break, cause the fluctuation of service of reactor, even without any effect.
Summary of the invention
The treatment process that the purpose of this invention is to provide a kind of citric acid production wastewater.Adopt the method, can improve the processing efficiency of citric acid production wastewater, reduce energy consumption, cost-saving, improve anaerobism section biogas output.
The invention provides a kind for the treatment of process of citric acid production wastewater, the method comprises citric acid production wastewater is under anaerobic contacted with anaerobic grain sludge, under aerobic conditions, to with aerobic sludge, contact again with the citric acid production wastewater after anaerobic grain sludge contacts, and carry out mud-water separation, waste water after obtaining solid mud and processing, it is characterized in that, the method also is included in citric acid production wastewater with before anaerobic grain sludge contacts, citric acid production wastewater is contacted with backflow tail water with the alkaline calcium salt precipitation agent, described backflow tail water is the waste water after above-mentioned processing.
In treatment process of the present invention, described backflow tail water is the waste water after aforesaid method is processed.Contain the acidication bacterium in this backflow tail water, can carry out acidification hydrolization to waste water, biomacromolecule in citric acid wastewater is resolved into to small molecules, can make the COD value of citric acid production wastewater reduce, improved the efficiency that follow-up anaerobic treatment and aerobic are processed, reduced energy consumption, reduced cost.In addition, by adding the alkaline calcium salt precipitation agent, remove the calcium ion that the calcium method is produced citric acid wastewater, solved the problem of subsequent disposal fouling obstruction reactor.Simultaneously, produce byproduct methane, create certain economic worth.That is to say, adopt the method, can reduce citric acid production wastewater, particularly produce the processing costs of the ion-exchange class high-concentration hardly-degradable waste water in citric acid, reduce energy consumption, is the treatment process of the citric acid production wastewater of a kind of low cost, less energy-consumption.The citric acid production wastewater that adopts the inventive method to process can reach tri-grades of emission requests of GB8978-88.
The accompanying drawing explanation
Fig. 1 is the citric acid production wastewater processing flow chart.
Embodiment
The invention provides a kind for the treatment of process of citric acid production wastewater, the method comprises citric acid production wastewater is under anaerobic contacted with anaerobic grain sludge, under aerobic conditions, to with aerobic sludge, contact again with the citric acid production wastewater after anaerobic grain sludge contacts, and carry out mud-water separation, waste water after obtaining solid mud and processing, it is characterized in that, the method also is included in citric acid production wastewater with before anaerobic grain sludge contacts, citric acid production wastewater is contacted with backflow tail water with the alkaline calcium salt precipitation agent, described backflow tail water is the waste water after above-mentioned processing.
The method according to this invention, described citric acid production wastewater can be starch based in citric acid production and ion-exchange class waste water.Generally, the COD value of citric acid production wastewater is for being greater than 12000mg/L, and preferably the COD value is 12000mg/L-15000mg/L.Making the COD of citric acid production wastewater by backflow tail water is 5000-10000mg/L, is preferably 5000-8000mg/L.And described backflow tail water can also provide the acidication bacterium, and citric acid production wastewater is hydrolyzed.Described backflow tail water is the waste water after method of the present invention is processed, as shown in Figure 1 and the hereinafter described limpid water outlet from second pond.Adopt backflow tail water to be processed citric acid wastewater, can regulate influent quality on the one hand, high-COD waste water is diluted, and the COD in acidication bacterium source of degradation water can be provided.
In the present invention, the backflow tail water of its initial period can adopt following methods to obtain, at initial initial period of the present invention, adopt industrial tap water to replace backflow tail water, after the COD value of citric acid production wastewater is adjusted to 3200-4300mg/L, carrying out Start-up and Adjustment is activated mud, then the waste water (this area is commonly called as " ion exchange wastewater ") produced with the exchange of citric acid production intermediate ion goes slowly to replace the water quality that acclimation sludge makes the waste water of mud energy adaptive system ion-exchange generation, the tail water partial reflux in this process, system produced, can be used as backflow tail water is used.
The method according to this invention, the temperature that described citric acid production wastewater contacts with backflow tail water with the alkaline calcium salt precipitation agent can be 30-50 ℃, pH can be 4.0-7.0.Being preferably temperature is 35-40 ℃, and the pH value is 4.8-6.2.Can select duration of contact according to the concentration of concrete citric acid production wastewater, generally is at least 8 hours, is preferably 9-12 hour.
In the present invention, the concrete mode that above-mentioned citric acid production wastewater contacts with backflow tail water with the alkaline calcium salt precipitation agent can be for add citric acid production wastewater in equalizing tank, and the COD value that backflow tail water is regulated citric acid production wastewater is 5000-10000mg/L.This backflow tail water, from the water outlet of second pond, also provides the acidication bacterium in the time of backflow tail water.Then, after adding the alkaline calcium salt precipitation agent to make the pH value of lemon acid producing waste water be 4.0-7.0, being preferably the pH value that adds the alkaline calcium salt precipitation agent to make the lemon acid producing waste water is to contact at least 8 hours after 4.8-6.2, is preferably 9-12 hour.The pH value of the citric acid production wastewater after contact is generally and is greater than 6.0, and preferably the pH value of the citric acid production wastewater after contact is 6.0-8.0.The usage quantity of described backflow tail water is at least 20% of citric acid production wastewater volume, is preferably 40-50%.The COD value that this backflow tail water can be regulated waste water on the one hand, on the other hand, can also provide the acidication bacterium, and citric acid production wastewater is hydrolyzed.
In the present invention, citric acid production wastewater contacts the COD value that makes the lemon acid producing waste water to be reduced with backflow tail water, can make macromolecular substance in high concentrated organic wastewater be decomposed into small-molecule substance under the effect of acidication bacterium and improve follow-up anaerobism and aerobic section processing efficiency, generally, can make the COD value of citric acid production wastewater at least reduce by 35%, the COD value that is preferably citric acid production wastewater reduces 35-50%.The COD value of the citric acid production wastewater after above-mentioned processing is 3200-4300mg/L, is preferably 3900-4100mg/L.
Simultaneously, at citric acid production wastewater with after the alkaline calcium salt precipitation agent contacts, generally can make the 80-90% of calcium ion in citric acid production wastewater precipitate, here above-mentioned alkaline calcium salt precipitation agent makes in citric acid production wastewater when calcium ion precipitates, the pH value of having regulated citric acid production wastewater.Generally, the consumption of alkaline calcium salt precipitation agent can add according to the pH value of citric acid production wastewater.The pH value that the consumption of alkaline calcium salt precipitation agent makes citric acid production wastewater in the present invention is 4.0-7.0, it is 4.8-6.2 that the consumption that is preferably the alkaline calcium salt precipitation agent makes the pH value of citric acid production wastewater, this is for preventing the subsequent reactor surface scale, stop up filler and aeration head, greatly extended reactor work-ing life, reduced energy consumption and reduce labor cleaning's cost and all be very helpful.
Above-mentioned calcium ion precipitation agent is preferably alkaline carbonate, more preferably sodium carbonate and/or sodium bicarbonate, more preferably sodium carbonate.
The method according to this invention, described anaerobic condition comprises that temperature is 35-40 ℃, pH>6.0, the time of contact is 3-10 hour.Being preferably temperature is 36-38 ℃, and pH is 6.0-8.0, and the time of contact is 4-6 hour.Waste water after the present invention preferably adopts the anaerobic biological treatment device to acidification hydrolization carries out anaerobic biological treatment, removes most of organism and COD.Described anaerobic biological treatment device is selected UBF (combined anaerobic biological filter tank) reactor.For example can adopt 4 UBF to form the two-stage series connection treater, treater is processed in first step treater and the second stage.Described granule sludge can utilize the mud in water self to be tamed, but this method domestication time is longer, is generally 20-30d.This anaerobic grain sludge can also be by being purchased, or put mud from operating internal-circulation anaerobic reactor (IC) or multistage internal-circulation anaerobic reactor (MIC) and obtain.The present invention is preferably directly and inoculates the mature granular sludge in anaerobic reactor in service in reactor.The affination waste water that the 1/3-1/2 that the inoculum size of above-mentioned granule sludge is the treater volume is first 35-40 ℃ by temperature and multistage internal-circulation anaerobic reactor (MIC) water outlet mix the activity that is started to recover granule sludge, and be 10-15d start time.Then, progressively allocate ion exchange waste water into, Contact Temperature is 35-40 ℃, and be 3-10 hour duration of contact.The citric acid solid that described affination waste water is gained in the citric acid production process is through the hot wash of 80 ℃ of left and right, to improve citric acid purity, the washing lotion of discharging.
In the present invention, the organic loading of described first step treater can be 14-22kgCOD/m
3d, the COD clearance reaches more than 90%; The organic loading of described second stage treater reaches 5-6kgCOD/m
3d, the COD clearance reaches more than 70%.Due in the present invention, the organic loading of treater is high, can improve anaerobism section biogas output, has improved economic worth.The reactor biogas yield is 0.48-0.6m
3cH
4/ kgCOD, methane content of bilogas>60%.
The method according to this invention, described aerobic conditions comprises that the temperature of contact is 35-40 ℃, and oxygen in water (DO) is 2-4mg/L, and sludge settling ratio (SV) is 30-40%, and the time of contact is 24-40 hour.Describedly with the citric acid production wastewater after anaerobic grain sludge contacts, adopt aeration mode to carry out oxygen supply again with in the aerobic sludge contact process, described aeration can adopt the high purity oxygen aerator, the deep well aeration device, the array configuration of one or more of Ai Er oxygen aerator etc. is carried out.The mud of described aerobic sludge in the system initial start stage has been moved ripe Sewage Plant Aerobic Pond for inoculation can be the mud of the rear reuse of contact under aerobic conditions in operational process.Can supplement the aerobic sludge in operational process by the mud in the backflow second pond in an embodiment of the present invention.As known in the art, in order more effectively to ensure the treatment effect under oxygen condition, under preferable case, also regularly second pond is carried out to spoil disposal, to prevent sludge aging.Particularly, the concentration of aerobic sludge can, for being greater than 5000mg/L, be preferably 5000-6000mg/L.
In the present invention, also be provided with second pond, above-mentionedly be drained in second pond with the water outlet after aerobic sludge contacts, with water outlet self after aerobic sludge contacts with mud.The second pond effect is mainly in order to allow the mud in sewage settle down as far as possible, to make water outlet limpid.As aerobic reactor H/O, the sludge concentration in HTO pond during lower than 5000mg/L, can, by the mud return line of second pond bottom, by the conditioning of mud quantity of reflux, make the concentration of aerobic sludge in aerobic reactor reach above-mentioned standard.
In the present invention, preferably adopt aerobic biological processor to carry out the aerobe processing to waste water.Described aerobic biological processor is combined by high tower Aerobic Pond (HTO) and aerobic biofilter (H/O) reactor two-stage tandem.In above-mentioned aerobic biological processor, with citric acid production wastewater after anaerobic grain sludge contacts, with aerobic sludge, contacting in temperature is 35-40 ℃, oxygen in water (DO) is 2-4mg/L, sludge settling ratio (SV) is 30-40%, the concentration of aerobic sludge is greater than under the 5000mg/L condition, contact 24-40 hour, oxygen in water (DO) can adopt pure oxygen aeration device aeration.With the COD clearance of aerobic sludge contact phase be 30-50%, ammonia nitrogen removal frank is 60-70%.Thereby make organic matter degradation in citric acid production wastewater to water outlet COD<100mg/L, reach emission standard.
Treatment process of the present invention, preferably complete according to following steps, and idiographic flow refers to Fig. 1.
The first step: high concentration wastewater from citric acid production is entered to equalizing tank, and the COD value that makes citric acid production wastewater by backflow tail water is 5000-10000mg/L, the 40-50% that the usage quantity of the tail water that wherein refluxes is the citric acid production wastewater volume.Add again the alkaline calcium salt precipitation agent to make the pH value of lemon acid producing waste water for after 4.0-7.0, controlling temperature is under 30-50 ℃, citric acid production wastewater with in backflow tail water with after alkaline calcium precipitation agent contacts 9-12 hour, the clearance of COD is 35%-50%, the calcium ion clearance is 80%-90%.The pH value of citric acid production wastewater is greater than 6.0.
Second step: through the waste water contacted with the acidication bacterium with the alkaline calcium salt precipitation agent, enter the first step and second stage combination anaerobic biofilter (UBF), seed sludge is the interior anaerobic grain sludge of internal-circulation anaerobic reactor in service (IC), the 1/3-1/2 that inoculum size is the treater volume, the affination waste water that is first 35-40 ℃ by water temperature and multistage internal-circulation anaerobic reactor (MIC) water outlet mix the activity that is started to recover granule sludge, and be the 10-15d left and right start time.Then, progressively allocate ion exchange waste water into, Contact Temperature is 35-40 ℃, and be 3-10 hour duration of contact.What in this process, each raising load was taked is first to improve flow, increase again the method for citric acid production wastewater amount, when reaching the 3200-4300mg/L left and right, inlet COD concentration only increases flooding quantity (citric acid production wastewater), until all ion exchange waste waters are all processed.
The 3rd step: after previous step gained sewage removes organic gas, enter high-efficiency aerobic biological processor (tower Aerobic Pond and aerobic biofilter), in temperature, be 35-40 ℃, oxygen in water (DO) is 2-4mg/L, sludge settling ratio (SV) is 30-40%, and the concentration of aerobic sludge is greater than under the 5000mg/L condition, contact 24-40 hour, make organic matter degradation in citric acid production wastewater be less than 100mg/L to water outlet COD, reach emission standard.
The 4th step: the water outlet after the 3rd step is processed enters second pond, and the effect of second pond is mainly in order to allow the mud in sewage settle down as far as possible, to make water outlet limpid.As aerobic reactor H/O, the sludge concentration in HTO pond is during lower than 5000mg/L, can be by the mud return line of second pond bottom, the conditioning of mud quantity of reflux, make the concentration of aerobic sludge in aerobic reactor reach above-mentioned standard, excess sludge enters sludge thickener, and for ease of by sludge lifting, mud is introduced into the collection mud sump and is refluxed or enter sludge thickener.
The 5th step: for reducing influent density, and, for the acidication bacterium is provided, the design water collecting basin is collected the water outlet of the 4th step, and, using this water outlet part as backflow tail water, enters equalizing tank, and another part directly effluxes (being the water outlet discharge in Fig. 1).
Below by embodiment, the present invention is further detailed, but the present invention is not limited in following examples.
Embodiment 1
The first step: citric acid is entered to equalizing tank from friendship class factory effluent (calcium ion concn is 50mg/L), making the COD value of citric acid production wastewater by backflow tail water is 8000mg/L, and the usage quantity of the tail water that wherein refluxes is 50% of citric acid production wastewater volume.After adding again sodium carbonate to make the pH value of lemon acid producing waste water be 6.1, controlling temperature is under 35 ℃, citric acid production wastewater contacts 12 hours with backflow tail water with sodium carbonate, the COD value that records the citric acid production wastewater after contact is 4000mg/L, calcium ion concn is 4mg/L, calculating learns that the clearance of COD is 50%, and the calcium ion clearance is 88%.
Second step: make through with alkaline calcium salt precipitation agent (sodium carbonate), with the citric acid production wastewater after backflow tail water contacts, entering the first step and second stage combination anaerobic biofilter (UBF), under anaerobic with anaerobic grain sludge, contact, the anaerobic grain sludge of inoculation is the interior anaerobic grain sludge of internal-circulation anaerobic reactor in service (IC), inoculum size is 1/2 of treater volume, the affination waste water that is first 35 ℃ by water temperature and multistage internal-circulation anaerobic reactor (MIC) water outlet mix the activity that is started to recover granule sludge, and be the 15d left and right start time.Then, progressively allocate the citric acid production wastewater after above-mentioned contact into, Contact Temperature is 35 ℃, and the pH value of contact is 6.1-6.3, and be 8 hours duration of contact.What in this process, each raising load was taked is first to improve flow, increase again the method for the citric acid production wastewater amount after above-mentioned contact, when reaching the 4000-4100mg/L left and right, inlet COD concentration only increases flooding quantity (citric acid production wastewater), until all ion exchange waste waters are all processed.Wherein, the organic loading of the first step and second stage combination anaerobic biofilter is respectively 20kgCOD/m
3.d and 6kgCOD/m
3.d, anaerobism section COD clearance average out to 90%, anaerobism section biogas yield is 0.52m
3cH
4/ kgCOD.
The 3rd step: after previous step gained sewage removes organic gas, enter modern high-efficiency aerobic biological processor (tower Aerobic Pond and aerobic biofilter), in temperature, it is 35 ℃, oxygen in water (DO) is 2mg/L, sludge settling ratio (SV) is 30%, and the concentration of aerobic sludge is under the 6000mg/L condition, stops 40 hours, make organic matter degradation in citric acid production wastewater be less than 100mg/L to water outlet COD, reach emission standard.
The 4th step: the water outlet after the 3rd step is processed enters second pond, the effect of second pond is mainly to provide active sludge for supporting well aeration, by most of sludge reflux to tower Aerobic Pond, be partly refluxed to the H/O pond, excess sludge enters sludge thickener, for ease of by sludge lifting, mud is introduced into the collection mud sump and is being refluxed or entering sludge thickener.
The 5th step: water collecting basin is collected the water outlet of the 4th step, and, using this water outlet part as backflow tail water, enters equalizing tank, and another part directly effluxes (being the water outlet discharge in Fig. 1).
Embodiment 2
The first step: citric acid is entered to equalizing tank from friendship class factory effluent (calcium ion concn is 80mg/L), making the COD value of citric acid production wastewater by backflow tail water is 6000mg/L, and the usage quantity of the tail water that wherein refluxes is 40% of citric acid production wastewater volume.After adding again sodium bicarbonate to make the pH value of lemon acid producing waste water be 4.8, controlling temperature is under 45 ℃, citric acid production wastewater contacts 9 hours with backflow tail water with sodium bicarbonate, the COD value that records the citric acid production wastewater after contact is 3900mg/L, calcium ion concn is 10.3mg/L, calculating learns that the clearance of COD is 35%, and the calcium ion clearance is 82%.
Second step: make through with alkaline calcium salt precipitation agent (sodium bicarbonate), with the citric acid production wastewater after backflow tail water contacts, entering the first step and second stage combination anaerobic biofilter (UBF), under anaerobic with anaerobic grain sludge, contact, the anaerobic grain sludge of inoculation is the interior anaerobic grain sludge of internal-circulation anaerobic reactor in service (IC), inoculum size is 1/3 of treater volume, the affination waste water that is first 40 ℃ by water temperature and multistage internal-circulation anaerobic reactor (MIC) water outlet mix the activity that is started to recover granule sludge, and be the 10d left and right start time.Then, progressively allocate the citric acid production wastewater after above-mentioned contact into, Contact Temperature is 40 ℃, and the pH value of contact is 7.6-7.8, and be 5 hours duration of contact.What in this process, each raising load was taked is first to improve flow, increase again the method for the citric acid production wastewater amount after above-mentioned contact, when reaching the 3900-4000mg/L left and right, inlet COD concentration only increases flooding quantity (citric acid production wastewater), until all ion exchange waste waters are all processed.Wherein, the organic loading of the first step and second stage combination anaerobic biofilter is respectively 20kgCOD/m
3.d and 5kgCOD/m
3.d, anaerobism section COD clearance average out to 80%, anaerobism section biogas yield is 0.46m
3cH
4/ kgCOD.
The 3rd step: after the mixture of previous step gained sewage removes organic gas, enter modern high-efficiency aerobic biological processor (tower Aerobic Pond and aerobic biofilter), in temperature, it is 40 ℃, oxygen in water (DO) is 4mg/l, sludge settling ratio (SV) is 30-40%, and the concentration of aerobic sludge is under the 5000mg/L condition, stops 24 hours, make organic matter degradation in citric acid production wastewater be less than 100mg/L to water outlet COD, reach emission standard.
The 4th step: the water outlet after the 3rd step is processed enters second pond, the effect of second pond is mainly to provide active sludge for supporting well aeration, by most of sludge reflux to tower Aerobic Pond, be partly refluxed to the H/O pond, excess sludge enters sludge thickener, for ease of by sludge lifting, mud is introduced into the collection mud sump and is being refluxed or entering sludge thickener
The 5th step: water collecting basin is collected the water outlet of the 4th step, and, using this water outlet part as backflow tail water, enters equalizing tank, and another part directly effluxes (being the water outlet discharge in Fig. 1).
Comparative Examples 1
Carry out according to the method in embodiment 1, use the water that does not contain the acidication bacterium to replace backflow tail water, and in equalizing tank, do not add the calcium ion precipitation agent.The organic loading of the first step and second stage combination anaerobic biofilter is respectively 20kgCOD/m
3.d and 6kgCOD/m
3.d, organic removal rate all drops to 60%, and anaerobism section biogas yield is 0.3m
3cH
4/ kgCOD.The COD value in friendship class waste water of the citric acid after anaerobic treatment is 300mg/L.And after moving one week, scale formation obviously appears in each reactor, situation about stopping up appears in the part aeration head.
Claims (6)
1. the treatment process of a citric acid production wastewater, the method comprises citric acid production wastewater is contacted with backflow tail water with the alkaline calcium salt precipitation agent, and under anaerobic, to with the citric acid production wastewater after backflow tail water contacts, with anaerobic grain sludge, contact with alkaline calcium salt, under aerobic conditions, to with aerobic sludge, contact again with the citric acid production wastewater after anaerobic grain sludge contacts, and carry out mud-water separation, waste water after obtaining solid mud and processing, described backflow tail water is the waste water after above-mentioned processing, described citric acid production wastewater contacts the COD value that makes citric acid production wastewater and reduces 35-50% with backflow tail water with the alkaline calcium salt precipitation agent, the calcium ion clearance is 80-90%, the 40-50% that the usage quantity of described backflow tail water is the citric acid production wastewater volume, the temperature that described citric acid production wastewater contacts with backflow tail water with the alkaline calcium salt precipitation agent is 30-50 ℃, and the time of contact is 9-12 hour.
2. method according to claim 1, wherein, it is 4.0-7.0 that the consumption of described alkaline calcium salt precipitation agent makes the pH value of citric acid production wastewater.
3. method according to claim 2, wherein, described alkaline calcium salt precipitation agent is sodium carbonate and/or sodium bicarbonate.
4. method according to claim 1, wherein, described anaerobic condition comprises that temperature is 35-40 ℃, pH > 6.0, the time of contact is 3-10 hour.
5. method according to claim 4, wherein, described anaerobic condition comprises that temperature is that 36-38 ℃, pH are 6.0-8.0, the time of contact is 4-6 hour.
6. method according to claim 1, wherein, described aerobic conditions comprises that temperature 35-40 ℃, oxygen in water are that 2-4mg/L, sludge settling ratio are 30-40%, the time of contact is 24-40 hour.
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| CN103508631A (en) * | 2013-09-12 | 2014-01-15 | 江苏和顺环保股份有限公司 | Wastewater treatment system in starch factory |
| CN103979710B (en) * | 2014-05-16 | 2015-07-01 | 吴江华诚复合材料科技有限公司 | Treatment method for starch processing waste water |
| CN107324595A (en) * | 2017-07-27 | 2017-11-07 | 广西农垦糖业集团红河制糖有限公司 | A kind of sewage disposal system |
| CN110589991B (en) * | 2019-09-10 | 2020-11-27 | 同济大学 | Method for removing calcium ions in high-concentration organic wastewater |
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