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Possible ways for post-treatment of biologically treated wastewater from yeast factory/Galimi papildomi mieliu gamyklos biologiskai valytu nuoteku valymo budai.

1. Introduction

Yeast production wastewater is a complex mixture. Most of the contaminants in the wastewater are due to the use of molasses as a main raw material. Molasses, being the main by-product of beet sugar process, are also used as raw material for the commercial production of yeast and ethanol. As a by-product of sugar manufacturing, molasses contain from 45 to 50% of residual sugars, 15 to 20% of non-sugar organic substances, 10 to 15% of ash (minerals) and about 20% of water.

Sugar beets contain no colouring materials, but they do contain colour-forming substances. Sugar and nonsugars such as phenol-iron complexes, melanins, that participate in the production of colour (caramel substances, melanoidines) or nonsugars as such (phenol-iron complexes, melanins) are responsible for the change. The degree of discoloration is related primarily to pH and temperature. The discoloration in sugar juices increases threefold for each 10[degrees]C rise in the temperature of processing. Colouring matter is formed not only when bases or acids react, but also, to some extent, from decomposition of saccharose. These mixtures of colour-conferring materials are referred to in the literature under various names, such as caramelan, caramelene, carameline, saccharan and fuscazinic acid. In addition, furfural derivatives are formed simultaneously with volatile compounds (aldehydes, such as acrolein) and also carbon dioxide is being discarged. The colouring matters, that appear in the course of sugar manufacturing, can be divided into the following groups (Olbrich 1973):

A) Caramel materials. These substances are the results of thermal decomposition (including loss of water) of saccharose- they contain no nitrogen. At constant pH the formation of caramel is directly proportional to the effective temperature.

B) Polyphenol-iron complexes. Pyrocatechol (plant pigment), which occurs in the epidermis and the head of beets (in amounts of about 0.02%), leads to a yellow-greenish discoloration of sugar juices. It is known that the change results from the formation of a pyrocatechol-iron complex. This is not entirely removed during the defecation of the juice and can be found in molasses.

C) Melanoidines. Melanoidines are high molecular weight polymers and main coloured compounds (Gonzalez et al. 1999). The formation of melanoidins comprises a set of consecutive and parallel chemical reactions taking place between amino compounds and carbohydrates during a Maillard reaction (Cammerer and Kroh 1995).

D) Melanins. Beet tyrosinase, which belongs to the polyphenol-oxidases, contains copper in its active group. On access with oxygen it can cause oxidation of various aromatic compounds (pyrocatechol, tyrosine) and produce blackish-grey discolorations. This reaction, known as melanin-formation, requires only enzymatically catalyzed oxidation for its initiation and then proceeds as a chain reaction passing through red and red-brown intermediate stages to orthoquinone-like compounds. Since this discoloration can be removed almost completely in the predefecation of beet-sugar juice, melanins seldom appear in molasses.

During yeast fermentation process sugars contained in molasses are utilized as carbon and energy sources. The major part of the non-sugar substances in molasses (molasses residuals), however, is not utilized by the yeast production and discharged unchanged to the processed wastewater, which represents the principal waste in the yeast production process. Besides molasses' residuals, yeast production wastewater also contains chemicals which are added during fermentation (e.g. various salts, antifoams, propionic acids, brine, etc), yeast metabolites and residual yeast cells.

Phenolic compounds responsible for beet molasses wastewater colour are partly removed (63% removal) during aerobic-anoxic treatment process, but the colour removal accounts for only 8-23% (Kalyuzhnyi et al. 2005). In accordance with other literature data (Francisca Kalavathi et al. 2001) the visible colour is mainly asociated with other substances than phenolic compounds namely, with persistent to biodegradation melanoidins.

Conventional anaerobic-aerobic treatment processes can accomplish the degradation of melanoidins only up to 6% or 7% (Gonzalez et al. 1999; Guimaraes et al. 1999).

Therefore, it is necessary to study additional treatment mehods to remove colour from molasses" effluents. This can prevent serious environmental problems such as reduction of both photosynthetic activity and dissolved oxygen concentration that coloured wastewaters can raise in river courses.

Technologies for treatment wastewaters can be divided into three types- chemical, physical and biological methods. The processes of biological and physicalchemical purification of wastewater were investigated by G. Vaboliene, A. Matuzevicius (2007), A. Riauka et al. (2006); A. Mazeikiene et al. (2005) and G. Vaboliene, A. Matuzevicius (2005).

Melanoidins can be removed by:

1) Biological treatment with certain bacteria and fungi have also been applied, leading to lower colour removal efficiencies (Miyata et al. 2000).

Many reseachers have tried to isolate microorganisms, which have the ability to decolorize melanoidins. Melanoidins have antioxidant properties and are toxic to many microorganisms in wastewater treatment (Frankel et al. 1978). It has been reported that basidiomycetes including Corius sp. No. 20 (Watanabe et al. 1982), dueteromycestes including Aspergillus fumigatus G-2-6 (Ohmomo et al. 1987), Aspergillus oryzae Y-2-32 (Ohmomo et al. 1988b) and bacteria including Lactobacillus hilgardi (Ohmomo et al. 1988a) showed melanoidindecolorization properties. Although the potential of these microorganisms to remove melanoidin from molasses wastewater is clear, their actual use for molasses' wastewater treatment processes might be difficult from the viewpoint of the stability and maintanace of colour removal activity. Operation of proposed biological process will be difficult due to the contamination with competetive microorganisms.

2) Chemical oxidation with ozone.

Ozone has been used in many countries for the treatment of drinking water. Ozonation processes are particularly attractive because ozone can destroy hazardous organic contaminants. In the last years ozone has successfully been applied to the treatment of specific compounds such as dyes, phenolic compounds, pesticides and organochlorides (Wu and Masten 2002; Kamenev 2003). Neverless, oxidation of molasses wastewater with ozone is rather limited to a few investigations. In these studies synthetic solutions or very diluted wastewater were oxidized with ozone (Kim et al. 1985; Gehringer et al. 1997). The chemical oxidation of biologically purified effluents of Salutaguse yeast factory with ozone was investigated in 2005 (Blonskaja et al. 2006). The research data showed that application of ozonation in a combined process seems to be promising for yeast wastewater purification. In this case the target of ozonation is the enhancement of biodegradability and removal of colour and odour.

3) Physical-chemical treatments.

These methods require high reagent dosages and generate a large amount of sludge (Gonzalez et al. 1999). It was reported (Gladchenko et al. 2004, Kalyuzhnyi et al. 2005) that application of iron and aluminium coagulation for molasses wastewater post-treatment of biofilter effluents showed that color, COD, nitrogen and phosphate decreased with incresing acting Fe and Al concentrations and the discharge limits were already archievable under iron concentrations around 200 mg/l and aluminium around 540 mg/l.

Zak (2005) showed, that the using of hydrogen peroxide and iron (II) sulfate or chloride in the chemical pretreatment of Saccharomyces cerevisae yeast industry wastewater can be effective.

The investigation proved that the use of Fenton's system permitted a high reduction of sugar-like substances and total decolorizing of non-sugar compounds. The level of COD reduction depended on the amount and mutual proportions of COD:Fe(II):[H.sub.2][O.sub.2], as well as a type of the applied salt Fe(II). For iron concentrations: 1000-4000 mg [l.sup.-1] with molar excess [[H.sub.2][O.sub.2]]:[Fe(II)]-2-14:1 and reaction pH-3.1-3.4, very high reproducibility of results and the COD reduction exceeding 75% were obtained, but the concentration of iron was very high. For this range of the reagent concentrations, the distribution of COD reduction values correlated with the equation: COD=[Ax.sup.4] + [Bx.sup.3] - [Cx.sup.2] + Dx -E (where: x = [[H.sub.2][O.sub.2]]:[Fe(II)]). Additional neutralization with the use of lime milk made the secondary reduction of CO[D.sub.r(CaO)] value possible, which resulted in the reduction of the total CO[D.sub.T] above 90%.

Salutaguse WWTP

The most common of all the treatment methods is biological treatment, because it is more economical than any other types. Therefore, it can successfully be implemented for wastewater treatment (Tables 1 and 2).

Wastewater (up to 350 [m.sup.3]/d) from the yeast production plant processing beet sugar molasses was treated with anaerobic sludge in modified anaerobic/anoxic reactors system. The anaerobic reactors were fed with mixture of raw wastewater and recycled anoxic sludge. The temperature of the anaerobic stage was kept between 30 and 36[degrees]C, the pH of between 7.2 and 7.5 and was self-regulated by the biological process without neutralization. Both anaerobic reactors were operating with COD loading of 12-16 kg CODx[m.sup.3]/d. During the last six years technological scheme was the following (Fig. 1).


According to the technological set-up presented in Fig. 1, the biological processes in the anaerobic reactors and in the anoxic reactor are inter-related with the returned sludge from the secondary sedimentation tank (by the anoxic reactor) to the inlet of the mixing tank.

Evaluation of the efficiency of anaerobic and anoxic stages as well as the total efficiency of the system has demonstrated that leading the wash waters back to the mixing tank improved the efficiency of the anoxic stage.

The results proved that the success of this type of purification process, based on the recirculation system with the use of returned sludge, depends significantly on the sludge loss prevention from the anaerobic reactors. The main results of wastewater treatment from yeast industry are given in Tables 1 and 2.

The general effluent from the yeast factory usually contains 22-35 g COD/l, 1.7-2.7g/l total N and sulphate as well a significant amount of recalcitrant for biodegradation and highly coloured melanoidins.

Wastewater treatment plant was working in the optimum regime, but concentration of effluent pollutants was very high, therefore the post treatment was required.

The wastewater from molasses processing presents a large amount of coloured substances that give dark brown colour and high organic load to the effluents. After a multistage biological treatment most of the organic load was removed. Although the treatment results showed that the brown colour does not disappear and it can even increase because of the repolymerization of coloured compounds.

The aim of this study was to investigate the precipitation of coloured substances with coagulation (as one of possible ways for post-treatment) of highly polluted biologically pre-treated wastewater from Salutaguse Yeast Factory where beet molasses are being processed. Successful implementation of treatment measures will prevent serious environmental problems, such as reduction of both photosynthetic activity and dissolved oxygen concentration, that colored wastewaters can cause in river courses.

2. Method

Post-treatment of biologically treated wastewater

Chemical methods are one of the possible ways for the post treatment process (for removal of non-biodegradable substances). These methods include chemical precipitation, chemical oxidation reduction, formation of an insoluble gas followed by stripped gas, and other chemical reactions that involve exchanging or shaping electrons between atoms.

The presence of organic matter in effluent from Salutaguse WWTP generally increases the required coagulant dosage and therefore it is always necessary to confirm a chemical treatment process by laboratory experimentation. Laboratory experimentation is always required to determine the optimum doses of coagulants.

In order to obtain more accurate data, the research group was testing the effect of different dose concentrations of coagulants on the performance of biologically treated wastewater. The coagulation process usually uses pH adjustment, addition of chemical precipitant, and flocculation. Flocculation was used as the further agglomeration of slowly-settling coagulated particles into large rapidly-settling flock and precipitation mainly had to convert dissolved ionic species into solid-phase particulates. In the precipitation process, coagulants and flocculation were used to increase particle size through aggregation and be removed from aqueous phase by coagulation and filtration. A suggested procedure for determining, optimum doses of reagent chemicals in the laboratory is as follows:

1. Place wastewater from effluents of Salutaguse WWTP in a glass.

2. Determine reagent doses to bracket the anticipated optima, regarding pH precipitant/coagulant/flocculants.

3. Mix rapidly for 30 seconds.

4. Mix slowly, so as to achieve good coagulation. Carry on for up to 30 minutes.

5. Allow settling.

6. Measure results.


Addition of coagulants was carried out less than 200 rpm and then intensity of stirring was reduced to 40 rpm to complete a flocculation process during which pH was maintained at 7.2-7.5 by addition of sodium hydroxide. All experiments were performed with 200 ml of anaerobic/aerobic pre-treated effluent in a laboratory glass under continuous stirring and pH control (Fig. 2).

All analyses (CO[D.sub.tot], COD, phenols, [], [], S[O.sub.4], TSS and VSS) were performed by Standard Methods for the Examination of Water and Wastewater (1998).

The colour was determined using a UV spectrophotometer.

3. Results and discussion

Some non-biodegradable substances, that are resistant to biodegradation, can be chemically altered to yield the material that is biodegradable. Hydrolysis, under either acidic or alkaline conditions, can be used to break up many large organic molecules into smaller segments that are amenable to biological treatment.

Hydrolyses derives its name from the chemical reaction when a carbon-carbon bond is broken, a hydrogen atom attached to the site on one of the carbon atoms, and OH group attaches to the site on the other carbon atom.

The basic reaction, when the A[L.sup.3+] ion is added to water, consists of the formation of aluminium hydroxide precipitate and release of a degree of acidity (hydrolysis):

[Al.sup.3+] + 3[H.sub.2]O = Al[(OH).sub.3] + 3[H.sup.-]. (1)

Each mole of cation should react with three moles of water to produce one mole of metal hydroxide and three moles of hydrogen ions. This acidity reacts with certain species in solution, especially bicarbonate ions.

HC[O.sub.3.sup.-] + [H.sup.+] = H[2.sub.O] + C[O.sub.2], (2)

[Al.sup.3+] + 3HC[O.sub.3.sup.-] = Al[(OH).sub.3] + 3C[O.sub.2]. (3)


Ferric salts are the most frequently used iron salts. Overall reaction is the same as that for aluminium salts

[Fe.sup.3+] + 3HC[O.sub.3.sup.-] = Fe[(OH).sub.3] + 3C[O.sub.2]. (4)

And for instance, with ferric chloride in water with calcium alkalinity

2Fe[Cl.sub.3] + 3Ca[(HC[O.sub.3]).sub.2] = 2Fe[(OH).sub.3] + 3Ca[Cl.sub.2] + 6C[O.sub.2]. (5)

With iron salts we have the same problems relating to the consumption of alkalinity products that have to be added in order to maintain pH within the optimum range.

The main results of experiments are given in Table 3.

Table 3 shows that the best results were obtained with the following coagulants Fe[Cl.sub.3]x6[H.sub.2]O and [Al.sub.2][(S[O.sub.4]).sub.3].

Performance of iron and aluminium coagulation step

Coagulants Fe[Cl.sub.3]x6[H.sub.2]O and [Al.sub.2][(S[O.sub.4]).sub.3] were analyzed additionally.

The results on efficiency of [Fe.sup.3+] and [Al.sup.+3] coagulation step for treatment of aerobic SBR effluent are presented in Tables 4 and 5. It is noticeable that all parameters (CO[], [], [] and color) decrease with the increase of acting Fe and Al concentrations and the discharge limits are already achievable under iron concentrations around 200 mg/l and aluminium around 400 mg/l.

The performance of colour removal by chemical coagulation depends on the characteristics of both colour substances and coagulants.

Gel-filtration of untreated yeast wastewater revealed that the substances responsible for visible colour (OD580) have symmetrical Gauss-type distribution of their molecular weights (MW) in the range of 0-30 kDa with a maximum at 6-7.8 kDa (>60% of colour is associated with the substances having MWs in the range of 2.6-14 kDa). On the contrary, substances with aromatic structures (OD280) have non-symmetrical distribution of their MWs with a clear prevalence of low MW molecules (maximum at 2.6-4.5 kDa; > 82% of UV-absorption is associated with MWs < 8 kDa). These data show that the visible colour yeast wastewater is not closely associated with the aromatics like phenolic compounds.

The colour of wastewater underwent dramatic changes from deep brown to pastel yellow after coagulation. These results are superior (with regard to coagulant added) to those reported in the literature for anaerobically treated baker's yeast wastewater (Kalyuzhnyi at al. 2003).

Varying ferrous chloride concentration (from 50[Fe.sup.3+] mg/l up to 500 [Fe.sup.3+] mg/l) and keeping pH constant were applied for the treatment of wastewater. A ferrous chloride concentration of 200 mg/l was necessary for an efficient COD removal to 830 mg/l and for colour removal by 60%, but did not significantly catalysed P tot and N tot removal.

Varying aluminium sulphate concentration (from 100 [Al.sup.3+] mg/l up to 800 [Fe.sup.3+] mg/l) and keeping pH constant were applied for the treatment of wastewater. Aluminium sulphate concentration of 400mg/l was necessary for an efficient COD removal for 1270 mg/l and for colour removal by 73%, but did not significantly increase P tot and N tot removal.

The sludge formed under an acting Fe concentration of 200 mg/l was relatively large (SVI = 270 ml/l TSS). The acting Al concentration of 400 mg/l produced much more sludge (SVI = 545 ml/l TSS). The iron sludge had higher (~90%) VSS content compared to the sludge obtained during Al coagulation step (56, 5% VSS) showing the significant removal of organic COD and nitrogen during the iron coagulation step.

Fig. 3 shows the evolution of colour removal and COD decrease for experiments carried out at different [Fe.sup.3+] and [Al.sup.3+] dosages.


As the result of coagulation, absorbance at 580 nm decreased significantly. Applied concentration of [Fe.sup.3+] and [Al.sup.3+] had positive effect not only on colour removal but also on COD. Melanoidins are responsible for the brown colour and included in COD.

Results of coagulations

--Application of iron chloride and aluminium sulphate coagulation for post-treatment of anaerobic-aerobic effluents may fulfil the discharge limits to the sewer under iron concentrations of around 200 mg/l and aluminium concentrations around 400 mg/l.

--Significant decrease of colour substances could be achieved by using coagulation. It is very important to meet biological standards when final effluent is treated with ultraviolet radiation.

--Generated during coagulation sludge could be the problem when full scale process applied. The iron sludge had much better SVI which is an important parameter for further handling of sludge (separation, de-watering).

--Considering that Salutaguse Yeast Factory has daily 330 [m.sup.3]/d of wastewater to be treated using coagulation process it could be proposed that up to 426 kg TSS/d would be generated additionally if [Fe.sup.3+] was used and up to 281 kg TSS/d in case of [Al.sup.3+]. It corresponds to amount of sludge 1.27-1.94 [m.sup.3]/d (at 22% DS after sludge dewatering).

--Installation of flotation unit is needed before sludge de-watering.


Chemical oxidation of biologically purified effluents of Salutaguse yeast factory with ozone was investigated for the period from 2005 to 2008. Some results of the experiments with ozone are presented in Table 6 (Blonskaja et al. 2006). The experiments indicated that the efficiency of post-ozonation in terms of COD (COD removal) ranged from 30% to 49%, and the ratio dn/ACOD, consumed ozone dosage mg of ozone per mg of COD removed, ranged from 1.2 to 2.5. The best result with COD removal was received in run 4.


During ozonation, pH decreases as a result of formation of carboxylic acids. However, in the experiments of post-ozonation of the yeast wastewater, pH decreased only in the run 2 (from 8.3 up to 8.1). In all other runs (1, 3, 4, 5) pH increased (from 7.3 to 7.9). The reason could be that acidic products of biochemical oxidation had been degraded by ozone. In all cases, ozonation removed the colour and distinct odour of the treated wastewater. Initially, the biologically treated wastewater was dark brown and had a distinct odour, and after ozonation it was practically transparent and colourless with no odour specific to this wastewater. Studies on the ozonization of effluents of yeast industry continue and the results of this study will be presented in the near future.

First results of ozonation

--The post-ozonation experiments indicate that ozonation can be used in the tertiary treatment of yeast wastewater for the reduction of colour, odour, and overall concentration of organic contaminants and matter. Since the biodegradability of the yeast wastewater increased during the ozonation, or at least in the beginning of postozonation, it is possible to include ozonation into a combined purification process simultaneously with anaerobic and aerobic bio-oxidation.

--In the combined process, the goal of ozonation is the enhancement of biodegradability and removal of colour and odour.

--Taking into account that ozonation is still an expensive technology, the last option--application of ozonation in combination with biological methods--may be more economical for yeast wastewater purification

--The ozone dosage required to decrease the residual COD noticeably was about 10001500 mg/l, and both CODtot and CODsol decreased. Haapea et al. 2002 reported, that electrical power consumption to produce pure ozone from air is 17-30 kWh/kg[O.sub.3].

Considering that Salutaguse Yeast Factory has daily 350 [m.sup.3]/d of wastewater to be treated using ozonation process it could be proposed that up to 495 g[O.sub.3]/d is required. It corresponds to 8415-14850 kWh/d of electrical energy consumption. In addition to the above mentioned installation a modern ozone generator is needed.

4. Conclusions

1. The results of coagulation-significant decrease of colour substances and also COD concentration could be achieved.

2. Colour removal by coagulation process using aluminium sulphate and ferrous chloride was more than 80%.

3. The most effective coagulants were (Fe[Cl.sub.3]x6[H.sub.2]O and [Al.sub.2] [(S[O.sub.4]).sub.3]) however, the required amount of inorganic coagulants was relatively high.

4. The post-treatment method of yeast factory effluent with coagulants and ozone can be used in the tertiary treatment of yeast wastewater, but the treatment is very expensive.

Submitted 19 November 2008; accepted 27 February 2009


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Viktoria BLONSKAJA. Researcher, PhD (1983), number of publications-55. Research interests: sewage and industrial wastewater treatment, sludge treatment.

Sergei ZUB. AS Salutaguse Parmitehas, manager of wastewater treatment plant, PhD (2008), number of publications-6. Research interests: sewage and industrial wastewater treatment, sludge treatment.

DOI: 10.3845/1648-6897.2009.17.

Viktoria Blonskaja (1) and Sergei Zub (2)

(1) Department of Environmental Engineering, Tallinn University of Technology, Ehitajate tee 5, 19086 Tallinn, Estonia (2) Salutaguse Yeast Factory, Kohila, 79702 Raplamaa, Estonia E-mail: (1); (2)
Table 1. The results of the treatment process

 Influent, mg/l

Years tot COD TSS N tot P tot S[O.sub.4]

2003 22 650 20 185 2 391 1 702 60 2 207
2004 22 975 20 542 2 433 1 853 32 2 475
2005 24 207 21 545 2 661 1 645 52 1 879
2006 31 798 29 330 2 468 2 706 81 3 521
2007 32 587 30 388 2 174 2 625 50 2 360
2008 34 945 31 150 3 795 -- -- 2 250


 Effluent, mg/l

Years tot COD TSS N tot P tot S[O.sub.4]

2003 2 723 2 183 486 395 45 343
2004 2 504 2 038 466 463 33 343
2005 4 368 3 555 813 533 29 235
2006 4 348 3 931 416 394 15 94
2007 2 744 2 446 314 490 20 20
2008 4 330 3 825 505 -- -- --

Helcom 250 10 2

--not detected

Table 2. Treatment effect during 6 years

Removal % 2003 2004 2005 2006 2007 2008

COD 88 89 85 86 92 88
H.a 90 84 87 92 87
Sulphate 84 86 88 97 99 --
N tot 77 85 68 85 81 --
P tot 25 -- 25 81 60 --

Table 3. The results of experiments with coagulants

 Acting Fe(Al)
Type of coagulants/floculants concentration, mg/l

Fe[Cl.sub.3]x6[H.sub.2]O 65 200 375 535
[Al.sub.2][(S[O.sub.4]).sub.3] 80 150 250 350
[Fe.sub.2][(S[O.sub.4]).sub.3] 150 350 450 700
[Al.sub.2][(OH).sub.6-x] 125 200 300 350
 [Cl.sub.x] * Y[H.sub.2]O
Zetak 7563 * 5
Zetak 7587 * 5 1 0,5
Zetak 7635 * 5
Magnofloks10 * 5

Type of coagulants/floculants The COD removal, %

Fe[Cl.sub.3]x6[H.sub.2]O 45 54 28 26
[Al.sub.2][(S[O.sub.4]).sub.3] 36 38 31 43
[Fe.sub.2][(S[O.sub.4]).sub.3] 10 30
[Al.sub.2][(OH).sub.6-x] 7 4 -- --
 [Cl.sub.x] * Y[H.sub.2]O
Zetak 7563 * 0
Zetak 7587 * 57 50 44
Zetak 7635 * 20
Magnofloks10 * 29

* Were used for sludge setting

Table 4. Performance of iron coagulation stage

 Acting Fe concentration, mg/l

 0 50 100 150 200 500

[COD.sub.tot], mg / l 2120 1750 1350 1040 830 710
Phenols, mg / l 288 260 224 178 125 99
[], mg / l 21 18.3 15,2 10,2 4,5 2.1
[], mg / l 310 245 125 101 78 61
[OD.sub.580] 0.414 0.380 0.331 0.250 0.165 0.067
Sludge percentage, -- ND ND 5.4 15.8 63.4
 % vol *.
SVI, ml [g.sup.-1] -- ND ND 210 270 420
Sludge VSS/TSS, % -- ND ND 90 88.9 33.5

* after 30 min of settling; ND-not detected

Table 5. Performance of aluminium coagulation stage

 Acting Al concentration, mg / l

 0 100 200 400 600 800

[COD.sub.tot], mg / l 2120 1910 1690 1270 800 760
Phenols, mg / l 288 144 82 67 64 59
[], mg / l 21 15.7 7.2 4.5 3.4 1.5
[], mg / l 310 180 112 74 65 54
[OD.sub.580] 0.414 0.361 0.139 0.112 0.076 0.065
Sludge percentage, -- 35.5 91.4 93.5 94.4 96.3
 % vol *.
SVI, ml [g.sup.-1] -- 655 615 545 355 341
Sludge VSS/TSS, % -- 42 52.4 56.5 52.2 39.8

Table 6. Results of post-ozonation of biologically treated wastewater

 WWTP effluent, mg/l Consumed ozone dosage,
 dn/[DELTA]COD, mg[O.sub.3]
Run [COD.sub.tot] BOD BOD/COD /mgCOD

1 2055 161 0.08 2.45
2 2120 579 0.27 2.47
3 1480 204 0.14 2.2
4 1860 308 0.17 1.2
5 1940 147 0.08 1.6

 Efficiency of Effluent after post-ozonation mg/l
Run [DELTA]COD, % [COD.sub.tot] BOD BOD/COD

1 30 1460 317 0.22
2 31 1470 381 0.26
3 34 970 310 0.32
4 49 940 297 0.32
5 30 1430 250 0.17
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Author:Blonskaja, Viktoria; Zub, Sergei
Publication:Journal of Environmental Engineering and Landscape Management
Article Type:Report
Geographic Code:4EXLT
Date:Dec 1, 2009
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