Comparison of Ozonation and Evaporation as Treatment Methods of Recycled Water for Bioethanol Fermentation Process
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The paper compared the performance of the ethanol yield after alcoholic fermentation with samples of rejected (RW) and permeate water (PW), RW and PW treated by oxidation with ozone (O3) (5 and 15 min) and evaporation, aiming the recirculation back to the bioethanol process. RW and PW were collected after an anaerobic bioreactor (AnBR) used for stillage treatment. Nine types of fermentations were made, where one used 100% tap water (control) and the remaining used 80% of recycled water and 20% of tap water. Comparing with the control (15.68%), evaporated permeate water and permeate water oxidized for 15 min achieved the highest and closest ethanol concentrations in v/v with 14.68 and 14.08% respectively. RW and PW had the lowest ethanol results with 8.43 and 8.68%. The studied methods for water treatment are effective to recycle water taking into consideration the ethanol yield, allowing a good possibility of recirculation. Chemical oxygen demand, ammonia nitrogen and phosphate content did not strongly affect the ethanol yield in all samples treated, with similar results. Oxidation was more environmental friendly and cheaper if performed in 5 min. Further research in the monitoring of the fermentation, ethanol quality and in the number of cycles of fermentation with recycled water is needed.
KeywordsFermentation Recycling Waste-water Waste treatment and waste minimisation Evaporation Ozonation
Biological oxygen demand
Chemical oxygen demand
Evaporated permeate water
Evaporated rejected water
Headspace capillary gas chromatography–mass spectrometry
Kilowatts per hour
Ammonia nitrogen content
Permeate water oxidized for 15 min
Permeate water oxidized for 5 min
Rejected water oxidized for 15 min
Rejected water oxidized for 5 min
Ethanol is one of the most common and abundant compounds especially in the chemical and food industry. Ethanol is commonly used as a solvent and heating agent, reagent in synthesis and it is used also in, flavoring and medicine. The ethanol is mainly produced by fermentation, where agricultural products like sugarcane, corn, wheat and others are used as raw material . There are two methods to produce ethanol, wet-mill and dry-grind process [2, 3, 4, 5, 6, 7]. Saccharomyces cerevisiae is the most popular and studied microorganism in alcoholic fermentation. It can produce ethanol concentrations in broth up to 18% (v/v), grow and survive within those values and can be compatible with other microorganisms present in the fermentation [8, 9, 10]. To obtain ethanol in a purity of 96 and 99% distillation and dehydration processes can be performed respectively [2, 11].
Stillage is produced in the bottom of the distillation column, presenting a dark brown color, acidic nature (pH 4–5) and a temperature between 70 and 80 °C. The presence of phenols and melanoidins are responsible for the dark brown color [1, 11, 12]. Chemical characteristics of the stillage differ, depending on the bioethanol feedstock, including chemical oxygen demand (COD) (15–176 gO2/L), biological oxygen demand (BOD) (7–96 gO2/L), total nitrogen content (0.2–4.2 g/L), total phosphate content (0.2–3.0 g/L), potassium (0.9–17.5 g/L) and sulfate content (2–6 g/L) [12, 13]. Treatments such as aerobic and anaerobic digestion, oxidation, adsorption, coagulation/flocculation, membrane separation, evaporation can be used to reduce the organic load of the stillage. One of the most popular process is the anaerobic digestion of the stillage. This process removes and reduces the content of COD and BOD, converts half of the COD in biogas and 10% in sludge [11, 12, 14, 15]. It can be successfully operated at high organic loading rates, low nutrient and energy requirements and stabilized sludge production [1, 5, 6, 7, 12]. Typical digestates from this type of treatment include among others total COD (around 55 g/L), sulfur based COD (around 10 g/L), nitrogen content (0.7–2.5 g/L) and phosphate content (1.5–10 g/l) [4, 5, 6, 7].
Even though the anaerobic digestion can reduce significantly the organic load of the stillage, but it is not enough effective if the purpose is to use the digestate to recycle it back to the fermentation process. In the recent years several studies were done to obtain a possibility of full recycle the treated water from the stillage, applying a further stages of treatment. This would enable to save water, minimize the waste produced and reduce the impact on the environment. Several technologies were tested and are already implemented in the industry. These technologies can include one stage treatment, namely simple centrifugation of the stillage [4, 16]. Others attempt to implement combination of treatment technologies like biological–physical process, namely a two stage anaerobic digestion and a centrifugation stage between the two anaerobic digestion stages [7, 17, 18, 19, 20]. Furthermore a two-step physical processes, like filtration and evaporation  as well as centrifugation and membrane filters  were studied. In this paper a biological–chemical and a biological-physical treatment processes are proposed. The use of chemical purification by means of oxidation no additional waste is produced, thus minimizing the impact on the environment when comparing with physical processes.
O3 is a powerful oxidizing agent, with a standard oxidation potential (E°) equivalent to 2.07 V, and is widely used in wastewater treatment and in treatment of tap water. It can decompose rapidly to free radicals that can instantly react with the organic compounds. The advantages of O3 are high reaction rate, almost a lack of harmful by-products formation and generating oxygen (O2) as an end product [22, 23]. Once present in a basic solution, O3 reacts with OH− producing hydroxyl radicals (E° 2.7 V) which are more reactive than O3 [23, 24, 25]. Another advantage of using O3 is the disinfection, i.e. ability to efficiently inactivate microorganisms. Disinfection with O3 is widely used in drinking water treatment and its efficiency depends upon the oxidation time and the concentration of used ozone . An evaporation process is proposed in this paper. The stillage is concentrated into syrup and the condensate, which has a low organic load and no inorganic salts and it can be used in closed cycle in the process [11, 12]. Evaporation can also inactivate microorganisms by heat and pressure shock. At the end, the collected distillate is free from the microorganisms and solid matter. The disadvantage of this process remains on the fact that no reaction occurs here, only separation, where the syrup has high concentration of organic load that still needs to be treated, which is considered an extra waste to the process.
The goal of this paper was to evaluate the possibility of recycling the treated wastewater to the fermentation process using evaporation or ozonation treatment, taking into account the ethanol yield. With this approach the goal is to reduce to the maximum the residues or wastes generated from stillage treatment and obtain a more environment friendly technologies. The treatment was applied to digester effluents, coming from different streams of an anaerobic digestion, namely rejected water (RW) and permeate water (PW). A comparison between ozonation for 5 and 15 min and evaporation of RW and PW samples and RW and PW samples without secondary treatment were performed. Chemical properties like COD, pH, ammonia nitrogen content (N-NH3) and phosphate content (PO43−) were compared in all studied processes. The effect of the chemical properties of all liquid samples on the ethanol yield was also studied.
Materials and Methods
Fermentation experiments were carried out using different types of water, containing 80% of recycled water and 20% of tap water, to determine the ethanol concentration in v/v and compared with control fermentation. Ethanol yield present in each fermentation was determined by HS-CGC–MS. The recycled water used passed by a secondary treatment, to increase the ethanol yield and purity of the digester effluents, i.e. PW and RW. Furthermore the efficiency of each treatment was controlled by COD, N-NH3 and PO43− removal.
Approximately 0.90 dm3 of RW and 0.70 dm3 of PW were kindly given by Veolia research laboratory (Netherlands). Figure 1 explains the method used in this work and the source of the samples used. The stillage comes from the bottom of the distillation column, where the fermentation broth is fed to produce ethanol which is collected at the top of the column. Afterwards it was first submitted to a centrifugation, where the liquid fraction was submitted to an anaerobic digestion in an Anaerobic Bioreactor (AnBR) coupled with an ultrafiltration equipment. PW was collected from the filtrate stream of the ultrafiltration. RW was collected from the liquid fraction of the centrifugation of the sludge from the AnBR. Both RW and PW can be considered digester effluents throughout this paper.
Evaporation was performed by a Heidoph Laborota 4000 efficient, vacuum rotary evaporator. A Heidolph 2 condenser was used as a condenser of the distillate. The operational conditions were, stirring at 60 rpm, vacuum pressure between 75 and 79 kPa and a temperature between 70 and 73 °C.
The gravimetric method was chosen as a first step to determine the ozonator efficiency. It was determined using a sodium sulfite solution during a certain period of oxidation time, using the apparatus in Fig. 2. The O3 molecules oxidize sulfite (SO32−) to sulfate (SO42−) which was determined gravimetrically as barium sulfate (BaSO4) salt. The flowrate of the streams was calculated to determine the molar flowrate of ozone that came out of the ozonator. Afterwards the oxidation system was prepared so that the ozonator would receive air instead of pure oxygen. The scheme of the oxidation system is presented in Fig. 2. Each flask was stirred by a magnetic spinner. Two flat bottom flasks with a porous frit were used in the oxidation procedures. The two flasks were sealed at top to avoid O3 loss. The flow reducing stream was used to reduce the flowrate to the flasks, which went to the venting system. Experimental procedures determined a flowrate around of 6.60 dm3/min in the stream leaving the ozonator, 6 dm3/min to the atmosphere and 0.60 dm3/min to the experimental flasks. O3 concentration determined was 75 mg/dm3. The ozonator used was an ozone generator type Tytan 32. The flowrate of the ozonator was set at 5.0 dm3/min. The pressure of the streams was 196 kPa. Approximately 0.10 dm3 of RW and PW samples were oxidized in the conditions described above for 5 and 15 min with O3 doses of 1.87 × 10−3 and 5.60 × 10−3 kg respectively. Oxidation was made at the primary pH of the samples and at room temperature.
Starch Conversion and Fermentation
The dry-grind process was used to carry out the fermentations done is this work, using corn as feedstock. Figure 1 described the steps to perform the fermentation. S. cerevisiae was the microorganism used to perform the fermentations. The preparation of the yeast and starch conversion was carried out in the following steps.The corn was kindly provided by Veolia Company. A 1 kg of corn was grinded in a Retsch type ZM200 mill. A 0.02 kg of milled corn was weighted using an analytical balance and transferred to the fermentation flask. A 0.10 dm3 of water was added into the flask, where in the control fermentation (CF) only tap water was used. In the rest of the fermentations a mixture of 80% of recycled water and 20% of tap water were used. Afterwards the pH was adjusted to 5.5 with HCl (35–38%) using a Hana type HI8817 pH-meter, 1.0 × 10−4 dm3 of α-amilase (liquefying enzyme provided by Veolia) was added and the mixture was heated to 85 °C and mixed for 60 min s in the heater described above. To monitor the starch degradation to simpler sugars an iodine test was performed with Lugol’s solution every 15 min. The test was stopped when there was no color change in the solution. Afterwards, the mash was cooled down to 60 °C, the pH was adjusted to 4.8 with HCl (35–38%) and 1 × 10−4 dm3 of glucoamylase (saccharification enzyme provided by Veolia) was added. After 5 and 15 min of adding the enzyme the iodine test was performed. When the mash reached 35 °C, 5.0 × 10−4 kg of dry yeast S. cerevisiae and 1.0 × 10−4 kg of Ammonium phosphate dibasic were added. The pH was adjusted to 4.8 with HCl 35–38% and the fermentation started in a 0.25 dm3 round flasks with a flat bottom inside a heater chamber research NCB-65G dryer, at 35 °C for 2 days without stirring. Liquid samples for ethanol determination were collected at the end of fermentation and filtered by a Millipore hydrophilic filter with a 0.45 µm pore diameter. A gas collection system was prepared to control the CO2 production rate during the fermentation. At the end of the airlock of the fermentation flask, a steal capillary was installed in order to collect the gases into two (connected in parallel) 3 dm3 tedlar bags immersed in water inside a recipient. A 2.0 dm3 beaker collected the water which came out from the recipient (when gas entered in the bags).
The determination of the COD was made by standard cuvette test. A Hach DRB 200 heater was used for mineralization. The analyses were made in duplicate samples. A Hach DR/2000 Spectrometer was used to read the COD values. N-NH3 was determined by the Nessler method, using the same spectrophotometer. The PO43− was also measured by the method 8048 developed by HACH . The ethanol concentration was analyzed by headspace capillary gas chromatography-mass spectrometry (HS-CGC–MS) [27, 28, 29]. The equipment used was a HP gas chromatograph, model 5890 series II and a HP single mass spectrometer quadrupole type, model 5972 A. A two point calibration curve for ethanol was used. The calibration points were 2 and 15% v/v. The samples were heated in the chamber at 80 °C for 45 min. Afterwards 2.0 × 10−4 dm3 of the gas phase was sampled by a gastight syringe and injected to the GC for analysis. The software used was the HP ChemStation. Every analysis was made in triplicate. The chromatographic parameters for the ethanol analysis are the following. Initial temperature 35 °C (5 min isothermal); rate of increasing 10 °C/min; final temperature 150 °C; gas used H2; flow 1.02 × 10−3 dm3/min; split ratio 20:1; column specifications DB-5ms (Agilent, USA) 60 m × 0.25 mm × 1.40 μm; injector temperature; 200 °C; detector temperature 200 °C. Using the calibration curve (external standard), concentration of ethanol was determined in percent (v/v).
Results and Discussion
The possibility of recycling water from a two stage stillage treatment was evaluated on the basis of the ethanol yield and compared with the CF. Furthermore an economical evaluation was performed on basis of the operational costs of each treatment studied.
Chemical Properties of RW and PW and Treated by O3 and Evaporation
The samples were analysed for pH, COD, N-NH3 and PO43− before and after treatment and their respective removal after treatment are represented in Table 1. The types of water studied and used in fermentations were the RW, PW, evaporated rejected water (ERW), evaporated permeate water (EPW), rejected water oxidized for 5 min (RWox5), rejected water oxidized for 15 min (RWox15), permeate water oxidized for 5 min (PWox5) and permeate water oxidized for 15 min (PWox15). A standard test method was used in all cases described in this work. In Table 2 the percentage of removal of the treated samples with ozonation and distillation is summarized. All samples of RW and PW treated revealed COD removal, where the ERW and EPW had higher COD removal. Regarding PO43−, it also decreased in all samples except the RWox5 and RWox15, where it increased 57.5 and 27.92% respectively when comparing with the RW.
Chemical properties of samples studied and their reduction after treatment
COD removal (%)
N/NH3 removal (%)
PO43− removal (%)
3635 ± 64
816 ± 21
12 ± 0
18 ± 0
3605 ± 71
3260 ± 35
428 ± 4
407 ± 10
Determination of the energy costs of each treatment applied in rejected and permeate water (RW and PW)
Equipment power (W)
Heat of vaporization (KJ/kg)
Volume treated (L)
Time of treatment (min)
Energy/volume treated (kWh)
Energy per m3 (kWh/m3)
Energy cost ($/m3)
Regarding the EPW and ERW, they were almost completely purified, with total removal of PO43−, which remained in the syrup. A 97.79 and 99.67% COD removal and partial removal of N-NH3 by 16.19 and 46.71% respectively was achieved. These results suggested a good separation of the organic load from the water.
Analysis of the results revealed that regarding the oxidized rejected water, there was partial removal of N-NH3 by 24.45% in RWox5 and 38.19% in RWox15. Phosphate removal was the opposite of the rest of the treatments with an increase of 57.50% in RWox5 and 27.92% in RWox15. A possible explanation can be related to the analysis of the phosphate content, which is related with the dissolved orthophosphate. Since the rejected water had some solid particles, organic phosphate digestion could occur during oxidation. The COD removal was 0.83% in RWox5 and 10.32% in RWox15. A possible explanation for such behavior can be related with the nature of the RW, which is more persistent to oxidation. In addition the COD reduction in 5 min of oxidation was 30 mg/L and in 15 min was 375 mg/L. The COD removal does not explain the differences in the ethanol yield, but it is clear that longer oxidation results in higher removal of COD, N-NH3 and PO43−.
Regarding the oxidized permeate water, its observable a high COD removal in first 5 min of oxidation, with 47.55% but after 15 min only an increase of 2.57% was observable comparing with 5 min of oxidation to 50.12%. PO43− removal was 59.36% in the PWox5 and 64.17% in the PWox15. The N-NH3 removal was 8.10% in the PWox5 and 27.14% PWox15. It is clear that longer oxidation time increased the removal rates of COD, N-NH3 and phosphate, but the removal was higher in the first minutes of oxidation.
Regarding the time of oxidation in overall higher oxidation time, it increased the removal of COD, N-NH3 and PO43−, with only one exception that was the PO43− in the RW.
Comparing the evaporation with oxidation as treatment methods for PW and RW, evaporation revealed by far higher COD and phosphate removal values, with more than 97.5 and 100% respectively. Regarding N-NH3 removal, EPW was lower than PWox15 (16 and 27%) and higher in the ERW comparing with RWox15 (47 and 38%). Evaporation results in higher removal values and quality of treated water, suggesting a good separation between water and the organic load. However the syrup produced results in additional waste generated, which is highly concentrated in organic compounds. In the oxidation no additional waste is generated, resulting in a more environmental friendly technology [23, 24].
Analysing the pH of all oxidation processes, it can be said that the pH was not optimal if the goal was to remove organic load from the water [23, 24]. Since the treated water had to be re-used in fermentation, alkaline pH would not be a reasonable choice, since the adjustment of the pH value would be a problem in a close cycle, which would increase the cost of the process. Furthermore the closer the pH of the recycled water to the pH of the tap water, the lesser amount of chemicals would be needed to adjust the pH value. Thus not changing the pH was the best choice.
A comparison of the concentration of ethanol in percent v/v for of all fermentations performed is presented in Fig. 3, which can be described as the ethanol yield of the fermentation due to the fact that the same final volume of water was obtained after fermentation. The CF (using only tap water) achieved 15.65% (v/v) of ethanol concentration very similar to values reported by Wang et al.  (15.5%). PWox15 and ERW had the highest ethanol concentrations, 14.08 and 14.68% v/v. The RWox15, ERW, PWox5 and RWox5 obtained reasonable ethanol concentrations v/v by 13.75, 12.74, 12.81 and 11.98% respectively, with values in the range of ethanol concentration in the fermentation broth [2, 3, 8]. It is clear that the recycled treated digester effluents had a twofold increase of the ethanol yield, when comparing with recycled untreated digester effluent (samples RW and PW).
Comparing the PWox15 and RWox15, similar values were found in ethanol concentration (14.08 and 13.75% respectively). Even though COD, PO43− and N-NH3 values were higher in RWox than in PWox (8.4 times in COD; 1.5 times in N/NH3; 1.15 times in phosphate), it did not seemed to make a strong effect on the ethanol yield. Thus the ethanol yield is not dependent on the COD, N-NH3 and PO43− content in the range of concentrations reported in this paper.
Comparing the RW and PW oxidized for 5 and 15 min, the ethanol yield increased for samples collected after 5–15 min of oxidation (PW 12.84–14.08% and RW 11.98 and 13.75%) revealing that longer exposure to O3 could enhance the ethanol yield.
The comparison between evaporation and oxidation treatments regarding the ethanol yield as performed. Regarding PW, EPW and PWox15 achieved similar ethanol yields (14.68 and 14.05% respectively). On the other hand in RW. Even though ERW had higher treatment efficiency, it obtained 1% lower ethanol yield than RWox15 (12.74 and 13.75%). Nevertheless the results are not significant different between treatments for PW and RW. The RW and PW had the lowest ethanol concentration in (v/v) of all fermentations performed with 8.43 and 8.68% respectively, which was approximately half of ethanol yield for the CF and some treated samples. These results are comparable with values of Gao et al.  which obtained 9.5% (v/v) ethanol concentrations using 90.9% (v/v) of the treated water by anaerobic digestion. Likewise Bialas et al.  obtained 9.5% (v/v) ethanol concentration using 75% of the treated water from a distillation process. Sun et al.  used a combination of two-stage UASB treatment on the treatment of stillage and also obtain ethanol concentrations around 10% using 100% of treated water. This study proved that the treatment of the digester effluent can increase significantly the ethanol yield to values close to the control fermentation. The combination of biological and physical/chemical treatment of the recycled stillage revealed to be effective in terms of ethanol yield after fermentation.
It is clear that is necessary to study BOD, sugars, microorganisms, acids and by-products during the fermentation, to determine if there are any inhibitions leading to lower ethanol production and consequently ethanol yield. In addition there is a need to conduct several recycle fermentations with the recycled water to check if the accumulation of the chemical parameters discussed here can influence the ethanol yield.
Figure 4 presents the CO2 production rate during the fermentation. The studies revealed that PWox15 had lowest production of CO2 (2.85 dm3), even lower than PW (3 dm3). In addition CF had similar values than DPW (3.27 comparing with 3.26 dm3). These results are not consistent with the ethanol yields described above. This proves that there is no relation between the ethanol yield and the CO2 production. Four phases in the alcoholic fermentation in respect to the CO2 production were observed. The lag phase can be seen between 0 and 2 h of fermentation, the exponential phase of CO2 production was between 2 and 8 h of fermentation, and from 8 to approximately 20 h of fermentation the CO2 production rate decreased significantly, where differences started to be noted. After 20 h of fermentation the CO2 production rate decreased to values close to zero, where this period can be considered as the stationary phase.
An economical evaluation was performed to determine which of the studied technologies is cheaper to implement in a real case scenario. The approach used was the determination of the operational costs. Since no chemicals are used in evaporation or ozonation, the operational costs are based only in the energy costs. The cost was determine for the treatment of 1 m3 of RW and PW. The power used in kilowatts per hour (kWh) was first determine for the volume of RW and PW treated in this work. In the case of ozonation it was done by multiplying the equipment power by the time of treatment. In evaporation it was determined by multiplying the mass of water treated by the heat of evaporation of water at atmospheric pressure and temperature. It was omitted the influence of salts, and particles on this value. It was considered an efficiency of 80% in the evaporation. Afterwards an energy consumption followed by the energy cost to treat 1 m3 of RW and PW was determined. In this work, the power of the ozonator was 450 W. The time of treatment was 5 and 15 min in the ozonation. The volume of RW and PW used is presented in Table 2. The heat of vaporization of water is 2257 KJ/kg. The energy cost in Poland for industrial clients is 0.1015 American dollars ($) per kWh (Fig. 4).
Looking to Table 2 it is proved that oxidation treatment is the cheapest with a value of 38 $/m3, but if the treatment is extended to 15 min the scenario changes and oxidation is more expensive with 114 $/m3 comparing with 80 $/m3 in evaporation technology. Taking this into account evaporation and oxidation during 15 min, it can be said that evaporation is the most economical choice, in basis of energy costs.
The aim of this study was to compare an evaporation and oxidation as a final stage of stillage treatment to recycle the treated water and use it in the ethanol process, namely the fermentation process. This comparison was made by analyzing the ethanol yield of all samples, with additional analysis of chemical parameters like COD, N-HH3 and PO43− content to check their influence in the ethanol yield. Longer oxidation time revealed higher ethanol yields and removal values of COD, N-HH3 and PO43− content, generating higher quality of treated WW. In overall evaporation achieved higher removal values in the parameters studied, generating higher quality of treated water. Nevertheless it produces additional waste with high content of phosphate, COD and N-NH3 which still needs treatment.
Regarding the efficiency of the fermentations, in respect to the ethanol yield, the results achieved were acceptable and close to the levels of the control fermentation. The chemical treatment after anaerobic treatment reveals to be a cleaner technology comparing with evaporation. In addition oxidation in 5 min revealed to be cheaper than evaporation in terms of operational costs, but in 15 min is more expensive than evaporation. Moreover all treated PW and RW and CF were within the range of normal ethanol yields [2, 3, 8], with PW having slightly higher values than treated RW. The COD, N-HH3 and PO43− content did not affect strongly the ethanol yields in all samples treated, proving that there is no connection between them. This conclusion is limited to the concentration level of this parameters and cannot be generalized. Thus the results are positive and enable a good possibility of recirculation of treated PW and RW in the alcoholic fermentation process and minimizing the waste produced in a bioethanol facility.
Nevertheless further research is needed to determine the main inhibitors which made the RW and PW untreated achieved only approximately half of the ethanol concentration in (v/v) in CF. Likewise fermentation parameters and by-products should also be monitored. In addition the monitoring of the quality of ethanol produced by the recycled water should be performed. The number of cycles of fermentation plays an important role regarding the implementation in industrial facility. This aspect needs further research to understand if the number of cycles of fermentation affects the ethanol production and quality. The results of this paper were used for patent registration of the technology of closed cycle in ethanol fermentation .
The authors would like to thank the Veolia, especially dr Bugusław Buczak (PhD. Eng.; Veolia Water), and Komers International for their cooperation on this project. The authors would like to thank also Mr. Wiesław Szyrszyng (Eng.) for technical help during the studies. This paper has been in part realized in the scope of project entitled Studies of alkaline hydrolysis of lignocellulosic biomass and conversion conditions of hydrolized products to biogas supported by National Science Centre Poland, (UMO-2014/13/B/ST8/04258).
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