Evaluation of membrane bioreactor for advanced treatment of industrial wastewater and reverse osmosis pretreatment
© Hosseinzadeh et al.; licensee BioMed Central Ltd. 2013
Received: 5 April 2013
Accepted: 23 September 2013
Published: 19 December 2013
The evaluation of a membrane bioreactor (MBR) for pretreatment of reverse osmosis (RO) in order to reuse and reclamation of industrial town wastewater treatment plant was investigated in this study. Performance of MBR effluent through water quality in term of parameters such as chemical oxygen demand (COD), total suspended solids (TSS), total nitrogen (TN) and total coliform (TC) were measured. Also Silt density index (SDI) was used as indicator for RO feed water. The results of this study demonstrated that MBR produce a high quality permeate water. Approximately 75%, 98%, 74% and 99.9% removal of COD, TSS, TN and TC were recorded, respectively. Also SDI of the permeate effluent from membrane was below 3 for most of the times. It means that pilot yield a high quality treated effluent from the membrane module which can be used as RO feed water.
Nowadays water resources are becoming increasingly scarce in many areas of the world particularly in arid regions such as Middle East due to factors such as increasing population, climate changes, industrial development and increasing water use per capita, etc. Because of the scarcity of water resources, wastewater reclamation and reuse is an effective tool for sustainable industrial development program in both developing and developed countries. Currently, treated industrial wastewater is typically discharged to the environment in most industrial towns in Iran. These effluents have a potential to reclamation and reuse for produce industrial process water. For reach this reuse application further treatment would be needed. Nowadays membrane separation processes are becoming quite popular in wastewater treatment and reclamation, since they combine process stability with an excellent effluent quality [1–4]. One of this membrane processes for water reuse and reclamation is reverse osmosis (RO) that is increasingly being used in all over the world [5–9]. The main problem of using RO is its membrane fouling that is prevalent in water reclamation applications. In fact membrane fouling is the main cause of permeate flux decline and loss of product quality in reverse osmosis Systems [10, 11]. Sources of fouling can be divided into four principal categories: scaling, particular fouling, bio fouling and organic fouling. To avoid common issues that can result in system failure, RO systems need to be coupled with an effective pretreatment.
MBR has been widely studied and applied on full scale in wastewater treatment and it is considered as a new pretreatment for reverse osmosis in water reclamation and reuse among many different pretreatment schemes for RO [12–18].
MBR is a process in which conventional biological system is coupled with the membrane process. There are two configurations for MBRs which are in-series and submerged MBRs which submerged membrane bioreactors have lower power requirements than the in-series configurations [19, 20].
Due to the shortage of water resources in the Shokouhieh industrial town (located in Qom province, Iran) reclamation and reuse of industrial wastewater treatment plant effluent using RO modules was put on the agenda. Effluents of this WWTP were not being adequately treated by biological treatment and there are biodegradable organic matters in effluent of wastewater treatment plant. This research has focused on the evaluation of the pilot scale operation and monitor of an MBR system to advance treatment of an industrial wastewater treatment plant effluent in order to produce water with appreciate quality as RO feed water. In other words this study has discussed the feasibility of RO pretreatment for water reuse from industrial wastewater treatment effluent (before disinfection) with operation of a MBR pilot. The removal of certain pollution parameters such as chemical oxygen demand (COD), suspended solids (SS), total nitrogen (TN) and total coliform (TC) were monitored.
Material and methods
Shokouhieh effluent characteristics
7.3 ± 0.62
223 ± 32
250 ± 64
51 ± 30
1.75×106 ± 35×104
MBR pilot unit
Specification of membrane
Dimensions (Width × Height)
Effective surface area
pH resistance range
Membrane was operated at a constant flow rate of 4 L/hr using a prestaltic pump. Air blower was used to provide required sufficient air during operating the MBR. Air was introduced via perforated plastic tube air diffusers which were located at the bottom of the reactor to produce fine and coarse bubbles for supply dissolved oxygen required for biological process in the reactor and reduce fouling on the membrane, respectively. Also pilot was equipped with control instruments for measuring temperature, dissolved oxygen (DO), pH and wastewater level.
Operation condition for MBR
Mode of operation
Permeate flow rate
pH in reactor
Mixed liquor DO
The membrane was cleaned chemically once the pressure reached about 60 kPa. In this stage after taking out the membrane, it was soaked in a 250 mg/L NaOCl solution and afterwards with 4000 mg/L citric acid solution for at least 4 hours. Then membrane was cleaned with tap water. Fine bubble aeration was provided to maintain the dissolved oxygen (DO) concentration in the biological reactor higher than 2 mg/L. Fine bubble aeration was accomplished using suitable diffusers placed at the bottom of the biological reactor. Also coarse bubble aeration was supplied to the membrane module to minimize membrane fouling.
Laboratory analyses were conducted to determine the characteristics of influent wastewater to pilot, activated sludge and MBR permeate. For this, suspended solids, chemical oxygen demand, total nitrogen and total coliform were analyzed. Most analytical techniques used in this research followed the standard methods described by APHA . Data in this paper was averaged by at least 2 experiment results at each process. MLSS was measured with a Whatman glass microfiber filter using APHA 2540E standard method. The COD content of the samples was measured using Hach COD reactor and TN of the samples was measured using the Merck TN kit. The determination of total coliform was carried out for MBR feed and permeate samples using standard method 9222 B procedure.
The temperature of inlet and outlet stream of MBR and MLSS temperature in the reactor was monitored using a digital temperature probe (JENWAY, England ). These data were verified periodically using an alcohol thermometer. Also MBR influent and effluent pH value were determined using a portable pH meter (JENWAY-370, England) and dissolved oxygen meter was used to determine DO level at reactor (JENWAY-970, England).
Field emission scanning electron microscopy (FESEM) technique for new membrane and used membrane was employed to investigate the morphology of membrane fouling due to the deposition of particle, biomass and other foulants. Also X-ray fluorescence (XRF) spectrometer was used for chemical analysis of sediment layer. To do this used membrane sheets were taken off from MBR module. Tap water was sprayed at the surface to remove any particle and attached biomass. Then membrane was cut into small pieces by sterile blades under room temperature and sent to University of Tehran laboratory for XRF analysis and instant FESEM scanning.
T1= the time required to filter the first 500 mL
T2= the time required to filter the second 500 mL
T = the elapsed filtration time (normally 15 minutes) after the start of collecting the first 500 mL
Results and discussion
Permeate water quality of MBR
As in Figure 3(a) was shown excellent solids separation achieved by the UF membrane. Removal of SS reached greater than 98% resulting in the MBR permeate with SS levels below 3 mg/L.
Figure 3(b) shows the removal efficiencies of COD for influent and effluent of MBR reactor. COD was selected as indicator of organic pollution.
It can be seen that the inlet COD varied from 187 mg/L to 314 mg/L with the average COD concentration of the influent 222 mg/L whereas COD concentration in Effluent varied between 41 mg/L and 51 mg/L and average elimination rate was higher than 75%. It means MBR system has produced good removal of organic constituents and it was capable of achieving a high removal of COD and therefor organic load could be decreased effectively. Some studies reported more than 90% of COD removal which is higher than results of this study [22, 23]. Lower COD removal in this study may be related to less organic material concentration in the bioreactor. Most of biodegradable organic matters are used by microorganisms during conventional treatment process. Thus, MBR feed stream (WWTP effluent) has lower amount of biodegradable matter.
TN as one of the parameters representing the content of nutrient matters is widely used in the field of wastewater treatment. Figure 3(c) depicts the TN concentrations in inlet and outlet of the MBR as a function of operation time.
As illustrated in Figure 3(c), during the experimental period, the MBR was able to reduce TN from 51±32 mg/L in raw wastewater to 11±3 mg/L on average. This means that 74% of the nitrogen was removed. The most likely reason for removal of TN should be the fact that nitrogen was removed mainly through biodegradation by microorganisms and then separation with membrane. Similar results were reported in some previous studies [24–26].
The results of total coliform analyses done on the feed wastewater and MBR permeate are shown in Figure 3(d). As results show total coliform values in the MBR effluent samples ranged from 75 to 140 MPN/100 mL, giving an overall log removal of >4 log for the total coliforms. As Figure 3(d) shows there is a trend of decreased permeate coliform with increasing time of operation. This would be expected because as the membranes become clogged the pore size is decreased which results in removal of microorganisms and other particles which could normally pass through the membrane. These data show high performance of MBRs for microorganism reduction.
TMP trends of the MBR and membrane fouling
Membrane fouling behavior could be reflected by the developing rate of transmembrane pressure at the constant flux. As mentioned earlier this constant flux by using a prestaltic pump was set at membrane. The TMP of membrane in this study is the average driving pressure required filtering wastewater through the upper and lower membrane at the given flow rate. In the other hand the TMP is described as below:
TMP = (Psuction - Ppermeate) (2)
Psuction = Pressure measured on the suction side of the membrane
Ppermeate = Pressure measured on the permeate side of the membrane
It is obvious that TMP increased and went up slowly in exponential manner due to the fouling of the UF membrane. TMP reached 58 kPa on the 13th day of operation which was the fastest fouled MBR. In this stage particle, colloidal, biological and organic matters rapidly accumulated onto the membrane, and formed a cake which was probably compressible, leading to a rapid increase in the TMP. Some of these foulants are easily removed through physical wash by water, thus called reversible fouling. There is another fouling that is not readily removable from the membrane surface and requires use of chemical cleaning. As was mentioned before, for remove fouling in this study membrane was soaked in a 250 mg/L NaOCl solution and afterwards with 4000 mg/L citric acid solution for at least 4 hours. Then membrane was cleaned with tap water. However, it still remains a bit clogging of the membrane pores that are not washed away and caused pore blocking. During operation of MBR and several cleaning of membrane, pore blocking increases. Thus, as was shown in Figure 4, the time interval between the membrane washing is reduced during operation and cleaning of membrane repeats in a shorter duration.
From Figure 5, it could be seen that in comparison with the flat surface of the clean membrane, an irregular and rough gel layer was extensively distributed on the surface of the membrane in the reactor. The gel layer was found to be mainly consisted of abiotic matter which appeared to be dense and nonporous.
Results of XRF analysis for foulants
Al 2O 3
P 2O 5
Fe 2O 3
As it is obvious in Table 4, organic matters and calcium oxides constitute the main components of membrane fouling and contribution of other components such as heavy metals is negligible.
In some cases the permeate SDI of the module was more than 3. High levels of organic compounds and associated biofouling, micro-air bubbles and colloidal substances are the three most likely reasons for the unexpected increase in SDI as was mentioned in previous studies [27, 28]. In general SDI values of less than 3 leading to little fouling by the subsequent RO membranes. Therefore results demonstrate that MBR able to produce high quality effluent so that it would be suitable for use by an RO system.
In this study the possibility and applicability of MBR to reclaim effluent of an industrial wastewater treatment plant was investigated and the MBR pilot was evaluated in terms of effluent quality. In general, it can be concluded that MBR can produce high permeate quality and is capable to be a very efficient method for RO pretreatment. Product permeate from MBR with average SDI less than 3 indicate that if MBR use as RO pretreatment, it can be anticipated that the rate of RO membrane fouling will reduce and the life of RO membrane modules will extend.
Through FESEM examinations, a gel layer was observed to be formed on the membrane surface in the MBR during the operation. Analysis of XRF results shows that organic matters and calcium oxides are the main components of membrane fouling.
Also effluent water from the MBR has a high quality according to SS, COD, TN and TC removal during operation. These results are promising and all indications show that this method is feasible for RO pretreatment and water reuse of industrial application.
Experiments in this research were supported by the Qom Water and Wastewater Company and Shokouhieh Industrial Town Director. The authors are grateful to the head of these companies for their helps.
- Tam LS, Tang TW, Lau GN, Sharma KR, Chen GH: A pilot study for wastewater reclamation and reuse with MBR/RO and MF/RO systems. Desalination 2007, 202: 106–113. 10.1016/j.desal.2005.12.045View ArticleGoogle Scholar
- Wintgens T, Melin T, Scha fer A, Khan S, Muston M, Bixio D, Thoeye C: The role of membrane processes in municipal wastewater reclamation and reuse. Desalination 2006, 187: 271–282. 10.1016/j.desal.2005.04.086View ArticleGoogle Scholar
- Comerton AM, Andrews RC, Bagley DM: Evaluation of an MBR–RO system to produce high quality reuse water: microbial control, DBP formation and removal. Water Res 2005, 39: 3982–3990. 10.1016/j.watres.2005.07.014View ArticleGoogle Scholar
- Meier J, Melin T: Wastewater reclamation by PAC/NF process. Desalination 2005, 178: 27–40. 10.1016/j.desal.2004.12.015View ArticleGoogle Scholar
- Radjenovića J, Petrovića M, Venturac F, Barcelóa D: Rejection of pharmaceuticals in nanofiltration and reverse osmosis membrane drinking water treatment. Water Res 2008, 42: 3601–3610. 10.1016/j.watres.2008.05.020View ArticleGoogle Scholar
- Salahi A, Mohammadi T, Rekabdar F, Mahdavi H: Reverse osmosis of refinery Oily wastewater effluents. Iran J Environ Health Sci & Eng 2010,7(5):413–422.Google Scholar
- Gholami M, Mirzaei R, Kalantary R, Sabzali A, Gatei F: Performance evaluation of reverse osmosis technology for selected antibiotics removal from synthetic pharmaceutical wastewater. Iran J Environ Health Sci & Eng 2012, 9: 19. 10 December 2012 10.1186/1735-2746-9-19View ArticleGoogle Scholar
- Sahar E, David I, Gelman Y, Chikurel H, Aharoni A, Messalem R, Brenner A: the use of RO to remove emerging micropollutants following CAS/UF or MBR treatment of municipal wastewater. Desalination 2011, 273: 142–147. 10.1016/j.desal.2010.11.004View ArticleGoogle Scholar
- Fadhil Abid M, Abdulahad Zablouk M, Muhssen Abid-Alameer A: Experimental study of dye removal from industrial wastewater by membrane technologies of reverse osmosis and nanofiltration. Iran J Environ Health Sci & Eng 2012, 9: 17. 5 December 2012 10.1186/1735-2746-9-17View ArticleGoogle Scholar
- Alexei G: A simplified RO process design based on understanding of fouling mechanisms. Desalination 1999, 126: 227–247. 10.1016/S0011-9164(99)00179-4View ArticleGoogle Scholar
- Choia J, Tae-Mun H, Leea S, Hongb S: A systematic approach to determine the fouling index for a RO/NF membrane process. Desalination 2009, 238: 117–127. 10.1016/j.desal.2008.01.042View ArticleGoogle Scholar
- Malamis S, Katsou E, Takopoulos K, Demetriou P, Loizidou M: Assessment of metal removal, biomass activity and RO concentrate treatment in an MBR–RO system. J Hazard Mater 2012, 209: 1–8.View ArticleGoogle Scholar
- Sahar E, David I, Gelman Y, Chikurel H, Aharoni A, Messalem R, Brenner A: The use of RO to remove emerging micropollutants following CAS/UF or MBR treatment of municipal wastewater. Desalination 2011, 237: 142–147.View ArticleGoogle Scholar
- Kent F, Farahbakhsh K, Mahendran B, Jaklewicz M, Liss S, Zhou H: Water reclamation using reverse osmosis: analysis of fouling propagation given tertiary membrane filtration and MBR pretreatments. J Membr Sci 2011, 382: 328–338. 10.1016/j.memsci.2011.08.028View ArticleGoogle Scholar
- Liu HB, Yang C, Pu WH, Zhang JD: Removal of nitrogen from wastewater for reusing to boiler feed-water by an anaerobic/aerobic/membrane bioreactor. Chem Eng J 2008,2008(140):122–129.View ArticleGoogle Scholar
- Nelson MI, Balakrishnan EE, Sidhu HS, Chen XD: A fundamental analysis of continuous flow bioreactor models and membrane reactor models to process industrial wastewaters. Chem Eng J 2008, 140: 521–528. 10.1016/j.cej.2007.11.035View ArticleGoogle Scholar
- Dhaouadi H, Marrot B: Olive mill wastewater treatment in a membrane bioreactor: process feasibility and performances. Chem Eng J 2008, 145: 225–231. 10.1016/j.cej.2008.04.017View ArticleGoogle Scholar
- Lyko S, Al-Halbouni D, Wintgens T, Janot A, Hollender J, Dott W, Melin T: Polymeric compounds in activated sludge supernatant-characterisation and retention mechanisms at full-scale municipal membrane bioreactor. Water Res 2007, 41: 3894–3902. 10.1016/j.watres.2007.06.012View ArticleGoogle Scholar
- Gehlert G, Abdulkadir M, Fuhrmann J, Hapke J: Dynamic modeling of an ultrafiltration module for use in a membrane bioreactor. J Membr Sci 2005, 248: 63–71. 10.1016/j.memsci.2004.09.026View ArticleGoogle Scholar
- Ueda T, Hata K, Kikuoka Y, Seino O: Effects of aeration on suction pressure in a submerged membrane bioreactor. Water Res 1997, 31: 489–494. 10.1016/S0043-1354(96)00292-8View ArticleGoogle Scholar
- APHA, AWWA: Standard method for the examination of water and wastewater. 20th edition. Washington DC: American Public Health Association; 1998.Google Scholar
- Hoinkis J, Deowana S, Pantenb V, Figolic A, Huangd R, Driolic E: Membrane Bioreactor (MBR) Technology–a Promising Approach for Industrial Water Reuse. Procedia Eng 2012, 33: 234–241.View ArticleGoogle Scholar
- Qin J, Wai M, Tao G, Kekre K, Seah H: Membrane bioreactor study for reclamation of mixed sewage mostly from industrial sources. Sep Purif Technol 2007, 53: 296–300. 10.1016/j.seppur.2006.08.002View ArticleGoogle Scholar
- Dialynas E, Diamadopoulos E: Integration of a membrane bioreactor coupled with reverse osmosis for advanced treatment of municipal wastewater. Desalination 2009, 238: 309–311.View ArticleGoogle Scholar
- Jun Qin J, Kekre KA, Tao G, Oo MH, Wai MN, Cui Lee T, Viswanath B, Seah H: New option of MBR-RO process for production of NEWater from domestic sewage. J Membr Sci 2006, 272: 70–77. 10.1016/j.memsci.2005.07.023View ArticleGoogle Scholar
- Hai F, Tessmer K, Nguyen L, Kang J, Price W, Nghiem L: Removal of micropollutants by membrane bioreactor under temperature variation. J Membr Sci 2011, 383: 144–151. 10.1016/j.memsci.2011.08.047View ArticleGoogle Scholar
- Sombatsompop K: Membrane fouling studies in suspended and attached growth membrane bioreactor systems. Asian Institute of Technology: Doctoral thesis; 2007.Google Scholar
- Zhang J, Chen L, Zeng H, Yan X, Yang H, Ye C: Pilot testing of outside-in MF and UF modules used for cooling tower blowdown pretreatment of power plants. Desalination 2007, 214: 287–298. 10.1016/j.desal.2006.12.004View ArticleGoogle Scholar
This article is published under license to BioMed Central Ltd. This is an open access article distributed under the terms of the Creative Commons Attribution License (http://creativecommons.org/licenses/by/2.0), which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.