ORIGINAL ARTICLES

 

The use of exogenous microbial species to enhance the performance of a hybrid fixed-film bioreactor treating coal gasification wastewater to meet discharge requirements

 

 

E Rava^{I, *}; E Chirwa^I; P Allison^II; M van Niekerk^III; MP Augustyn^III

^IUniversity of Pretoria, Water Utilisation Division, 0002, South Africa,
^IIScientific and Technical Consulting Services, P.O. Box 699, Port Alfred 6170, South Africa
^IIISasol Group Technology (Pty) Ltd, Private Bag X1034, IB4901, Secunda 2302, South Africa

 

 

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ABSTRACT

The objective of this study was to determine whether inoculating a hybrid fixed-film bioreactor with exogenous bacterial and diatoma species would increase the removal of chemical oxygen demand, nitrogenous compounds and suspended solids from a real-time coal gasification wastewater to meet environmental discharge requirements specified for petrochemical refineries. The COD removal increased by 25% (45% to 70%) at a relatively high inoculum dosage (370 gm^-3) and unit treatment cost (12.21 €-m^-3). The molar ratio of monovalent cations to divalent cations (M/D >2) affected nitrification, settling of solids and dewatering of the sludge. The use of a low-charge cationic flocculant decreased the suspended solids in the effluent by 70% (180 mg-L^-1 to 54 mg-L^-1) and increased the sludge dewatering rate by 88% (61 s-L-g^-1 to 154 s-L-g^-1) at a unit treatment cost of 2.5 €-t^-1 dry solids. Organic compounds not removed by the indigenous and exogenous microbial species included benzoic acids (aromatic carboxylic acids), 2-butenoic acid (short-chain unsaturated carboxylic acid), I(2H)-isoquinolinone (heterocyclic amine), hydantoins (highly polar heterocyclic compounds), long-chain hydrocarbon length (carbon length > C₁₅) and squalene. These organic compounds can thus be classified as poorly degradable or nonbiodegradable which contributed to the 30% COD not removed by the H-FFBR. The use of exogenous microbial species improved the quality of CGWW; however, not sufficiently to meet discharge requirements. The cost of such treatment to meet discharge requirements would be unsustainable. Alternative technologies need to be investigated for reusing or recycling the CGWW rather than discharging.

Keywords: ammonia, catalytic reactor technology, COD, fixed-film bioreactor, hydantoins, thiocyanates

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INTRODUCTION

Integrated refineries, such as those using the Lurgi coal gasification process, generate large volumes of wastewater with high concentrations of hazardous contaminants. The composition of coal gasification wastewaters (CGWW) and coking wastewater are similar with respect to the organic and inorganic constituents. However, the effluent from CGWW is more complex and contains more toxic recalcitrant hydrocarbons than coking wastewater (Li et al., 2011). Regulations regarding the discharge of wastewater from petrochemical processing facilities, of which coal gasification systems are a part, are becoming stricter, and therefore more efficient wastewater treatment systems are required before releasing the effluent into the environment (Rubalcaba et al., 2007).

The contaminants present in CGWW include phenols, cyanide, thiocyanates, polycyclic aromatic hydrocarbons, nitrogen-, oxygen- and sulphur-containing heterocyclic compounds, long-chain hydrocarbons, pyridine, and quinolone (Li et al., 2014). Most of these refractory organic compounds have been reported to be mutagenic and teratogenic in living organisms (Wang et al., 2012). To treat and recycle the CGWW will reduce the demand on water resources and also prevent environmental pollution (Li et al., 2014).

A number of biological treatments have been developed for treating CGWW including activated sludge (CAS), such as biological nitrogen removal (BNR) systems and sequencing batch reactors (SBRs), and fixed-film processes such as fluid-ised-bed reactors (FBRs) and membrane bioreactors (MBRs). Unfortunately, the conventional biological systems rely on mesophilic bacteria sourced from soil and wastewater, and which are not resistant to high levels of toxicity and lack pathways to break down the complex aromatic compounds found in CGWW Moreover, bacteria from municipal treatment plants do not perform well under low chemical oxygen demand (COD) levels (below 125 mg-L^-1) and ammonia-nitrogen (below 15 mg-L^-1), despite high removal efficiencies of biological oxygen demand (BOD₅), phenols and cyanide (Zhou et al., 2014). Therefore, the H-FFBR together with the inoculation of exogenous microorganisms was investigated for the removal of COD, nitrogen-containing compounds, phenols and other organic compounds.

Bio-augmentation has been reported as being a feasible option to enhance the biological treatment of high strength CGWW (Bai et al., 2010) with the following advantages: higher reactor biomass, strong capacity to handle shock loadings, lower excess sludge production and increasing microbial population diversity in the bioreactor (Tavares dos Pasos et al., 2010). Biological treatment is viewed as a cleaner technology since chemicals are not used, it has a smaller carbon footprint, smaller water footprint, fewer emissions and a disposable sludge is generated (Ishak et al., 2012).

Bio-augmentation is the addition of a different gene pool with metabolic properties that complement the existing one to increase the degradation of organic compounds (Domde et al., 2007). The bacteria carry plasmid-encoded catabolic genes that increase the degradation potential of the indigenous population via horizontal gene-transfer, enabling direct inheritance by future generations without reproduction (OECD, 2010). The three main mechanisms of gene transfer are: (i) transformation - gene transfer resulting from the uptake of free extracellular DNA from the environment; (ii) conjugation - genetic material is transferred from one bacteria to another by cell-to-cell contact, which is significant for bacteria found in biofilms and bio-aggregates such as activated sludge; and (iii) transduction - transfer of genetic material between bacteria mediated by bacteriophages (Wasilkowski et al., 2012). Horizontal gene transfer can range between 0% and 14% and peaks on the third day. A higher concentration of inoculum does not increase gene transfer rate; however, a higher concentration of activated sludge cells is associated with an increase in gene transfer rate. A 20:1 (activated sludge: Pseudomonas putida) ratio was associated with the highest number of gene transfers (Pei and Gunsch, 2009).

Bio-augmentation using naturally adapted bacteria does not introduce other species into the environment since horizontal gene transfer is a common process and major driving force of bacterial adaptability and diversity in wastewater (OECD, 2010).

The objective of this study was to determine the cost and sus-tainability of inoculating a pilot H-FFBR with exogenous bacterial and diatoma species to increase the removal of COD, organic compounds, suspended solids and nitrogenous compounds from CGWW to meet environmental discharge requirements specified for petrochemical refineries.

This study differs from other bio-augmentation publications in that the pilot plant was fed continuously with real-time CGWW for a period of 18 months and the performance of the bioreactor was related to the actual financial cost of bio-augmentation. Most reported studies have been based on batch processes using synthetic CGWW under ideal laboratory conditions which does not reflect fluctuating conditions in an operational plant.

 

MATERIALS and METHODS

Pilot plant design

The stainless steel pilot plant H-FFBR (1 000 L) consisted of 3 aeration compartments, designated as Zone 1, Zone 2 and Zone 3, containing acclimatised fixed and suspended biomass, and a clarifier. The volume of each zone was approximately 250 L, 150 L and 600 L for Zone 1, Zone 2 and Zone 3, respectively (Fig. 1).

The AnoxKaldnes K1 plastic biofilm carrier filling fraction (based on volume) for the aeration zones was approximately 70% for Zone 1, 50% for Zone 2 and 30% for Zone 3. A 70% filling of biofilm carrier media corresponded to an effective biofilm growth area equal to 350 m²-m^-3, with 50% fill equal to 250 m²-m^-3 and a 30% fill equal to 150 m²-m^-3 (Ratcliffe et al., 2006; Ayun et al., 2008). Each aeration zone was linked to a data collection system (DCS) and parameters such as temperature, dissolved oxygen (DO), recycling rate, feed rate, desludging rate, hydraulic retention time, pH and sludge retention time were controlled and optimised automatically.

Reactor operation

The CGWW was diluted to 33% to reduce the toxicity towards the biomass and to maintain an influent COD around 2 000 mg-L^-1. Dilution was 1 part CGWW to 2 parts recycled activated sludge (RAS) and fed to Zone 1 of the H-FFBR. The reactor was operated at 36±1°C and monitored over a period of 64 weeks. The pH was adjusted with 20% (m/v) sulphuric acid (H₂SO₄) or 10% (m/v) sodium hydroxide (NaOH) to maintain a pH of 8.0±0.5. Food to mass ratio (kg-COD-m^-3-d^-1) was maintained at < 0.45 of the biodegradable COD fraction, sludge retention time (SRT) was about 18 d and the hydraulic retention time (HRT) was 33 h. Dissolved oxygen (DO) level was maintained between 5 mg-L^-1 and 6 mg-L^-1.

Sampling procedures

Composite samples (1 000 mL) of the influent stream (feed) and effluent stream (clarifier overflow) were collected daily and tested for pH, calcium, magnesium, soluble COD (filtered through a 0.45 μm membrane filter) and total COD, suspended solids, ammonium-nitrogen and nitrate-nitrogen, suspended solids, and capillary suction tests (CST). Grab samples (1 000 mL) of the feed and effluent were taken monthly, extracted with dichlo-romethane and the extractions analysed ('finger-printed') by gas chromatography- mass spectroscopy (GC/MS).

Preparation of exogenous inoculum

The selectively adapted exogenous inocula, sourced from Buckman Africa, were mobilised by hydrating the respective inocula (20% w/v) using chlorine-free tap water and stirring using an over-head stirrer for 60 min at 80 r-min^-1. Hydration was required to resuscitate the freeze-dried cultures. The hydrated inocula were then filtered through a 100 μm mesh to remove the carrier. For the purpose of this study, the exogenous inocula, i.e., XP16-014, XP16-015, XP16-016 and XP16-017 were labelled as PA1, PA2, PA3 and PA4, respectively.

Oxygen uptake rate of bio-augmented samples

The oxygen uptake rate (OUR) of laboratory-inoculated bioreactor samples (20 mg-L^-1 to 250 mg-L^-1) were measured on-site at 36±1°C using a calibrated HACH model HQ40d multi-meter with a LDO 101 dissolved oxygen probe. A biochemical oxygen demand (BOD) sample bottle (300 mL) was filled with 150 mL feed, bio-augmented with the respective hydrated products, and then filled up with 150 mL carrier media taken from the respective zones to simulate a 50% media fill fraction (by volume). The dissolved oxygen (DO) was measured every 60 s for a period of 10 min. The OURs of the exogenous microbial species were calculated by linear regression obtained from the plot of DO concentration versus time. The choice of inocula for the pilot plant study was based on the OUR increase versus the unit treatment cost. The exogenous inocula selected were thus 50 mg-L^-1for PA1, 150 mg-L^-1 for PA2, 150 mg-L^-1 for PA3 and 20 mg-L^-1for PA4.

Characterisation of the inoculum

Hydrated mobilised micro-organisms were plated out for enumeration using Plate Count Agar (Oxoid CM0325) for hetero-trophic plate counts (HPC) and Bacillus spp. Pseudomonas agar (Oxoid CM0579) supplemented with selective CFC supplement (SR0103) and selective CN supplement (Oxoid SR0102) was used for the enumeration of Pseudomonas species. Aeromonas medium base (Oxoid CM0833) supplemented with ampicillin (Oxoid SR0136) was used for the enumeration ofAeromonas species. All the agar plates were incubated at 35°C for 48 h.

Colony identifications and enumerations

All colonies present on the respective agars were identified using the bioMêrieux VITEK MS automated microbial identification system that uses the Matrix Assisted Laser Desorption Ionization Time-of-Flight (MALDI-TOF) mass spectrometry technology. The sample is applied to a target slide and irradiated with a laser. The unique protein spectrum of the micro-organism is used for identification. The diatoma were identified using a standard microscope at 400x magnification and confirmed using an inverted microscope at 600x magnification.

Colony forming units (cfu) were multiplied by the respective dilution factors and converted from cfu -mL^-1 to cfu-g^-1. Diatoma counts were multiplied by the dilution factor and reported as cells-g^-1.

Inoculation of the bioreactor

The respective hydrated inocula were added daily directly into aeration Zone 1 of the H-FFBR. Each inoculation step was allowed to run for a period of 12 weeks to allow sufficient time (2 weeks to 3 weeks) for the exogenous micro-organisms to acclimatise to the CGWW and achieve maximum growth rate and biological activity. The reactor was subjected to 3 sludge ages (Stamoudis and Luthy, 1980).

Flocculation and settling of the suspended solids in the clarifier

Cationic flocculants, Sourced from Buckman Africa, were prepared as 0.1% (m/v) aqueous solutions and allowed to hydrate for 30 min before dosing. The flocculants were then dosed between 1 kg-t^-1 and 3 kg-t^-1 dry solids into 500 mL sample aliquots taken from the clarifier. Flocculation tests were performed using a Velp jar stirrer. The sample aliquots were flash mixed for 3 min at 230 r-min^-1, the flocculants were dosed followed by another 10 s of flash mixing. The jar stirrer speed was then reduced to 80 r-min^-1 and mixing continued for another 7 min. The jar stirrer was switched off and the sludge was allowed to settle for 10 min. The suspended solids of the respective supernatants were then determined gravimetrically. Performance of the flocculants was based on the lowest amount of suspended solids in the respective supernatants. For the purpose of this study, the flocculants evaluated, i.e., XP13-025, XP13-026, XP13-027, XP13-5511 and XP13-5182P were labelled as C1, C2, C3 and C4, respectively.

Analytical methods

The suspended solids (SS) were analysed gravimetrically by filtering 100 mL aliquots through Whatman GF/C filter paper under vacuum, capillary suction tests (CST) were performed using a Triton 304 CST unit (Triton Electronics Ltd, England), and pH was measured using the Hach model HQ40d multi-meter and a calibrated Hach PHC101 gel-filled pH probe. The metal ions were determined by inductively-coupled plasma/optical emission spectrometry (ICP-OES) using an Agilent (Agilent Technologies, USA). COD, ammonia-nitrogen and nitrate-nitrogen were determined using a calibrated Hach DR 890 colorimeter and validated Hach methods 8000, 8155 and 8192, respectively. Phenols and biological oxygen demand (BOD₅) were analysed using Standard Methods (APHA, 2012).

Gas chromatography-mass spectroscopy (GC/MS) analyses

The dichloromethane liquid-liquid extractives of the feed and effluent were characterised using an Agilent 7890A gas Chromatograph (Agilent Technologies, USA) equipped with an Agilent 5975C inert mass selective detector (MSD) (Agilent Technologies, USA). A DB-5MS capillary column was used (30 m x 0.3 mm ID x 0.25 μm) with split injection mode (10:1). Helium (1.1 mL-min^-1) was used as the carrier gas and the GC oven was programmed at a temperature gradient of 40°C to 300°C over a period of 35 min. The electron ionisation (EI) spectra of the compounds were identified by searching the National Institute of Standards and Technology (NIST05) mass spectral library.

Laboratory scale nickel-catalyst reactor parameters

The nickel catalyst was activated using sodium hypochlorite for a period of 24 h before treating the CGWW. The pH of the CGWW was maintained at 9.5 to prevent leaching of the metal from the catalyst and the temperature was maintained at 50°C to increase the oxidation reaction rate. The operational parameters for the reactor are indicated in Table 1. The CGWW was sampled before and after treatment and analysed for phenol, COD, BOD₅ and ammonia-nitrogen.

 

 

All equipment and instrumentation used during the pilot plant study were calibrated according to the manufacturer's instructions and the test methods were validated according to the ISO/IEC 17025:2005 technical requirements.

 

RESULTS and DISCUSSION

Identification and quantification of the exogenous inoculum

The respective hydrated inocula were plated out to identify and quantify the culturable micro-organisms used for enhancing the performance of the H-FFBR treating the CGWW. The heterotrophic plate count (HPC) ranged between 1.3 x 10⁶ and 3.0 x 10⁹ cfu-g^-1, Pseudomonas spp. ranged between 8.0 x 10⁴ and 4.0 x 10⁹ cfu-g^-1 and Bacillus spp. ranged between 4.0 x 10⁶ and 1.9 x 10⁹ cfu-g^-1. The diatoma cell count was 5.4 x 10⁴ cells-g^-1(Table 2).

 

 

The bacterial species in inoculum PA1 were identified as Bacillus pumilus, Bacillus amyloliquifaciens, Bacillus subtilis, Rhodococcus spp, Pseudomonas spp and Pseudomonas putida. The bacterial species in inoculum PA2 were identified as Bacillus amyloliquifaciens, Bacillus subtilis and Pseudomonas putida. The main bacterial species in inoculum PA3 were identified as Pseudomonas putida. There were other pseudomonads present which were not identified. The diatoma in inoculum PA4 were identified as Cocconeis spp and Nitzschia spp. PA4 was included in the study since diatoma can facilitate spontaneous flocculation of bacteria to improve the quality of the effluent and prevent cells from being washed out of the bioreactor (Farooqi et al., 2008).

The indigenous population in the H-FFBR consisted mainly of Pseudomonas stutzeri, Aeromonas hydrophila and Bacillus cereus.

Microbial degradation of organic compounds

Most phenol-degrading bacteria can degrade other aromatic compounds; however, there are differences between the strains with respect to the kind of aromatic compounds biodegraded (Ambujom, 2001). The critical step in biodegradation is the cleavage of the aromatic ring. The initial catabolic step involves the insertion of two hydroxyl groups on the aromatic nucleus. Ring fission proceeds via the meta or the ortho pathway of the hydroxylated aromatic compound (Mulcahy, 1993). The meta pathway is plasmid encoded and the ortho pathway is chromo-somally encoded (Ambujom, 2001). The bacterial consortium that degrades via the ortho pathways has a slower rate of degradation compared to the meta-cleaving bacterial consortium (Ambujom, 2001).

Rhodococcus, Pseudomonas and Burkholderia degrade C₅-C₁₆ alkanes, fatty acids, alkyl benzenes and cycloalkanes (Das and Chandran, 2011). Rhodococcus and Pseudomonas can utilise phenols, aliphatic and aromatic hydrocarbons as carbon sources and are the most active bacteria in coal gasification wastewater (Meng et al., 2015). Pseudomonas and Burkholderia produce the required enzymes to access hydantoins and hydantoin-like molecules as metabolic substrates (Dürr et al., 2006). Pseudomonas has also been reported to biodegrade aromatics such as pyro-catechol, alpha-naphthol, hydroquinone, naphthalene, iso-quinoline, indole and sulfonated aromatic compounds (Nawawi et al., 2014). Pseudomonas aeruginosa and Pseudomonas stutzeri degrade phenol (Arunkumar and Anitha, 2014) and several Pseudomonas species have been isolated and identified as cyanide-degrading bacteria which utilise cyanide as a source of carbon and nitrogen. Cyanide metabolising bacteria include Bacillus species such as Bacillus megaterium, Bacillus pumilus, Bacillus stearothermophilus and Bacillus cereus. (Perumal et al., 2013). Pseudomonas and Bacillus spp. are capable of heterotrophic nitrification (Lin et al., 2006). Pseudomonas and Aeromonas produce enzymes such as protease and lipases which assist with the reduction of waste activated sludge (Yasin et al., 2014) and have been reported to be tolerant towards heavy metals found in CGWW (Kasan and Baecker,1989).

Reactor performance in removing soluble COD and suspended solids

The co-inoculation sequence was based on the potential removal of COD as follows:

• Week 1 to 12: PA1 (50 mg-L^-1) and PA4 (20 mg-L^-1)

• Week 12 to 24: PA1 (50 mg-L^-1), PA2 (150 mg-L^-1) and PA4 (20 mg-L^-1)

• Week 24 to 36: PA1 (50 mg-L^-1), PA2 (150 mg-L^-1) PA3 (150 mg-L^-1) and PA4 (20 mg-L^-1)

The weekly average COD and SS data for the pre-treatment, exogenous inoculations and post-treatment phase is presented in Fig. 2 and Table 3, respectively. The cost per treatment programme was calculated on an average purchasing price of 33 €-kg^-1 dry inoculum.

The average soluble COD of the feed was relatively constant throughout the pilot plant study (Table 2). The inoculation with PA1 and PA4 increased the removal of soluble COD by 4% (45% to 49%) which was not significant (p > 0.05) when compared to the baseline data. The addition of PA2 to the inoculum increased the removal of soluble COD by 12% (49% to 61%) which was significant (p < 0.05) when compared to the baseline data and the inoculation without PA2. The addition of PA3 to the inoculum increased the removal of soluble COD by a further 9% (61% to 70%) which was significant (p < 0.05) when compared to the baseline data and inoculation without PA3. A 25% improvement in the removal of soluble COD was achieved at a cost of 12.21 €-m^-3. The removal of soluble COD started to decrease about 2 weeks after the last inoculation (Fig. 2), suggesting that the gene transfer of catabolic plasmids between the bacterial populations was dependant on the survival of donor plasmids which had a limited long-term impact. The cost of the bio-augmentation programme could potentially be reduced from 12.21 €-m^-3to 1.74 €-m^-3 by inoculating the bioreactor weekly rather than daily.

The increase in COD removal indicated that more compounds were available for degradation. Even though a 70% removal in COD was achieved, the effluent did not meet the Minimal National Standards (MINAS) for discharge (125 mg-L^-1), nor the global effluent standards for refineries, i.e., World Bank (150 mg-L^-1), USA (30 mg-L^-1), European Union (30 mg-L^-1 to 225 mg-L^-1) and Nigeria (40 mg-L^-1) (Mazema et al., 2008).

Inoculation of the bioreactor increased the dispersed biomass which settled very slowly and consequently was washed out from the system resulting in increased SS in the clarifier overflow (Table 3). Therefore, daily inoculation was required to replenish the washed-out biomass. The inoculation with the diatoma containing inoculum, PA4, did not improve the settling rate of the biomass as anticipated. Thus, the SS of the effluent did not meet the MINAS limit (20 mg-L^-1), nor the global effluent standards for refineries, i.e., World Bank (30 mg-L^-1), USA (30 mg-L^-1), European Union (2 mg-L^-1 to 80 mg-L^-1) (Mazema et al., 2008).

Effect of flocculants on sludge settling and dewatering properties

Cationic flocculants (Table 4) with different cationicities and molecular weights were tested between 1 kg-t^-1 and 3 kg-t^-1 dry solids to improve the biomass (activated sludge) settling rate and dewatering properties. Cationic flocculants were selected since sludge flocs have a negative charge due to the ionisation of the anionic functional groups and are not likely to aggregate naturally due to repulsive electrostatic forces and hydration interactions between them (Liu and Tay, 2004).

 

 

Flocculant C1, dosed at 2 kg-t^-1 dry sludge solids, reduced the suspended solids by 70% (180 to 54 mg-L^-1) which will reduce the total COD of the effluent due to less carry-over of colloidal and suspended solids. The dewatering properties of the sludge were measured using a capillary suction tester (CST). The specific CST (SCST) [(CST (s)/solids (g-L^-1)] increased from 61 s-L-g^-1 to 154 s-L-g^-1 thus indicating a significant improvement (p < 0.05) in the sludge dewatering rate due to improved floc structure. The unit treatment cost was calculated to be 2.5 €-t^-1 of dry sludge solids.

Removal of nitrogenous compounds

No nitrification took place in the H-FFBR since there was no difference between the average influent nitrate-nitrogen (NO₃-N) (5.7 mg-L^-1) and the average effluent NO₃-N (5.7 mg-L^-1). No increase in nitrate also indicated that hydantoins were not removed (Turner and Wernberg, 1985). The 14.5% difference between the average influent ammonium-nitrogen (NH₄-N) (415 mg-L^-1) and the average effluent NH₄-N (355 mg-L^-1) was most probably due to evaporative stripping rather than nitrification having taken place. The average concentration of cations was 89 mg-L^-1 for sodium (Na+); 4.5 mg-L^-1 for calcium (Ca²+) and 2.2 mg-L^-1 for magnesium (Mg²). The molar ratio of monovalent- to-divalent cations was higher than 2 (M/D > 2) thus inhibiting nitrification and the removal of cyanides, thio-cyanates, aromatic amines and ammonia which form part of the soluble COD (Sharma and Philip, 2014). The carbon:nitrogen ratio (C/N) was greater than 1.5 thus heterotrophs dominated the microbial population inhibiting the growth of autotrophic nitrifiers. Compounds having a similar structure to ammonia can interfere with the active site of ammonia mono-oxygenase and metal-binding compounds can reduce the availability of copper thus inactivating the enzymes involved in the nitrification process (Michaud et al., 2006).

Removal of organic compounds

Gas chromatography-mass spectroscopy (GC/MS) of the feed and effluent indicated the presence of 2-methylcyclopentanone, 3-methylcyclopentanone, aniline, o-phenol, 5-quinolinol, 1-methyl-2-acetylindole, I(2H)-isoquinolinone, butenoic acid, hexanoic acid, heptanoic acid, octanoic acid, n-hexadecanoic acid, 2-methylbenzoic acid, 3-methylbenzoic acid, 4-meth-ylbenzoic acid, 2,5-dimethylbenzoic acid, 4-ethylbenzoic acid 3,4-dimethylbenzoic acid, 3,5-dimethylbenzoic acid, 4-(1-meth-ylethyl)benzoic acid, 5,5-dimethylhydantoin (DMH), 5-ethyl-5-methylhydantoin (EMH) and squalene.

The indigenous and exogenous microbial species were effective in biodegrading/oxidising the compounds such as saturated carboxylic acids (C₄ to C₁₆), aniline (cyclic amine), 5-quinolinol (benzopyridine), 1-methyl-2-acetylindole (heterocyclic ketone), o-phenols. However, they were not effective in biodegrading the benzoic acids (aromatic carboxylic acids), trans-2-butenoic acid (short-chain unsaturated carboxylic acid), I(2H)-isoquinolinone (heterocyclic amine), hydantoins (highly polar heterocyclic compounds), long-chain hydrocarbon (carbon length > C₁₅) and squalene. These compounds can be classified as poorly or non-biodegradable and are thus contributing to the remaining 30% COD. Unidentified organic compounds, inorganic compounds and nitrogenous compounds such as ammonia, thiocyanate, and cyanide will also contribute to the soluble COD.

Qualitative analyses of the feed indicated that total phenols ranged between 100 mg-L^-1 and 150 mg-L^-1, carboxylic acids between 150 mg-L^-1 and 250 mg-L^-1, hydantoins between 200 mg-L^-1 and 250 mg-L^-1, oil and grease (dichloromethane extraction) between 10 mg-L^-1and 30 mg-L^-1, nitrogen- and sulphur-containing organics between 20 mg-L^-1 and 30 mg-L^-1. Qualitative analyses of the effluent indicated that total phenols ranged between 0.35 mg-L^-1 and 5.0 mg-L^-1, carboxylic acids < 20 mg-L^-1, and nitrogen- and sulphur-containing compounds between 20 mg-L^-1 and 30 mg-L^-1.

Combination of technologies to meet discharge requirements

Preliminary laboratory results using a laboratory-scale fixed-bed metal-oxide catalyst reactor (Table 1) showed a significant removal (p < 0.05) of phenols (150 mg-L^-1 to < 10 mg-L^-1), COD (1 710 mg-L^-1 to < 10 mg-L^-1), BOD₅ (78 mg-L^-1 to < 10 mg-L^-1) and ammonium-nitrogen (450 mg-L^-1 to < 10 mg-L^-1). The unit treatment cost (excluding operational costs) for the high-quality effluent was calculated to be approximately 25 €-m^-3 of effluent The choice of technology, or combination of technologies, will largely depend on the cost to achieve the quality of effluent required to meet discharge requirements and the respective penalties imposed for not meeting the discharge requirements.

 

CONCLUSIONS

The study showed that the exogenous bacteria enhanced the removal of COD; however, the performance of the H-FFBR was dependent on the survival of the donor plasmids (exogenous inoculum) which had a limited long-term impact. Bioaugmentation did not improve the quality of the CGWW sufficiently to meet the discharge requirements in terms of COD, ammonia-nitrogen and suspended solids. Bio-augmentation can be used as a pre-treatment step; however, the treatment cost would not be financially sustainable due to the large volumes of CGWW generated by refineries. Alternative more cost-effective chemical and physical technologies should be investigated for treating the CGWW.

 

ACKNOWLEDGEMENTS

The authors would like to thank Buckman Africa for financing the chemical and microbiological analyses and Sasol Group Technology (Pty) Ltd for the use and operation of the pilot plant.

 

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Received 9 June 2015
Accepted in revised form 27 June 2016

 

 

* To whom all correspondence should be addressed. s +27 833978524 / e-mail: emrava@buckman.com