A Major Problem In Palm Oil Mill Effluent Engineering Essay

A Major Problem In palm inunct Mill Effluent Engineering experimentIn Malaysia, for example, 9.9 moveion tons of solids wastes consisting of empty fruit bunch , fibre and fruit shell and approximately 20 million tons of palm fossil fossil vegetable anoint mill effluent (POME) be gene sayd every year. In response to this, t hither(predicate) has been increasing efforts to manage the wastes generated from mills. A major problem in Palm Oil Mill Effluent is their Biological atomic number 8 Demand (BOD) and Chemical Oxygen Demand ( come up) characteristic in final discharge (waste piss). BOD is a chemical substance procedure for determining how fast biological organisms use up oxygen ( finished degradation of organic material) in a body of pissing. COD is to determine the nub of organic pollutants found in uprise water. The purpose of this study was to minimize the BOD and COD level in waste water finenessment sic using the Sequencing Batch reactor Process (SBR) syste m. The capability of treatment efficiency was proven during the system is widely used in other industry.As Malaysia forges forwardhand with its plan to become a fully developed nation, palm oil mills imparting have to adapt to various tonic challenges, including more strict environmental regulation, labor pifflingage and competition from other lower cost palm oil producing countries. Basically milling engine room has not changed in toll of developing a new sustainable and economics process to extract more oil and kernel. This may sound odd with so m any new mills built and best time to incorporate new technology being to start on a green field.Anyway new technology has developed with concentrated on weaken mechanical handing, higher throughput, and more durable and reliable equipment with longer intervals between failure and renewal.The extraction of palm oil and kernel from the palm fruit is a commonly known in palm oil process. But this extraction process also produces a chocolate-brown effluent which can devastate any aquatic life if dumped directly into our river. It is estimated that for every tone of palm oil produced, 2.5 tons of wastewater is generated. Thus, with Malaysias palm oil production is standing close to 8 million tons per annum , the amount of palm oil mill effluent ( POME ) generated would be equivalent to that of sewerage discharged by a population of 22 million peoplePalm oil mill effluents are high volume lucid wastes which are non toxic but have an unpleasant odor. They are highly polluting. The Biological and Chemical Oxygen Demand (BOD COD)of this effluent is very high and goes for the Total Nitrogen, ammonium hydroxide Nitrogen and Oil Grease. The effluent also acidic. The nature of raw effluent, it is hot, has a bad aroma and brown in color. An effluent with its quality and sum of money were to be discharged into river, all aquatic life will perish.At present there are many manners to treat this raw effluent. The or so common method of treatment being employed is the biological treatment. This method of treatment is by using a combine effect of the aerobic, anaerobiotic and facultative ponds where at the hold back of the case-hardened effluent is dumped into a river.Alternatives treatment methods have propped up in the recent past. In this case, proposed a method which involved Sequencing Batch reactor ( SBR ) engineering with aerated oxygen enriched air. The sequencing batch reactor (SBR) is a batch process for treating wastewater. This process is capable to minimized BOD and COD in a reactor.2.0 writings REVIEW2.1 Typical period ChartsTypical Palm Oil Mill Schematic Flow DiagramAs the palm oil industry grows rapidly, the enactment of palm oil mills also increases significantly especially in Malaysia. Therefore, one of the major problems arises from this industry is the large amount of wastes generated during the processes. for the most part, operation of the palm oil mill generates many by-product and liquid waste which may pose a significant impact on the environment if they are not dealt with congruously. The most common method is biological effluent treatment system (ponds).2.2 Effluent Treatment PlantThe function of the biological effluent treatment plant is to treat the mill liquid waste to levels within the prescribed limits set by the Department of Environment (D.O.E).The method of biological treatment in the mill is the anaerobic process. This process comprises three stagesThe anaerobic digestion in the acidification phaseThe anaerobic digestion in the methanogenic phaseThe inactive facultative stage of aerobic digestion.The complete anaerobic digestion or bio-degradation of the mill effluent is a complex operation as this process requires the acid forming organisms to grow in harmony with the methanogenic formers. Any imbalance of activities of these two organisms would at sea the digestion process.The acid producing bacterium and their associate d enzymes degrade most typeface of organic material into fatty acids. The methanogenic bacteria convert the soluble products of the acid produces into methane and carbon dioxide.The acidification stage is controlled to put up the growth of the acid formers. While in the second stage i.e. the methanogenic phase, the environment is optimum to form the methane formers. The biological effluent treatment plant in the mill comprises of the followingDe-oiling storeful2 Acidification ponds1 primary anaerobic pond2 anaerobic maturation ponds2 facultative pondsDe- sludging facilitiesDe-oiling tank/ gunk reactSludge waste from this mill is pumped into the tank.The purpose of this tank is to trap remnants of free oil and permit solids to calm down out. Solids settled here should be take away on a regular basis in order that working levels be reserveed. Regular checks should be make and any trace of oil here must be postulated.Acidification pondsThere are 2 ponds and these are operate d in parallel. The acidification stage is a very rapid process converting the organic components of the waste water into volatile fatty acids (vfa) and depresses the pH of the system. However recycling of the anaerobic liquor is done here for buffering i.e.Obtaining the desirable pH levelCooling to obtain the craved temperatureSeeding i.e. introducing active organisms populationThe above is practiced at this stage to prepare the feed before entering into the anaerobic ponds.Hydraulic Retention Time (HRT) here in individually pond is 2 daysTemperature 35c 45cPH 4.0 to 5.5Vfa 5000 mg/lPrimary anaerobicIn this stage the strictly anaerobic bacteria called methanogen converts the volatile acids to methane, CO2 and other trace gases. Destruction efficiencies are high here wherein from a high B.O.D. of 24,000mg/l B.O.D. levels of the supernatant at the pond outlet are reduced to 300mg/l.Temperature at Anaerobic 2 outlet is approx. 30-35c with a pH in the neighborhood of 5.5 to 6.5. Vfa=1 000 to 2000 mg/l. Alkalinity = 1500 to 2000 mg/l.Anaerobic Maturation PondThis is a final step of the methanogenic anaerobic stage where further reduction of BOD is made possible. BOD at this stage is down to about 200mg/l . Temperature at the outlet end is 20 to 30c with a pH in the region of 7.0. Vfa is approximately 700mg/l and alkalinity above 1500mg/l.Facultative PondsThe use of anaerobic digestion alone would not be sufficient to meet the standards stipulated by DOE thusly further treatment of effluent is necessary in the facultative. These facultative ponds are for quiescent aerobic respiration of the aerobically interact waste water. These 3 ponds are in series and in these ponds sufficient oxygenation to the waste water is introduced. The effluents after sedimentation in these ponds are allowed to discharge into the water course, with BOD levels below 110 ppm as compulsory by the Dept. of Environment.Temperature at the outlet of the Facultative is 25 to 30c with a pH of 7 .0 9.0. Vfa less than 100. Alkalinity in the region of 1000mg/l.De-sludging of the pondsThe ponding system is operated at low rate with organic loading ranging from 0.2 to 0.35 kg BOD/cu.m/day. Because of the size and configuration of the ponds mixing is hardly adequate. Also the rising biogas will bring along with them fine suspend solids and therefore it is common to find islands of solids floating in the anaerobic pond. This often guides in dead spots which will lead to short circuiting in the ponds. Undoubtedly it is very labor intensive to maintain the ponds in satis calculatey condition at all times. It is also imperative to ensure that as little oil as possible be allowed into the ponds as the oil will agglomerate with the rising solids brought up by the biogas and from a scum which is punishing to remove.Due to the inadequate mixing by biogas, solids build up at the canful of the ponds, especially the anaerobic ones. Excessive solids built up at the bottom of the ponds w ill reduce the effective design capacity and consequently shorten the hydraulic computer storage time. This will adversely affect the treatment efficiency of the system.In view of the above regular desludging of the ponds is a must. A de-sludging pond is made available for this purpose. Solids from the ponds are pumped using submersible pumps into this desludging pond and water liquid re wheel aroundd while solids are left to dry out and subsequently removed.2.3 Operation proceduresSludge pits / Fluming tankSupervisors / operators are to visually check the pit on a regular basis throughout processing and ensure that a trace of oil is recovered soonest possible.Also when spendthrift trace of oil is sighted, agile measures must be taken to trace and arrest the source of this excessive oil loss.Schedule cleaning of the dung pit and tanks must be instituted to remove solids / sands and any debris on a scheduled basis.Pumps in this area must be checked to be in good run condition. A ny faults or malfunction noticed must be reported for immediate repair.Buffering PondsEnsure that recycling of anaerobic liquor is carried out as per instruction. unsay any solids scum / oil traces on a daily basis.Ensure free flow into and out of the ponds.Anaerobic pondsMonitor visually ponds bacteria for any signs of fouling.Solids removal should be carried on a regular basis.Ensure stirrer / mixers are operated as per instructions.Ensure that in flow and outlet discharge is proper and feed to downstream ponds is regulated as involve.Facultative pondsRegulate final discharge as necessary.Ensure solids recycling where necessary.Desludging pondsEnsure that pumping of solids into the pond is monitored.Ensure that excessive liquid is recycled to the anaerobic ponds.3.0 METHODOLOGY3.2 Sequencing Batch reactor (SBR) TechnologySequencing Batch contradictor (SBR) is an activated sludge biological treatment process. The process uses natural bacteria and when the bacteria are aerated, t hey grow and multiply using the organics or pollution as food. This purifies the wastewater before it is discharged to the environment.The process is managed in a suffice and draw, or batch fashion. This process allows for exceptional flexibility and controls which results in a highly tough effluent that will not harm the environment when it is discharged. Generally the SBR process can be conveniently described in five distinct stepsStep 1 Fill/ReactThe treatment Reactor contains bacteria or biomass that processes the wastewater. The cycle starts with the Reactor at least half full of activated sludge. When the wastewater enters the Reactor, air is intermittently supplied by a blower, to maintain an aerobic (air enriched) environment. The pollution in the wastewater is consumed by the biomass as food. The biomass grows and multiplies during this treatment process assuring the system is sustained for further treatment. This cycle of filling and intermittent aeration continues until the Reactor has filled.Step 2 React onlyDuring this step incoming wastewater is diverted to a second Reactor or is stored. The full Reactor is aerated or mixed continuously during this step. The React only step provides time for additional treatment or graduateing of the wastewater to meet require discharged consents. The duration of the react only step is easily adjusted at the computerized control panel.Step 3 SettleThe biomass in the Reactor must be separated from the treated liquid or supernatant, so there will be sufficient biomass remaining for treatment of the next batch of wastewater. In the SBR system the Reactor becomes the settling device or clarifier when all the pumps and blowers are turned off. This creates quiescent settling conditions to allow the biomass and the treated liquid to separate. After settling, the treated clarified liquid is discharged or decanted from the Reactor.Step 4 DecantThe treated clarified liquid is discharged or decanted using pumps which ha ve their recess located at the midpoint of the Reactor depth. This assures that any floating debris or settled biomass is not discharged from the Reactor. A non-return valve on the pump breathing in prevents the entry of solids into the Decant pump and piping during the aerated treatment steps.Step 5 IdleWhen the Reactor has decanted, and there is no wastewater waiting to be pumped to the Reactor enters an idle or waiting phase. In idle, with no wastewater load, it is not necessary to run the blowers at the same rate as during the filling stage. The blowers automatically reduce the volume of air at idle, saving energy. When the Reactor receives more wastewater, it automatically switches back to the Fill/React step, and the entire cycle repeats.Sludge wasteSince the biomass continues to grow or increase in volume during each treatment cycle it is necessary to remove excess biomass from the Reactor on a regular basis. The biomass volume is always maintained below the pump intake and at the proper level by means of automatic sludge waste pumps. The excess biomass is pumped to the Trash Tank at the end head end of the plant where it is anaerobically (without air) decomposed. Regular sludge wasting ensures that fair to middling biomass stiff in the Reactor to treat the next batch of wastewater, but does not increase to the point where it would be pumped out of the reactor during the Decant cycle.3.3 FLOCCULATION intercessionRaw effluent from facultative pond (last pond) is pump into vertical steel clarifier. Flocculation agent and pH correction agent is dose into the pipe line before entering clarifier to ease coagulation process.PRE AERATIONThe clarified raw effluent will over flow into the 1st holding tank. Filling is estimated for 3 hours.While in the holding tank, the raw effluent is subjected to pre aeration for 2 hours before transfer to the reactor tank.Pre-aeration is done through fine air bubbles passes through an array of disc type diffuse at tank base.SBR PROCESSThe pre-aeration effluent from holding tank is transferred into the reactor tank via transfer pump.The SBR process inside the reactor tank will be control through a present time for 24 hours operation based on the following activityFilling 3 hours soft aeration 4 hoursFast aeration 10 hoursSettling 2 hoursDischarge 2 hoursFillingPre-aerated anaerobic liquid is pump from holding tank. During start up, seeding of bacteria is carried out. The quantity from of seeding is depending on the MLSS concentration in the reactor.Slow aerationWhile filling up of the pre-aerated anaerobic liquid half of the diffuser inside the reactor tank will activate, via control valve install at the distribution header.Fast aerationFilling completed and full aeration processes activate.SettlingTo allow solids and liquids are separated under true quiescent conditions.DischargeThe treated or clarified supernatant is pump into a final treated effluent tank for storage. The excess sludge wil l settle and remain in the reactor tank. Desludging will depend on the MLSS concentration, not to exceed 20-30 % by ratio of the pre-aerated anaerobic liquid. This can be done by taking sample and allow to settle naturally.StandbyThe reactor tank is ready for the next batch.The treated water will overflow through a constant level flexible outlet into a transfer (clarified) water tank. The clarified water enters an activated carbon leach via booster pump, which act to polish the water before discharge out to river. At this stage the BOD level should be 20 ppm. A reject line is installed to return treated effluent into anaerobic pond if the BOD level exceeds 20 ppm.3.4 NOPOL- diffuserThe NOPOL system has a suitable diffuser for any wastewater application.Reliable kinkThe main component of the system is the NOPOL dual layer polyethylene disc. This has a thin fine top for maximum oxygen transfer efficiency. All deposits are easily removed by the formic acid.The NOPOL disc aeration sy stem is ideal for all biological processes. An aeration system covering the entire bottom of the basin gives the want oxygen content throughout. Mixing energy is evenly distributed throughout the basin. Uniform mixing prevents any sludge sedimentation. Adjustment range-volume of air per diffuser is wide enough for any load variation. The disc aeration system does not cool down the activated sludge or produce any harmful aerosols.3.5 SBR system tank and pipe layout4.0 ANALYSIS4.1 A BASIC DESIGN OF SBR SYSTEM energy 1080 m / dayInfluent BOD 200 ppmDischarge BOD 20 ppmBasic design dataActual waste water quantity discharged from plant 1080 m / day ( max )Design waste water quantity 1080 m / day or 45 m / hourBOD 200 mg / lCOD (assume) 300 mg / lPH 7.2Temperature 26 cSuspended solids (assume) 300 mg / lOil grease (assume) 20 mg / lSequence of operation of SBR reactor tank No.1 or 2Filling and slow aeration time 8 hoursFast aeration time 12 hoursSettling time 2 hoursDischarg e of treated effluent 2 hoursSizing of tanksBased on the above operation sequence and the two trains of SBR tank operating alternatively, the sizes of the holding tank and reactor tanks are as followsHolding tankTank required 1 building blockWaste water flow rate 45 m / hourThe retention time for the holding tank 6 hoursVolume of tank required 270 mSelected holding tank size is 8700 m - 7.62 m heightCapacity 400 mReactor tanksWastewater flow rate 45 m / hourNo of tanks required 2 unitsRetention required for reactor vessel 12 hourVolume of waste water in each reactor tank 540 mVolume of activated sludge to be retained in reactor tank 20 % of the waste waterTherefore required volume of reactor tank 648 mSelected reactor tank size is 11650 mm - 7.62 m heightCapacity 800 mCalculation of air required for aeration at reactor tankProcess utilized Palm Oil Mill EffluentType of waste IndustrialDesign flow 1080 m / dayBOD5 design 200 mg / l = 216 kg / dayTemperature of wa ste 26 cDissolved oxygen to be maintained in waste water ( C ) 2.0 mg / lOxygen to BOD5 ratio 1.5 (assume)Oxygen required per hour (216 - 1.5) / 12 = 27 kg / hourOxygenation capacity required per hour = 02 required per hour / correction factorCorrection factor = () (C) C 1.024 (-20)/ CH20C H20 oxygen solubility factor = 0.9 = 0.95C at 26c at 200 ft elevation = 8.11.024 (-20) at 26c = 1.153C = 2 ppmTherefore, oxygenation capacity required per hour = 27 / 0.7289= 37.04 kg / hourDensity of air at 26c = 1.18 kg / m Volume of air required taking oxygen content in air is 20% by unit weight = (37.04-5m/hr)/1.18= 157 m / hourEfficiency of aeration by using Nopol diffuser at 4m water dept = 18 % at 4m / hr per unitFlow rate of air blower required = 157 m / hr / 18 % = 872 m / hrUse air blower = 900 m / hrNo. of diffuser required = 900 / 4 = 225 pcsTherefore,No. of diffuser installed per reactor = 225 (for 1080 m/day) operating at 12 hoursDetermination of number of diffusers per tank fo r holding tankThe required aeration for waste water in holding tank is to ensure fecundation concentration of oxygen dissolved in water.Based on temperature of 26c, the saturation concentration of oxygen in water is = 8.11 mg/lWith influent flow rate = 45 m / hourTotal oxygen required = 364.9 g / hourAllow 20% extra air to ensure saturation, the actual aeration rate = 438 g / hourNo. of diffusers at 1 m / hour per unit at 18 % = 11 nos.No. of diffusers installed at holding tank for primary aeration and mixingto saturation point = 30 nos. (At 0.4 pc/m distribution density)Total diffuser used for 2 trains system = 510 nos.Selection of two ( 2 ) units of surface aeratorModel = EEE FA- 1010Specifications are enclosed.The application of these surface aerations installed at facultative pond is forProper mixing of the effluent before pumping to the effluent treatment plantTo supply some aeration to the facultative pond so as to minimize the inlet BOD to the effluent plant and at the same time to improve the bacteria activity.Selection of one ( 1 ) unit activated carbon filter at treated effluent discharge pointDimension = 2420 mm - 1828 mm SLSurface area = 4.59 mFlow rate = 60 m / hourFlow velocity = 13.0 m / hourVolume of activated carbon = 4.1 mThe activated carbon filter acts as a polishing filter for the final treated effluent.5.0 DISCUSSION AND CONCLUSIONA more responsible biological treatment process through a proven automated operation program responding on time every situation and alarm in a reactive way so that the plant performance can be maintained regardless of the operator attendance and equipment failure.Lower investment and recurrent cost, as secondary settling tanks and sludge return systems are not required.Lower space requirements.Better settling, as settling conditions in an SBR areIdeal while the sludge population changes towardsbetter settle able micro-organisms.Improved effluent quality.Improved operational reliability.Hardly any or no smell p roblems.Better temperature control.Lower effluent COD and BOD. The batch nature process and high organic concentrations (feast)during Fill encourages the growth of organisms with high organic uptake rates. The famine period at the end of React encourages the utilization of recalcitrant organics. The combined effect of the feast and famine periods is the optimal removal of BOD and COD.Better settling sludge. The feast-famine conditions that naturally occur in each cycle promote the growth of floc-forming organisms and disfavor filamentous organisms, thereby eliminating the use up for polymers.In a number of situations the application of an SBR system will thus result in lower investment as well as operational costs. Critical in this respect are the load and concentration of the wastewater, the design and the local anesthetic situation.6.0 SUGGESTION FOR FURTHER WORKAt this study, Sequencing Batch Reactor process, raw effluent from facultative pond (last pond) is pump into clarifier in system. Thereby, the pond still need for this system due to oil recovery in first 2 ponds. In future study, the pond system which consumed a large area need to remove. The wastewater from the mills, directly pump to SBR system tanks for further treatment. The new method for oil recovery in SBR system will be taken in action. The discharge water which in brownish color need to be analyze due to remove the color.