Pilot Scale Test to Treat High Concentration Gasification Wastewater Using Catalytic Oxidation and A

140Jourmal of Donghue University (Eng. Ed.) Vol. 25, No.2 (2008)Pilot Scale Test to Treat High Concentration Gasification Wastewater UsingCatalytic Oxidation and Aerobic Biological Fluid-Bed Combination ProcessLINa (李娜)-2;, HUANG Jun-li (黄君礼)", WANG Wei (王威)1 ,ZHAO Jjian-wei (赵建伟)' ,WANGGui-lin (王桂林)3 ,CUI Chong-wei (崔崇威)'School of Municipal and Enrirommental Engineering，Harbin Instinue of Technology, Harbin 150090, China2 Department of Environmental Science and Engineering , Northeastemn University at Qinhuangdao, Hebei, Qinhuangdao 066004 , China3 Chongqing Accelerant Chemistry Company, Chongqing 400042, ChinaAbstract: The gasification wastewatar is a kind of typicaloxygen and sulfur and so on. Many of these compounds, suchonganic industrial wastewater with high chemical axyenas pyridine, furan, carbeazole and biphenyl, are carcinogenicI.demand (O0D) and aommonia ntrogen, which ∞ould not beNowadays, the treatment methods of gasificationcompletely degraded by the traditional physical, chemical andwastewater include A/O四, SBR(3,0, adsorption [s们,biologial method. So it is very important to find an effectivecatalytic wet air oxidationF?#] and other methods C0, 1.treatment process. A combination process of catalytic oxidationAlthough these technologies are effective, there are somewith noble metal catalysts and acrobic biologial fluid-bedshortcomings, such as the long hydraulic retention timepacked with the new ultrastructure biological carriers, which(HRT), the addition of power active carbon and so on. Aswas developed by ourselves, was investigated to treat thea kind of advanced oxidation technologies, the catalytic wetgasification wastewater. The pilot scale test with 0.5 n2/hair oxidation attracted much attention for its special effectinfluent flow was carried out to investigate the performance ofthis ncw combination process. The results showed that thein the treatment of wastewater with high toxicity andCOD1815]. But there is to be high requirement forefflueant QOD was 84. 02 mg/L，ammonia nitrogen wa14.15 m/L, and total phenol was 0.20 mg/L, which couldmeeting of effluent standard to the reaction condition andcompletely meet the Grade I of Wastewater Dischargeequipment of this method, so that it will increase theStandard (GB8978-1996), when the influent average CODinvestment and running cost.was5 564 mg/L, ammonia nitrogen was 237 mg/L, andIn this paper, in order to decrease the invetment andtotal phenol was 1 100 mg/L. The two catalytic reactorsrunning cost, the combination process of catalytic oxidationcould evidently improve the wastewater biodegradability,with noble metal catalysts and aerobic biological fluid-bedand the value of BOD/0COD (B/C) increased from 0.23 topacked with ultrastructure biological carriers was investigated0.413 in the oe-stage catalytic reactor and from 0. 273 toto treat the gasification wastewater. The biological fluid-bed0. 421 in two-stage catalytic reactor. The further experimenthas the higher treatment efficiency than activated sludge due toresults showed that the efluent quality of this newits operation of fluidization, which was in favor of the masscombination process could still meet the discharge standard,transfer between the solid, liquid and air (0418] . Noble metal Ptwhen the COD loading was 8.65 kg/ (m'●d). Most ofwas selected as catalyst bcause of its exellent catalyticaromatic and heterocyclic compounds were degradedefficiency for the chain-breaking and ring-opening reaction ofeffectively in this combination process.big molecular organic compounds [942].Key words: gasi fication wasterwater; catalytic oxidation;fluidbed biological oxidation1 ExperimentalCLC number: X 703Document code; A .Article ID: 1672 - 5220(2008)02 - 0140 - 081.1 Wastewater and seed sludgeThe gasification wastewater used in the pilot scale testIntroductionof the combination process was collected from the lurgipressurized gasifier and the qualities of raw wastewaterGasification wastewater is a kind. of typical organicwere listed in Table 1. From Table 1, it could be seen thatindustrial wastewater consisting of phenols, polyeyclic aromaticthe value of BOD /COD was only 0. 23, indicating the lowcompounds and heterocyclic compounds containing nitrogen,biode中国煤化工YHCNMHGReceived date; 2007 - 10- 25Supported by the Key Project in Science and Technology of Heilongjiang Province, China (No. GB06C20401)Correspondence should be addressed t0 HUANG Jun-li, E-mail: junli hit@ 126. comJouma/ of Donghua University (Eng. Ed.) Vol. 25, No.2 (2008). 141Table 1 Water quality of the rawreactor. After the continuous aeration for 24 h, thegasification wastewatercontinue flow of 0. 1 m2/h was used in the following00D/BOD:/BOD3/domestication course. The influent COD increased fromltem(mg.L-1)mg.L~)00D2000 to 5 000 mg/L gradually. And the COD removalefficiency of above 90% was considered as the end mark ofRaw data5564.1 2790.23Standard data10030domestication process.1.2 Preparation of catalysts and biological carriersItemTotal Phenol/ Ammonia NitrogenpH1.2.1 Preparation of catalysts(mg.L-1) (NH3-N)/(mg.L-1)The homemade Pr/TiO2/Al2O /SiO2/ZnO catalyst1 100237.9was used in the catalytic oxidation reactors. Nanopowder0.51with fixed ratio of TiOr, Al2O, SiOr and ZnO were well-The seed sludge was obtained from the aeration basinmixed with shaping agent, curing agent and binder agent inin the raw treatment process of this gasification plant,the ball mill, and then the mixture were pressed andwhich had been used in treating gasification wastewatercalcinated 3 h at 800C in the atmospbere of Nz to form thewith COD of less than 2 000 mg/L for over 6 years. Sincecomplex carriers. The main activity part of catalysts Pt wasthe seod sludge was aclimated to the gasification wastewater,prepared by the incipient impregnation method. After theno substrate except high concentration wastewater was addedcomplex carriers were impregnated in 1% (Wt.) PICl solutioninto the influent in the operation of the domestication.over night, the catalysts were calcinated 5 h at 300C in theThe volume of the added seed sludge with 2.9 g/L ofatmosphere of N. The basic parameters of catalysts in twomixed liquor suspended solid (MLSS) was 20% of thecalytic oxidation reactors were listed in Table 2.Table 2 Basic parameters of catalysts in two catalytic oxidation reactorsSpecific surfaceBulk density/ShapeComponentSize/ mmarea/(m2●m~3)Porosity/%(kg.m-3)Catalysts in one-stageColumn18% TiO, 28. 7% Al2Oz,DXH=5X3.1 09253.61.42catalytic reactor34% SiO2 and 5% ZnOCatalysts in two-stage Sphericity27. 2% TIO, 28.7% AlLO3，D=568.21.171.2.2 Preparation of biological carriersThe new-style ultrastructure biological material,which was developed by ourselves (as shown in Fig. 1)，was used as the packing media in the two biologicalreactors. This ultrastructure basic material was preparedwith the mixture of activated sludge in multiplicatewastewater treatment plants by the curing process of4.7-6.2s at high-temperature. Many kinds ofbiological enzymes extracted from activated sludge wereimmobilised among the layers of this basic materialunder high temperature to form the ultrastructure(a) Common digital photobiological carriers. The basic performance parametersof the ultrastructure biological material were listed inTable 3. It was found that this new-style ultrastructurematerial had excellent porosity and rough surface,which was favorable to improve the coherence ofmicroorganism.Table 3 Basic performance parametersof the biofilm carrierVParticleSpecific surface Porosity/ Bulk density/中国煤化工0009diameter/mm area/(m2 ●m-”)%(g. cm~3)MHCNMHG0.6-18 700570.18Fig. 1 Pictures of biological carriers142Jourmal of Donghua University (Eng. Ed.) Vol, 25, No.2 (2008)1.3 Combined process flow of pilot scale testcatalysts in the two-stage catalytic reactor. The utrastructureThe detail and main technological parameters ofbiological material is used as biological crrers in the two stagecombined process flow used in the pilot scale test wasbiological aeration fluid-bed reactors. The loading level of theshown in Fig. 2, and the effective volumes of theultrastructure biological carriers in two biological reactorsstructures in this process were listed in Table 4. Thewas all 30% (v/v). Since the percentage of carbon,wastewater flowed into the one stage calytic down-flownitrogen and pbosphor in the wastewater was maladjustedfixed-bod reactor with 2 m height and 0.7 m catalysts heightafter the one-stage biological reaction, the domestic sewageafter pH adjusted to4- 5 in the adjustment tank. Cooled toof 100 L/h and 217 mg/L COD was added into the two-48C，the effluent of catalytic reactor entered the aerobicstage biological reactor by a metering pump. And 50 mg/Lbiologial fluid-bed to renove the most of biodegradableof polyaluminium chloride was added into the sedimentatedcompounds. The remained difficult biodegradable compoundswater to remove the remained COD and chroma to makein the sedimentated water were further oxidized on homemadethe effluent meet the discharge standard.T 70-85CWater LineHRT=2hDO=1.-2 mg/LBlower1720-259pH=7-82.5 mg/LT 20-30C; HRT-8hSluge LineT-25-30CHRT-3h ! MLSS-ll kg/m'Sewage LineHRT=3hRecycled Ratc- 100%H=7T-20-25CCoagulant40%HLSO4Wastewater_1610TreatedH-H+H1pH=4-5Tospuai-80C pH=7-8HRT-4hDO-0.5-1.0 mg/LHRT-2h11 Sewage12 pH=7-8HRT-8hDO-5.0 mg/Q=100 LhMLSS=4-7 kg/m'Note: 1- adjustment tank; 2- one stage catalytic reactor; 3- air bheater; 4- one -stage biologial fiud-bed; 5- oe stage biologjial sedimentationtank; 6-two-stagc atalytic reactor; 7- -two-stage catalyic sodimentatio tank; 8- two-stage biological fluid-bed; 9- two-stage biologicalsedimeatation tank; 10--cagulating sodimeqtatioo tank; 11- metering pump; 12- recycled sludge pump; 13- air tube; 14- - -aeration tube;15- -thermometer; 16- -pH meter; 17- -gas flow meterFig.2 Process flow diagram and technological parameter in the pilot scale testTable 4 Effective volume of structures inSpectrometer with a flame iooizatin detector(FID) detectorthis new combination processafter dehydration and concentration. A quartz apillary columnpacked with OV-101 with 0. 25 mm inner diameter and 50 mName of structureEffective volume/m'length was used, and the partial flow ratio was1 : 25. TheAdjustment tank2gsification compartment temperature was 280C. TemperatureCatalytic reactorcontrol program was 70C for 3 min, then increasing to 280CBiological reactorwith an rate of 3C /min. Ion source temperature of MS wasSedimentation tank1.200C , and electron energy was 70 eV.Two-stage biological sodimentation tanko.Coagulating sedimentation tank2 Results and Discussion1.4 Analytical methodsSoluble COD, BOD, NH-N and pH were analyzed by2.1 Performance of the two stage reactorsthe standard methods. Microorganisms in the effluent wasIn order to evaluate the performance of two stageobserved by common XSP-16A light microscope andreactors, the one-stage catalytic and biological reactors ranrecorded by the investigative OLYMPUS BX51 lightfor 10 d without the carriers, then the two-stage catalyticmicroscope.and biological reactors ran for the same time without the200 mL of wastewater was extracted three times bycarri中国煤化工.1 m2/h was adopted30 mL of methylene dichloride under the acidic, neutral andin thwas stable. The CODCNMH Gwasalkaline condition, respectively. The obtained organic phasesvariautu儿uruD piuos w∞ostown in Figs.3 and 4.were analyoed by a Agilent 6890 N - 5973 N GC/MSIt could be seen that the effluent COD fluctuated fromJoumal of Donghua University (Eng. Ed.) Vol.25, No.2 (2008) 143349.1 to 893. 5 mg/L during the running of only one-stagenew-style ultrastructure biological carriers, the removalcatalytic and biological reactors, the removal efficiencyefficiency of COD reached 97%. Although there werewas 80% and 93. 2% correspoundly. These indicated thatstill fluctuation on the effluent COD in the followingthe system was not stable.running time of 6 d, but the average removal efficiency ofCOD was above 95%. Especially, in the last two days, the6000100effluent quality of this combination process was best, the955 000)oeffluent COD was about 100 mg/L, and the removal4 000g5、efficiency was above 97%. So it could be considered that3 00080the cultivation process of this combination process wa200075!finished and the biomembrance on the ultrastructure70.biological carriers was mature enough to start the next1 000ssstable operation.|2345678910800000εTime/d7000I5gCeaInfluent四a Efluent -▲Removal eficiencyF 600009鱼5000Fig.3 COD change curve of influent and efluent!400085after the start-up of one- stage reactors吕30002000|00。1000I757 000”12345678 9 101112130, 90Infuent EMuent -★ - Removal eficicncye 4000-85含30000|.80Fig.5 COD change curve of influent and effluentafter the addition of utrastructure material2 000- 751000The changes of total phenol and ammonia nitrogen inthis course were also investigated and the results werepresented in Figs. 6 and 7. When the influent total phenolC Infuent CCC Efluent -▲Removal eficiencychanged between 1 024 and 1 384 mg/L, the effluent valuefluctuated from 0. 37 to 2. 70 mg/L. At the initial stageFig.4 COD change curve of influent and efluent afterthe startup of two-stage reactorswith ultrastructure biological carriers, the removalefficiency of total phenol was lower, then it increased andHowever, when the two-stage catalytic and biologicalretained above 9% with the maturation of biomembrancereactors without carriers were also started, the effluentgradually. The variations of ammonia nitrogen were similarquality of the whole system was improved, and the effluentand the removal efficiency was stabilized gradually to aboutCOD was 200 mg/L, the removal eficiencn was above 90%.91% from 84. 5%，and the effluent NH3-N was retainedEven the influent 00D fluctuated from 5533 to 18921 mg/L,about 28 mg/L with the fluctuation range of 3-4 mg/L.the removal efficiency could reach 95%. Therefore, thetwo stage catalytic and biological reactors in series careffectively improve the effluent quality, impact resistibility1400i 100.0and stabilization of the combination process.99.82.2 Effect of ultrastructure biological materialsIn order to evaluate the effect of ultrastructure| 000biological materials, these materials were added into thetwo stage biological reactors. The influent flow (Q) of0.1 m' /h was adopted in these operations until the system199.2was stable.1213149.0Fig. 5 showed the change of effluent COD of this中国煤化工011combination process. The effluent COD in the initialRemoval efolkoncystage was about 400 mg/L, and the removal efficiencyFHCNMHGwas about 90%. After 7 days, it was found that theFig.6 Total phenol change curve of influent and effluentbiomembrane had grown rapidly and maturated on theafter the addition of ultrastructure material144Jourmal of Donghua University (Eng. Ed.) Vol. 25，No. 2 (2008)00 r100 g00 t4000300 t70:艺200f00(c) Rotifer (x200)(d) iliate (x200)Ih.h.h.hhso 豆2345678910111213Fig.8 Microscope photos of biological carriers beforeTime/dand after loading the biomembrancea Influent a EMuent一 士Removal efficiencyFrom Fig. 8, lots of zoogloeas can be found aroundFig.7 NHg-N change curve of influent and effluent afterthe ultrastructure biological carriers after the acclimation,the addition of ultrastructure materialand large numbers of vorticella, ciliate, rotifer and otherTherefore, the ultrastructure biological carriers couldmetazoans were also discovered,which showed thatimprove effectively the effluent quality of this combinationoperation of the aerobic biological reactor was in a goodprocess, the removal efficiency of COD, ammonia nitrogenstateOn one hand, the microzoons could be used as theand total phenol was 97.8%， 93.8% and 99. 9%，bio indicator of the wastewater treatment; on the otherrespectively, when the system was stable. Compared withnand, they could promote the formation of zoogloea andthe ffluent quality without these carriers, the removaldecrease the concentration of cffluent suspended solidsefficiency of COD could increase 4. 7%. Furthermore,due to the good capability of phagocytosing the organicbecause the enzyme immobilized beforehand in theparticle and free bacteria. The abundant diversity ofbiological carriers was helpful to the growth ofmicrobes on the ultrastructure carriers was favorablebiomnembrance on the surface of carriers, the betterthe excellent effluent quality of aerobic biologicaltreatment efficiency could be achieved. The maturationreactor.period of biomembrance was 7-8 d. So we chase 10 d as2.4 Running of pilot scale combination processthe acclimation time of biomembrance OD the carriers,When the system was stable, the influent flow (Q)which could shorten the starting time of biological reactorwas increased from 0.2 m/h to 0.5 mr/b with the rate ofin the practical application.0.1 m/h every 20 days in order to prove the impact2.3 Biological phase characteristicresistance, and the results were plotted in Fig. 9.During the accommodation course, the sludge grewfast on the surface of new ultrastructure biological carriers95because of its good adsorption. After the domestication of7 d, the color of sludge changed from black to gray. After9085continue runoing for 28 d, it was observed that thesedimentation velocity of biomembrane with snuff color80was very fast, the sludge settlement ratio could reach31. 7% only in 7 min. According to the measurement, theJ71213116171sludge settlement ratio of 30 min (SVs) was 29. 5%，andt/dits concentration was 4396 mg/L of MLSS.一Infuent COD loading. COD termoval ficicicngThe observation of microscope for the biomembranceaunumonia ntrogcnNoval fficiency ofTota phenoland ultratructure biological carrirs was aso arried on inFig.9 Eect of infuent COD loadingorder to realize the growth and form of biomembrance,on the effluent qualityand the microascope pictures were presented in Fig. 8.As shown in Fig. 9, with the increasing of influentflow and organic loading, the removal efficiency of CODwas relatively stable at about 97%. When the influent flowwas 0. 5 m' /h, the removal efficiency of COD was lower at10 d, the efluentqualit中国煤化工。renoval eficienececouldC N M H Gal pbenol of efluent(a) Raw biological carriers (x200 )(b) After loading thekept stable and was 1ess inan 073 mg/L, and the removalbiomepbrance (x200 )efficiency was above 99, 9%. Under the Condition of theJoumal of Donghua University (Eng. Ed.) Vol. 25, No.2 (2008)145bigger influent COD loading, the removal efficiency ofand further improved the effluent quality. Furthermore, itammonia nitrogen had the bigger fluctuation, but thewas found that though the removal efficiency of COD wasconcentration of effluent was less than 15 mg/L, thelow in the one -stage catalytic oxidation reactor, the valueaverage removal efficiency could reach 93. 3%. Especially,of BODs increased from 1 279 mg/L to 2 059 mg/L, andwhen the influent COD loading was 8.65 kg 00D/ (m2● d),the value of BOD, /COD increased accordingly from 0. 23good effluent quality was still obtained, the removalto 0.413. After the two stage catalytic oxidation reactorefficiency of COD, ammonia nitrogen and total phenolthe value of BODs also increased from 442.2 mg/L towere 98. 69%, 97. 30% and 99. 99%，respectively. So this634.7 mg/L，and the value of BOD, /C0D increasednew-style combination process could tolerate big pulse ofaccordingly from 0. 273 to 0. 421, which further provedorganic and hydraulic loading, and it could keep the goodthat the catalytic oxidation reaction could increase theand stable effluent quality under the high influent flow andbiodegradability of wastewater. So there was the betterorganic loading.removal efficiency of COD and total phenol in the twoWhen the influent flow was 0.5 m' /h, the averagetage biological reactors. But the removal efficiency ofremoval efficiency of COD, NHs-N and total phenol inammonia nitrogen in one-stage biological reactor waseach reactor of this combined process was listed in Table 5.higher than that in two-stage biological reactor. This couldThe results showed that much phenolic compounds werebe explained by the lower dissolved oxygen (DO = 0.5 -decomposed in the onc-stage and two-stage catalytic1 mg/L) in the one-stage biological reactor. Under thisoxidation reactors, and the removal efficiency of totalcondition, the aerobicsimultaneous nitrification andphenol was 34.57% and 27. 38%，respectively, whichdenitrification could remove the nitrogen compoundsreduced the toxicity of the following biological treatmenteffectively.Table 5 Analysis sheet of the effluent quality in each reactorCODBODsNHs-NTotal PhenolHRTItemB/C/bC/(mg.L-1) R/% C/(mg.L-I) R/%C/(mg.L1) R/% C/(mg.L-1) R/%Onc-stage Catalytic reactor 24 98710.372 059-60.99 0.413234.01. 26719.7 34.57One-stage Biological reactor 11 62067.52442.2 78. 520. 27355. 1976.4246.70 93.51Two-stage Catalytic reactor 51 5086.91634.7-43.53 0.42153. 163.6833.91 27. 38Two-stage Biological reactor 9113.489.2832.6494.85 0. 28716.6168.750. 1299.64Coagulanting Sedimentation 288.8721.6323.5127. 9714. 8910. 310.113.79Note: C Concentration in the wastcwater; R-Removal eficiency.After the running of 80 days, it was found that, undercompounds were detected in this gasification wastewaterthe conditions of the high influent loading without the dilutedwithout dilution. Among these, the major pollutants werewater and the 0.5 m' /h influent, the combination process ofphenolic compound, quinolines, and other heterocycliccatalytic oxidation and aerobic biological fluid-bed couldcompounds. Their contributions of COD were 3 246. 54,maintain good stability and effluent quality for the treatment1 480.0 and 252. 04 mg/L, respectively.of the gasification water. When the influent average CODThree- stage aerobic acration technology with hydraulicwas5 564 mg/L, ammonia nitrogen was 237 mg/L, andretention time (HRT) of 15, 8 and8 h was used as existenttotal phenol was 1 100 mg/L, the effluent COD wastreatment process in this gasification plant, but the diluting84.02 mg/L, ammonia nitrogen was 14. 15 mg/L, and totalwater is added to adjust COD≤2 000 mg/L before one-phenol was 0.20 mg/L, which could completely meet thestage aeration tank. The effluent COD was 384. 23 mg/L,Grade I of Wastewater Discharge Standard (GB8978 -which was much higher than the value of the discharge1996).standard. Fig. 10 (b) showed the results of GC/MS analysis in2.5 Quality analysis and comparison with the rawthe effluent of raw treatment process. The concentration andprocessspecies of detected organic compound was decreased evidently,In order to analyze the effluent quality of twoand aldoxime, quinine and benzene compounds were noprocesses further, raw three-stage aerobic aerationdetected, the main residual organic compounds were alkanestechnology and new combination process, GC/MSwith中国煤化工L，the coctratioanalysis was performed to obtain the species of organicof phclic compounds wascompounds of influent and efluent. The results wereTYHC N MH G extent procss wasshown in Fig. 10.effective, the phenolic, polycyclic and heterocyclicAs shown in Fig. 10 (a), 11 species of main organiccompounds wasn't degraded completely.146Joumal of Donghua University (Eng. Ed.) Vol. 25, No.2 (2008)3 500respectively, ketones and heterocyclic compounds were not3246.54detected, and the residual concentration of phenolic and2500aromatic compounds were very low. Comparison with the2 0001480results of raw treatment process, it was obvious that the1500new combination process had the better removal effect of1000phenolic compounds, and the difficult biodegradable252.04224.23.. 52.8617.25compounds, such as quinoline, pyridines and otherbeterocyclic compounds, were all decomposed. Therefore,891011the new combination process of catalytic oxidation anaerobic biological fluid-bed was more effective to treat the1- -PIgasification wastewater than the raw three-stage aerobicQuinone; 7- - Benzenes; 8- Polycyelic aromatic hydrocarbons; 9-aeration technology, and the most of aromatic andQuinoline; 10- Pridines; 11一Other heterocyclie compoundbeterocyclic compounds was degraded by this combination(@) Results of the raw wastewater (COD=5 563.90 mg/L)process.z 1803 Conclusions160168.3E 140The good treatment efficiency for the wastewaterg 100from gasification plant was obtained by the new61.52combination process of catalytic oxidation and aerobic。「33. 1242.84。biological fluid-bed. When the influent average COD was20 [12.76221.9 14.795 564 mg/L, ammonia nitrogen was 237 mg/L, and totalphenol was 1 100 mg/L, the efuent CD was 84. 02 m/L,23456789ammonia ntrogen was 14. 15 mg/L, and total phenol wasSpecies ofoganic compounds0. 20 mg/L, which could completely meet the Grade I ofWastewater Discharge Standard (GB8978 - 1996). The twoaromatic hydrocarbons; 6- Quinoline; 7- Pyridines; 8 - Otherstage catalytic reactor could evidently improve theheterocyctic compound; 9- Alkaneswastewater biodegradability, the value of B/C increased(b) Results of the effluent of raw treatment processfrom0. 23 to 0.413 in the one-stage catalytic reactor and(COD-384.23 mg/L)from 0. 273 to 0.421 in two-stage catalytic reactor. Thefurther experiment results proved that this new-style云70厂combination process could tolerate big pulse of organic and59.23bydraulic loading. Under the condition of high influentloading without dilution and influent flow of0.5 m' /h, theeffluent quality still could be stable up to the discharge0tstandard. Most of aromatic and heterocyclic compoundswere degraded effectively in this combination process. It is8.722.7a feasible method to solve the problem of the gasificationwastewater contamination.Specias oforganic compoundsReferences1- Phenols;2- Eser;3- -Organic acid; 4- -Benzencs; s- - Polyeyeicaromatic hydrocarbons; 6- Alkanes;7- Alkenes[1] Banat F A, Al-Bashir B, AI-Asheh s, et al. Adsorption of(c) Results of the ffuent of new combination processPhenol by Bentonite [J]. Erviroumental Pollution, 2000,(COD-84.02 mg/L)107(3); 391 - 398.[2] Merzouki M，Delgenes J， Bernet N. 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