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Anaerobic digestion of baker's yeast wastewater using a UASB reactor and a hybrid UASB reactor Chiu, Chen 1990

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ANAEROBIC DIGESTION OF BAKER'S Y E A S T WASTEWATER USING A U A S B R E A C T O R A N D A HYBRID UASB R E A C T O R By Chen Chiu B.A.Sc, University of British Columbia, 1986  A THESIS SUBMITTED IN PARTIAL FULFILLMENT OF THE REQUIREMENTS FOR THE DEGREE OF MASTER OF APPLIED SCIENCE in THE FACULTY OF GRADUATE STUDIES Department of Bio-Resource Engineering  We accept this thesis as conforming to the required standard  THE UNIVERSITY OF BRITISH COLUMBIA April 1990 ° Chen Chiu, 1990  In presenting this thesis in partial fulfillment of the requirements for an advanced degree at The University of British Columbia, I agree that the Library shall make it freely available for reference and study. I further agree that permission for extensive copying of this thesis for scholarly purposes may be granted by the Head of my Department or by his or her representatives.  It is understood that copying or  publication of this thesis for financial gain shall not be allowed without my written permission.  Department of Bio-Resource Engineering The University of British Columbia 2075 Wesbrook Place Vancouver, Canada V6T 1W5 Date: April 27, 1990  ABSTRACT The start-up and step-up operation of two 16-liter, continuously operated, upflow anaerobic reactors receiving baker's yeast wastewater is presented in this thesis. The two reactors (A and B) were almost identical in construction. Reactor A was a conventional upflow anaerobic sludge blanket (UASB) reactor, and reactor B was a hybrid reactor. In addition to all the features of a UASB reactor, a fixed-film structure was installed in the mid section of the reactor B.  Both reactors were  operated at 35 °C and at a constant hydraulic retention time of 7 days.  The waste  strength, expressed in chemical oxygen demand (COD), was varied from 8 g COD liter- (during the start-up) to 58 g COD liter . The organic loading rate ranged from 1  -1  1.1 to 9.4 g COD liter day . The start-up lasted for the first 46 days. Towards the -1  -1  end of the start-up, methane production rates of 0.23 and 0.28 liter C H liter day -1  -1  4  and COD reductions of 62.2% and 67.2% were achieved at organic loading rates of 1.1 and 1.3 g COD liter day -1  -1  for reactors A and B respectively.  operation, maximum methane  production rates were,  respectively, 0.91 and 0.95 liter C H liter day -1  4  6.4 g COD liter  -1  day . -1  -1  During the step-up  for reactors  A and B  at organic loading rates of 5.8 and  In addition, reactor profiles for sludge concentration, pH,  volatile fatty acids, and COD are also presented.  ii  T A B L E OF C O N T E N T S ABSTRACT  ii  TABLE OF CONTENTS  iii  LIST O F T A B L E S  v  LIST O F FIGURES  .  vi  LIST O F ABBREVIATIONS  vii  ACKNOWLEDGEMENT  viii  I. I N T R O D U C T I O N  1  A . Problem Statement B. Proposed Solution and Objectives of the Experiment C. Thesis Organization  II. L I T E R A T U R E R E V I E W  4  A. Anaerobic Wastewater Treatment 1) Overview 2) Anaerobic Digestion B. U A S B Concept C. Sludge Granulation in the U A S B Reactor 1) The Effect of Seed Sludge Characteristics 2) The Effect of Amount of Seed Sludge 3) The effect of Wastewater Characteristics 4) Operational Parameters D. Sulfate Toxicity  III. M A T E R I A L S A N D M E T H O D S A. B. C. D. E.  1 1 2  Feed Substrate Reactors Seed Sludge Operation Analysis  4 4 5 6 7 9 10 10 11 12  15 15 16 18 19 20  IV. S T A R T - U P  21  A . Results and Discussions 1) Biogas Methane Composition 2) Effluent C O D 3) Methane Yield 4) Volatile Suspended Solids 5) Volatile Fatty Acids, p H , and P/A Ratio B. Chapter Conclusion  V. STEP-UP OPERATION  21 22 25 31 35 39 44  46  A . Results and Discussions 1) Steady-state and Transient Analysis  iii  47 47  a) Biogas Methane Composition b) Volumetric Methane Production c) COD Reduction d) Methane Yield e) Volatile Fatty Acids f) Sulfate Toxicity 2) Reactor Profile Study a) Sludge Profile and Total Sludge Growth b) pH Profile c) CODProfde d) VFA Profde B. Chapter Conclusion VI. VII.  CONCLUSIONS  49 53 56 57 59 63 64 65 70 72 76 79 82  RECOMMENDATIONS  84  VIII. R E F E R E N C E S  85  iv  LIST OF T A B L E S TABLE TABLE TABLE TABLE TABLE TABLE  3.1: 4.1: 4.2: 5.1: 5.2: 5.3:  Raw baker's yeast wastewater characteristics Start-up feed Characteristics Average steady-state data summary of start-up period Step-up operation treatment efficiency Volatile fatty acids of the step-up operation Sludge profile  V  16 21 24 52 61 69  LIST OF FIGURES Figure Figure Figure Figure Figure Figure Figure Figure Figure Figure Figure Figure Figure Figure Figure  3.1: Configuration of U A S B reactor 4.1: Biogas methane composition versus time 4.2: Total C O D versus time 4.3: Soluble C O D versus time 4.4: Total C O D reduction versus time 4.5: Soluble C O D reduction versus time 4.6: Methane yield based on C O D added versus time 4.7: Methane yield based on C O D destroyed versus time 4.8: Volatile suspended solids versus time 4.9: Volatile solids versus time 4.10: Volatile fatty acids versus time for reactor A 4.11: Volatile fatty acids versus time for reactor B 4.12: Effluent p H 4.13: Effluent propionic-to-acetic ratio 5.0: Time plot of step-up operation methane composition of reactors A and B Figure 5.1: Treatment efficiency versus organic loading Figure 5.2: Treatment efficiency versus time Figure 5.3: Volatile fatty acids versus time Figure 5.4: Sludge profile versus reactor height Figure 5.5: p H versus reactor height Figure 5.6: Total C O D versus reactor height Figure 5.7: Soluble C O D versus reactor height Figure 5.8: Acetic and propionic acids versus reactor height Figure 5.9: Isobutyric and butyric acids versus reactor height  vi  17 23 27 28 29 30 32 33 37 38 40 41 42 43 48 50 51 60 66 71 73 75 77 78  LIST OF ABBREVIATIONS BOD  5  Five-day biochemical oxygen demand according to the Standard methods for the examination for waste and wastewater  COD  Chemical oxygen demand  DS  Dry solids  TS  Total solids  TSS  Total suspended solids  TVFA  Total volatile fatty acid  UASB  Upflow anaerobic sludge blanket  VFA  Volatile fatty acid  VS  Volatile solids  VSS  Volatile suspended solids  vii  ACKNOWLEDGEMENT The author would like to express his sincere gratitude to his thesis committee members— Dr. K.V.Lo, Dr. S.T. Chieng, and Dr. R.M.R. Branion— for their special guidance. Special thanks go to Dr. P.H. Liao who provided a great deal of technical and laboratory advice.  The author is also very grateful to Adeline Lau for her  assistance in laboratory analysis. Finally, the author would like to thank his wife and parents, who were always very supportive.  viii  1  I. INTRODUCTION A . Problem Statement Baker's yeast wastewater is a by-product of the bakery yeast growing process. The wastewater consists mostly of polysaccharides, long-chain organics, minerals, and sulfate. The wastewater is characterized by a high COD content (60 to 100 g liter ), -1  which prohibits its direct disposal into the sewer.  Aerobic treatment of this  wastewater is not possible without substantial dilution, since aerobic microorganisms can only degrade wastewaters with COD concentrations in the order of a few thousand milligrams per liter.  Anaerobic digestion, however, can treat wastewaters of high  organic strengths, requires little energy to operate, and yields methane which may be burned as a supplemental energy source. The presence of high concentrations of sulfate in the wastewater causes concern in relation to anaerobic fermentation.  High concentrations of sulfurous  compounds have been known to either lower the anaerobic digestion efficiency or, in 1  worse cases, hamper the process altogether.  Nevertheless, the problem of sulfate  toxicity is not impossible to overcome. B . Proposed Solution and Objectives of the Experiment The process chosen was anaerobic digestion, and the type of reactor was the upflow anaerobic sludge blanket reactor. Two reactors operated continuously were used in this experiment. Reactor A was a conventional UASB reactor; reactor B was a hybrid UASB reactor since, in addition to the basic UASB configuration, it was equipped with ropes as afixed-filmmedium to increase surface area for bacteria to attach. UASB reactors were employed in this experiment because they are efficient and yet simple in design, and as a result have been used extensively in Europe and 1  The digestion efficiency technically refers to methane yield, which is the amount of methane gas produced per unit of feed (e.g., a gram) utilized.  2  China (Wang et al., 1985). The success of UASB reactors lies in their ability to retain sludge, which is essential to high reactor performance. The objectives of this experiment are 1) To investigate the treatment efficiencies of a UASB reactor (reactor A) and a hybrid UASB reactor (reactor B) fed with baker's yeast wastewater. 2) To study the behaviors of the two reactors during the start-up and step-up operation. 3) To determine the impact of the fixed-film system on the performance of reactor B, as compared with a conventional UASB reactor and other reactors. 4) To gain some insight into the extent of sulfate toxicity effects on the performances of the two reactors. C. Thesis Organization This thesis is organized into chapters: "INTRODUCTION," "LITERATURE REVIEW,"  "MATERIALS  AND  METHODS,"  "START-UP,"  "STEP-UP  OPERATION," "CONCLUSIONS," "RECOMMENDATIONS," and "REFERENCES". The "INTRODUCTION" serves as the overall introduction for the thesis.  The  "MATERIALS AND METHODS" is also a general section which explains such items as how the reactors used in the experiment functioned; seed sludge employed; feed material; operational regime; and chemical analyses conducted. Instead of lumping everything together in one single results-and-discussions chapter, the results and discussions have been treated in two separate chapters, namely, "START-UP" and "STEP-UP OPERATION".  The latter chapter is divided into two sections: "Steady-  state and Transient Analysis" and "Reactor Profile Study". In particular, the reason for treating the steady-state and transient results and discussions in the same chapter is merely a matter of compactness.  Had the steady-state and transient parts been  dealt with individually, repetition would be unavoidable.  3  Because the chapters "START-UP" and "STEP-UP OPERATION" are rather extensive, a chapter conclusion has been included for each of them. The thesis-wide conclusion then sums up all of the chapter and sectional conclusions, and is followed by the recommendations based on the thesis results and findings.  4  II. LITERATURE REVIEW A . Anaerobic Wastewater Treatment 1)  Overview With growing environmental concerns and energy considerations, anaerobic  treatment of wastewaters has drawn substantial interest (Lettinga et al., 1980). Listed below are the advantages and disadvantages of anaerobic treatment of wastewaters (Lettinga et al, 1980): Advantages  •  No energy is required for aeration.  •  Nutrient requirements are low.  •  Methane is generated as a by-product, which may be burned as a supplemental energy source.  •  High loading rates can be accommodated under favorable conditions.  •  Excess sludge production is low.  •  The produced sludge is highly stable and dewaters readily.  •  Active anaerobic sludge may be preserved unfed for a long period of time.  Disadvantages  •  Anaerobic bacteria grow slowly, so long periods of time are required for reactor start-up, and recovery from upsets.  •  Anaerobic digestion is very sensitive to environmental and operating factors such as toxic compounds and pH.  •  Anaerobic treatment is only a front-end treatment process; post-treatment of the treated wastewater is needed to meet disposal requirements.  •  More experience needs to be gathered with the application of the process to direct treatment of wastewaters.  5  2)  Anaerobic Digestion Anaerobic digestion involves four stages: hydrolysis, acidogenesis, acetogenesis,  and methanogenesis (Chung et al., 1988; Hill et al., 1987). In hydrolysis, complex organic matter in wastewater is broken down to soluble organics; next, in acidogenesis, they are further broken down, by acidogenic bacteria, to fatty acids (acetic, propionic, and butyric acids). Once the organic matter is in the form of acetic acid, it is then converted to methane and C0 by methanogenic bacteria (methanogenesis). 2  Long-  chain volatile fatty acids (VFA's), propionic and butyric acids, must first be degraded to acetic acid, H , and C0 2  by hydrogen-producing bacteria (acetogenesis).  2  Alternatively, another group of bacteria (homoacetogenic bacteria) also contribute to methanogenesis by converting H and C 0 to methane. 2  2  According to Chung et al.  (1988) and Hill et al. (1987), it is well accepted that 70% of the total methane derives from acetic acid while the remaining 30% results from the conversion of H and C0 . 2  2  Methanogenic bacteria are known to grow more slowly than acidogenic bacteria; besides, methanogenic bacteria are rather sensitive to environmental factors such as pH and inhibitory compounds.  Hence, it is important to make sure that the  methanogenic bacteria are not under stress if the digestion process is to proceed stably. Based on the aforementioned criteria, an accumulation of acetic acid implies that methanogens are not able to convert acetic acid into methane as fast as it is produced. Furthermore, an increase in propionic-to-acetic ratio (P/A ratio) indicates that the bacteria that break down propionic acid to acetic acid are under stress, since it has been found that propionic acid is the precursor to acetic acid (Hill et al., 1987; Segretain et ai, 1987; Denac et al., 1988). There has been much effort put into establishing criteria which give some indication as to how healthy an anaerobic digester is and when process failure is imminent. Hill et al. (1987) conducted a literature survey on the acetic and propionic  6  acids and their ratio as an indicator of process stability.  Later, Hill et al. (1988) went  on with further work, focusing on the longer-chain V F A ' s such as butyric and valeric acids. Their most important conclusions are as follows: 1) Total volatile fatty acid (TVFA) concentrations greater than 2000 mg liter- , 1  acetic acid concentrations higher than 800 mg liter , and a P/A ratio greater -1  than 1.4 are reliable methods of predicting the failure of anaerobic process. Of these criteria, the combination of acetic acid and the P / A ratio provides the best index for digestion failure prediction. 2)  Longer-chain V F A ' s , butyric and valeric acids and especially their iso-forms play an important role in detecting the stress which precedes failure.  3)  When the iso-butyric and iso-valeric acids concentrations are below 5 mg liter , -1  the anaerobic digestion is under little or no stress. If these iso-forms rise to the concentration range of 5-15 mg liter , the digester is under much stress and -1  failure is impending if the problem is not corrected. Concentrations of iso-forms higher than 15 mg liter  -1  means that failure has already set in.  B . U A S B Concept The basic idea of the U A S B process, first conceived in 1971 by Lettinga and his  co-workers  in The Netherlands,  is  the  reactor's  ability  to  retain  a  high  concentration of viable sludge, combined with a good contact between the sludge and the incoming wastewater (Lettinga et al., 1980). The wastewater is introduced into the reactor from the base. It then slowly flows up the reactor column through the sludge bed and blanket and is digested in the process. -The ability to keep active sludge in the reactor is vital both to a quick start-up and superior reactor performance.  The U A S B reactor achieves high sludge retention  through a liquid-solids-gas separator.  This separator comprises a cone, with its larger  base either facing up or down, sealed to the reactor inner wall near the top of the reactor. In either case, the underlying principle is the same: the device achieves high sludge retention by creating a quiescent zone near the top of the reactor which helps  7  rising sludge floes form larger aggregates and sink back down.  The mechanism  through which sludge floes rise can be turbulence or flotation. The type of separator discussed here is one with the cone's base facing upward. At some clearance directly in front of the cone tip (which faces downward) is fitted a smaller cone with its tip pointing toward the tip of the larger cone. This construction minimizes sludge loss by blocking the uprising mixed liquor from hitting directly the tip of the larger cone. Generated biogas, though, becomes collected in the smaller cone, and, when it fills the smaller cone, it escapes from the perimeter of the cone upward and collects in the space between the reactor liquid surface and the base of the larger cone which is sealed to the reactor wall. The biogas collecting in the cone headspace is then routed to a gas volume measuring device.  In addition, as floes of bacteria rise, through buoyancy  provided by rising gas bubbles or lack of settleability of the bacteria, and travel through the cone, the liquor velocity tapers off due to the enlargement of the diameter of the cone. As a consequence, the rising bacteria particles slow down and tend to gather near the liquor surface and form larger floes which will then sink down the reactor. C.  Sludge Granulation i n the U A S B Reactor The success of a UASB reactor depends on the development and immobilization  of a sludge with high activity and superior settling characteristics (Lettinga et al., 1980, 1985).  Newly generated bacteria may become immobilized on particulate  matter and immobile surface through mechanisms of attachment, entrapment, or intertwinement.  In the case of sludge immobilization on particulate matter,  aggregation of bacteria takes place and leads to the formation of granules. In the case of immobilization onto afixedmedium, a layer of biomass develops on the surface of thefixed-medium.Fixed-film immobilization, in particular, plays a significant role in  8  retaining sludge, especially in reactors started up with thin and not-so-well-settled seed sludge.  The idea of retaining as much biomass as possible is applicable for all  anaerobic reactors treating a whole range of wastewaters. Lo et al. (1984), treating dairy manure in laboratory-scale 4-liter batch reactors, confirmed the significance of support material for retaining biomass and thus improving treatment efficiency  and tolerance to stress.  It has been found that  immobilization both on fixed surface and on particulate matter occurs rather easily. The basic mechanism for granulation is briefly discussed here.  Newly generated  bacteria attach to the primary nuclei which are the heavier sludge floes in the seed sludge, which is commonly digested sewage sludge. Later in the start-up, the eruption of attached bacterial films or break-up of larger bacterial aggregates will give rise to secondary nuclei. Similar to the primary nuclei, the secondary nuclei themselves will eventually form granules.  Unlike a fluidized-bed reactor, for instance, the U A S B  reactor has the ability of retaining the smaller secondary nuclei, which can gradually grow into larger aggregates (Lettinga et al., 1985). The sludge with these qualities is one that is well-pelletized.  It has been reported that the sludge in a U A S B reactor  stratifies according to the sludge particle size: from large aggregates to fine suspended sludge particles (Andrews et al., 1988). Larger and dense particles tend to be granular and occur mostly in the lower region of the sludge bed. Next up are the sludge floes which are less dense than the granular ones. volume indices of 10-20 and 20-40 ml g  - 1  Lettinga et al. (1980) reported sludge  for granular and flocculant sludge. The same  authors also found that granular sludge was superior to flocculant sludge in activity and settleability.  Furthermore, two types of granules can form: granules comprising  predominantly filamentous-type or rod-type microorganisms. difference are not well understood (Andrews et al., 1988).  The causes  for the  9  Sludge granulation in the UASB reactor may be seen in three phases (Barford, 1988; Wu etal, 1985): •  First Phase. This phase is the start-up period. The reactor is started with seed sludge. The organic loading rate at this time is low. The sludge bed expands upwards as gas production picks up. Filamentous organisms tend to grow, and hence sludge settleability deteriorates.  •  Second Phase. As loading increases, poorly-settled sludge floes become washed out the system; denser sludge particles start to compact at the bottom of the reactor and grow larger giving rise to thefirstnew granules.  •  Third Phase. As the loading is further raised to near the optimum, sludge granulation proceeds rapidly. Once the sludge is in the granular form, sludge washout reduces to a minimum; hence there is a positive net sludge growth. The reactor is then able to operate stably at high volumetric loading regimes. Major factors affecting sludge granulation include seed sludge characteristics,  the amount of seed sludge used at start-up, wastewater characteristics, and operational parameters and management (Lettinga et al., 1985). These factors are each elaborated in the following sub-sections. 1) T h e Effect of Seed Sludge Characteristics The choice of seed sludge is of great importance, especially in relation to startup. Commonly, digested sewage sludges are used as seed materials. Lettinga et al. (1985) recommended the use of thick types of sludge with dry solids (DS) concentrations of 60 g DS liter . Thinner types of sludge (less than 40 g DS liter ) -1  -1  are higher in methanogenic activity than the thicker types, but thicker sludges display better settleability than the thinner. In spite of its lower methanogenic activity, the thicker digested sludge will be retained more easily in the reactor allowing the development of more granules. When a thinner seed sludge is used, it takes relatively little time for the sludge bed to expand upward and throughout the entire reactor height.  This excessive expansion implies that the sludge retention time is greatly  10  shortened and hence there may not be enough time for the development of well-settled bacterial aggregates.  In this case, bacterial granulation can only take place via  attachment to inert well-settleable support particles and to the reactor wall. As far as speeding up the granulation process is concerned, two methods are mentioned by Lettinga et al. (1985). First, enhanced granulation may be realized by supplying to the reactor contents inert granular carrier material such as hydroanthracite or gravel. This first method bases on bacterial attachment to inert wellsettleable particles as explained above. Second, granulation will proceed more readily if a small amount of crushed granular sludge is added to the seed sludge. The added crushed granular sludge consists of small active nuclei which, if properly managed, will grow into larger granules and segregate from the more flocculant sludge. 2)  T h e Effect of A m o u n t of Seed Sludge The amount of seed sludge that is needed for a good start-up is not arbitrary.  Normally, one would judge that, the more seed sludge one uses, the faster the start-up and better subsequent reactor performance will be. However, it has been shown that excess seed sludge leads to an unnecessarily expanded sludge bed which will tend be washed out the system. Conversely, too little seed sludge will cause the start-up to take very long. Existing experiences suggest a mixed liquor concentration of 12-15 g VSS liter if thick digested sewage sludge is used. For the case of a thin digested -1  sewage sludge (less than 40 g TS liter ), a 6 g VSS liter mixed liquor concentration -1  -1  should be maintained (Lettinga et al., 1985). 3) T h e effect of Wastewater Characteristics The ease with which granulation occurs is highly waste-dependent. Barford (1988), Lettinga et al. (1980, 1985), and Wu et al. (1985) made the following important points:  11 •  Granulation occurs most readily in wastes rich in soluble carbohydrate, such as sugar beet and potato processing effluents. In wastes like render waste, distillery waste, and corn starch waste, granulation proceeds at relatively slow pace.  •  Granulation is a result of bacterial growth; therefore, all nutritional requirements (i.e., N, P, S, and trace elements) must be present in sufficient concentrations; otherwise, they must be supplemented to the wastewater. Influent nitrogen levels must be in the quantity of 30:1 to 55:1 in terms of COD:N ratio. When there is enough buffering capacity in the reactor mixed liquor, a COD:N ratio of 200:1 is acceptable. (In anaerobic digestion, buffering capacity is provided by ammonium hydroxide, which results from the breakdown of proteinaceous matters in the feed substrate.) The phosphorus requirement is commonly assumed to be one-fifth of the nitrogen requirement. As a general rule, the minimum concentrations of N, P, and S may be estimated based on the bacterial composition and growth yield factor. As to trace elements, the addition of Ni, Co, Mo, and ZnS0 has led to positive results. 4  •  The presence of low levels of C a (less than 200 mg liter- ) has been found to exert a positive influence on granule formation. The probable reason is that C a may serve as a cementing agent providing mechanical strength for the floes. However, when granular sludge is employed to treat a wastewater rich in C a , CaC0 scaling of the granules occurs. In addition, excess C a may raise the density of the sludge bed such that the contact between the incoming wastewater and the sludge bed becomes hindered. High concentrations of N H have also been found to be inhibitory to granulation. 2+  1  2+  2+  2+  3  +  4  4)  Operational Parameters Operational parameters are vital in contributing to granulation; the following  guidelines should be adhered to (Lettinga et al., 1985; Wu et al., 1985): •  pH should be kept between 6.5 and 7.8.  •  For mesophilic digestion, the reactor operating temperature should be maintained in the optimal range of 35°C to 40°C.  •  The control of sludge loading plays an important role in the speed at which granulation proceeds. According to the research done by Wu et al. (1985),  12 granules began to appear at a sludge loading of 0.3 g COD g VSS day for brewery wastewater. The same finding was confirmed by other authors treating distillery and citric wastes. Moreover, Wu et al. (1985) suggested that after start-up the sludge loading rate be raised to over 0.6 g COD g VSS day so as to speed up granulation. -1  -1  -1  -1  •  Hydraulic loading is important in that it can be used to impose a selection pressure on the system. Higher hydraulic loading rates have been proven to be beneficial to granulation. At higher hydraulic loading rates, light and bulking sludge tends to migrate upwards whereas heavy sludge tends to collect at the bottom of the reactor. Since the nutrients (the incoming wastewater) are introduced from the base of the reactor, the heavy sludge is allowed to get its food first and granulation takes place more quickly than when no selection pressure is imposed. Hydraulic loading rates of 0.25 to 0.4 m m hr have been suggested. Where a wastewater is high in strength (higher than 5 g COD liter ), pulse feeding is recommended (Wu et al., 1985; Lettinga et al., 1985). 3  -2  -1  -1  •  Granulation proceeds best when the feed wastewater strength is low: 1.5 to 4 g COD liter is recommended. When the wastewater strength is low, continuous feeding should be employed; if the wastewater strength is high (over 5 g COD liter ), pulse feeding or effluent recycle will be necessary. The purpose of using a dilute wastewater is to apply a high selection pressure on the system, i.e. relatively high hydraulic loading. The selection pressure promotes the washout of finely dispersed matter from the seed sludge and newly formed dispersed bacterial matter— while allowing the heavier sludge to remain in the reactor. The presence of high concentrations of inert and biodegradable suspended matter discourages (and in some cases inhibits) granulation. -1  -1  D . Sulfate Toxicity Sulfurous compounds are commonly found in many industrial wastewaters (Sarner et al., 1988; Lettinga et al., 1985). When sulfurous organic compounds are biologically oxidized, they give rise to sulfate.  Sulfate can be reduced to hydrogen  sulfide (and elemental sulfur and/or organic sulfurous compounds, to a lesser extent) anaerobically by sulfate-reducing bacteria (SRB), which utilize sulfate as an electron acceptor. The electron donors are hydrogen and acetate, which are the main substrate for methanation. SRB have a greater affinity for hydrogen and acetate because sulfate  13  reduction is thermodynamically favored over the reduction of bicarbonate (Isa et al., 1986). The competition between methane production and sulfate reduction is shown below: Methane Production:  4H + HCOg- + H+ —> CH + 3H 0 2  4  2  CHgCOO- + H 0 - » CH + HCO 2  4  s  Sulfate Reduction:  4H + S + H  HS- + 4H 0  +  2  2  CHgCOO- + S0 2- - » HS- + 2HC0 4  3  HS- + H+ —» H S 2  Sulfate itself does not pose the worst problem in anaerobic digestion. Lettinga et al. (1985) stated that sulfate levels below 5 g S 0  = 4  liter do not cause significant -1  inhibition. Usually, the concern is focused on the main by-product of sulfate reduction, H S, and its dissociation species, HS- and S , as shown below. =  2  H S <-+ HS + H -  +  2  HS- <-• S= + H+ H S is most toxic, followed by HS , which is in turn more toxic than S (Sarner -  =  2  et al., 1988). It has been shown that, as long as the COD/S0 H S inhibition is rather insignificant. 2  = 4  ratio is above 10 g g , -1  The reason is that H S is naturally removed 2  from an anaerobic reactor through the so-called gas stripping process.  As H S is 2  produced in the reactor mixed liquor, it is mixed with the rest of the biogas and leaves the system.  This built-in ability of removing H S is significantly reduced as the 2  COD/S0 = ratio falls below 10 g g . -1  4  14  There are several ways through which H S toxicity can be controlled (Sarner et 2  al, 1988): •  Dilution of the wastewater helps alleviate the toxic effects of H S.  •  Removal of H S through precipitation with the addition of metal ions such as BaCl (Lo et al, 1989).  2  2  2  •  Adjustment of pH to the range of 7.5-8, where most H S is in the less toxic form, US'. In practice, S may be disregarded because it exists in negligible levels for a pH below 8. 2  =  •  External H S stripping (Lettinga et al., 1985). 2  III. MATERIALS AND METHODS A . F e e d Substrate The feed was prepared from baker's yeast wastewater obtained from a local bakery yeast grower. Raw baker's yeast wastewater was diluted down to the desired COD concentrations ranging from 8 to 60 g liter . The characteristics of the raw -1  wastewater are summarized in Table 3.1. Worth noting is the low BOD -to-COD ratio 5  (1:3 to 1:6), which implies that a good percentage of the wastewater consists of hardto-degrade organics. The concentration of nitrogen required to support biological growth is estimated as 30:1 to 55:1 in terms of COD:N ratio. Using a COD:N ratio of 45 and a raw wastewater concentration of 80,000 mg liter , the required nitrogen is calculated to be -1  1780 mg liter ; then 355 mg liter of phosphorus is needed. As it was, the raw -1  -1  wastewater used seemed to contain adequate nitrogen (1,610-2,060 mg liter ) but was -1  lacking in phosphorus (only 108 mg liter of P0 -1  3+ 4  ).  As a nutrient supplement,  NH C1 and K HP0 were added to the feed at proportions of 0.50 and 0.24 g liter 4  2  respectively.  -1  4  The supplemented nitrogen (170 mg liter  -1  as N H , by weight +  4  percentage) ensured that there was plenty of nitrogen. As for phosphorus, about 130 mg liter of phosphate was supplemented to the feed substrate. Because dilution of -1  raw wastewater was always the case, nitrogen and phosphorus requirements would work out to be less than the numbers calculated above for full-strength wastewater. Hence the amount of phosphorus added was considered adequate. Also the feed was pH-adjusted to about 7 at the time of preparation, and it 2  was stored at 4°C in a walk-in cooler. Whenever needed, a portion of the stored feed was transferred into the feed tank which in turn was kept in a refrigerator maintained  2  pH adjustment was done by adding concentrated NaOH solution to the feed which was thoroughly stirred and whose pH monitored by a pH meter.  16  between 2°C and 4°C. No batch of feed was ever kept for longer than 2 weeks. During the two-week period, it was found that the various characteristics of the feed (such as TSS, pH, and COD) did not change to any significant extent.  T A B L E 3.1: Raw baker's yeast wastewater characteristics* 5-day BOD COD BOD-to-COD ratio  18,340-27,200 70,000-100,000t 1:3 to 1:6 3,800-7,300 1,610-2,060 108 1,700-3,200 4.0-5.0  Total Kheldahl Nitrogen Sulfate pH * All, except pH, expressed in mg liter , t 80,000 mg liter is the norm. -1  -1  B . Reactors Both reactors were of UASB reactor design except that reactor B incorporated a fixed-film system to increase surface area within the reactor for bacteria to adhere onto. The UASB reactor configuration is depicted in Figure 3.1. The reactor was a cylinder made of acrylic plastic with an inner diameter of 11.5 cm and a total length of 168 cm. The working volume was 16.0 liters. Eleven sampling ports were installed along the length of each reactor starting from near the bottom. The spacing between two neighboring sampling ports was such that it widened towards the top of the reactor. A feature in the reactor design that distinguishes UASB reactors from others is the conical three-phase separator located near the top of the reactor as indicated in Figure 3.1.  The separator separates and collects the biogas produced from the  wastewater. The biogas goes through a water column (which regulates the liquid level  17  (c)  :  7.  y  ....7.  (e)  (c) *w  \  : -  (f)  -J  Figure 3.1:  (a) (b) (c) (d) (e) (f) (g) (h)  Effluent Three phase separator Biogas Wet gas meter Water seal Sampling taps Feed pump Feed tank  Configuration of UASB reactor  18  around the separator) and passes through a wet gasmeter.  Furthermore, the  separator is constructed in such a fashion that its conical base faces upwards. As the cross section area increases, the velocity of the fluid flow drops and causes the sludge to be retained in the reactor. The effluent overflows from the top of reactor and is collected in a container. In addition to its basic UASB design, reactor B was equipped with a matrix of 19 parallel ropes (0.4 cm in diameter and 88.9 cm in length) in its mid section, beginning at a height of 33.0 cm measured from the base of the reactor. The ropes were intended to increase the surface area on which bacteria could attach. With the ropes, reactor B's surface-to-volume ratio was boosted from 32.1 (same for both reactors) to 45.4 m rrr , an increase of 41.4%. 2  3  A peristaltic pump was used to continuously draw the feed from the feed tank, pass it through a copper-alloy coil immersed in a warm-water bath to bring the feed temperature up to near that of the reactor mixed liquor, and then introduce it into the reactor from the bottom. The reactor mixed liquor was kept at 35 °C via a series of heating pads wrapped around the body of the reactor which were feed-back controlled through a multi-channel temperature controller. C. Seed Sludge Sludge from the effluents of other laboratory-scale anaerobic reactors treating baker's yeast wastewater was incubated at room temperature (about 20 °C) in a glass jar for over a month before being seeded into the reactors. During this period the sludge was fed regularly with raw baker's yeast wastewater.  The aim of the  incubation of the sludge was two-fold: (1) growing a large enough quantity of seed sludge for use and (2) developing active bacteria in the form of granules. At the time of seeding, the seed sludge was mostly fine particles with some floes and granules.  19  Each reactor received 5.1 liters of this seed sludge at 11.4 g liter VSS; hence the -1  initial amount of sludge in each reactor was 58.3 g (i.e., 3.6 g for each liter of reactor volume) in the form of volatile suspended solids . 3  D . Operation The reactors were continuously fed and run at a fixed hydraulic retention time (HRT) of 7 days which was about 2.3 liters of feed pumped in everyday. The low loading rate was thought to minimize perturbation in the reactor; perturbation could lead to excessive sludge washout before the sludge had time to establish itself. This first period of time constituted the reactor start-up which lasted 46 days. The reactors were first fed with a feed at 8 g COD liter until they stabilized. During -1  this time period, the organic loading rate was kept relatively low and constant (other operating parameters also kept constant) so that the seeded sludge would have time to accustom to the new reactor environment and so that observations thus obtained would represent the true start-up behavior of the reactors. Then, during the step-up operation period, the feed COD concentration was increased stepwise to 18, 25, 30, 35, 40, 45, 50, 55, to 58 g COD liter . It was the -1  intention of the author to investigate the entire loading range covered to find such things as the operating setting in which the gas production was maximum and the setting in which the reactor became unrealistically inefficient. Moreover, the loading regime was planned with the hope that total system failure might be reached within the loading range imposed.  VSS is widely accepted as a measure of amount of biosludge.  E . Analysis The same set of chemical analyses were done on both the feed and effluent. The total solids (TS), volatile solids (VS), total suspended solids (TSS), volatile suspended solids (VSS), BOD , and S 0 5  methods (A.P.H.A., 1975).  = 4  were determined according to the standard  Both total and soluble COD were determined by the  colorimetric method (Knechtel, 1978).  Biogas composition and volatile fatty acids  (VFA) were analyzed on a Hewlett Packard 5890A gas chromatograph. The volume of biogas was measured with a wet gasmeter; the measured volume was corrected to the standard temperature and pressure (STP) which are 0°C and one atmosphere. Total Kjeldahl nitrogen (TKN) and ammonia nitrogen (NH -N) were determined using a 3  block digester and a Technicon Auto Analyzer II respectively (Schumann et al., 1983). BOD and S 0 5  in this thesis.  = 4  tests were done only as a check; no results have been shown  IV. START-UP The start-up period was meant to help the seeded sludge to multiply and, at the same time, acclimate to the new reactor environment.  A t the beginning of the start-  up, each reactor was seeded with 58.3 g of sludge which had previously been incubated for the purpose.  The feed strength was maintained at 8 g C O D liter  -1  at an average  H R T of 7 days. The relatively low feed strength was intended to help minimize loading shock and buoyancy effects caused by gas bubbles in the reactor mixed liquor, and thus establish an active and, preferably, granular sludge as early as possible. The characteristics of the feed for the start-up period are summarized in Table 4.1.  T A B L E 4.1: Start-up feed Characteristics pH V S (g liter ) V S S (g liter ) C O D (g COD liter ) Total.... Soluble B O D (g BOD liter ) B O D - C O D ratio V F A (mg liter ) Acetic Propionic Isobutyric Butyric -1  -1  7.0 6.91 1.52  -1  -1  8.11 7.03 2.51 1:3  -1  301 43 7 29  A . Results a n d Discussions Existing literature on the anaerobic treatment of baker's yeast wastewater utilizing the U A S B reactor is very scarce, rendering comparison between results found in this study and those from the literature extremely difficult.  Therefore, comparison  has mostly been done between the two reactors— mainly to identify any effects of the ropes in reactor B.  22 1) Biogas Methane Composition The biogas methane composition can serve as an indicator of the stabilization of the fermentation process (Figure 4.1).  It is clear that the methane percentage in 4  biogas increased essentially monotonically from 14.5% and 24.0% on day 1, A and B respectively, to 59.0% and 55.1% on the 46th day. Noteworthy is the presence of a small dip for both reactors around day 10; after the dip, the methane content climbed rather rapidly until day 18. Thereafter, the methane content appeared to have come to a plateau with some minor depression near day 30 for reactor B. Information about reactor A at this point was not available because a gas leak was detected between day 18 and 38. Hence, the missing points were thought best represented through linear interpolation. Steady state during the start-up has been defined as the state of the reactor system (the microorganisms and reactor environment) in which the system parameters (methane production, VFA levels, etc) did not vary by more than 10% over a time span of three or four days.  Basing merely on Figure 4.1, reactor B virtually achieved  steady state after day 17, but reactor A did not reach steady state until after day 43. Basing calculations on days 43 to 46, the corresponding mean methane compositions achieved were 59.1% and 54.8% for reactors A and B respectively. A summary of all steady-state data is found in Table 4.2. On the basis of the methane compositions between days 43 and 46 alone, it appeared that reactor B did not perform better than reactor A. However reactor B's volumetric production rate was significantly higher than that of reactor A (0.28 ± 0.01 versus 0.23 ± 0.02 liter CH liter day ). The implication here is that if reactor -1  -1  4  B were to achieve the same methane yield as reactor A, reactor B would have to, and in fact did, sustain a proportionally higher COD utilization. In addition, as hinted at 4  Throughout the thesis, biogas methane composition was always expressed as percentage on a volume-to-volume basis.  BIOGAS METHANE COMPOSITION  FIGURE  4.1: B i o g a s Methane C o m p o s i t i o n v e r s u s Time  24  earlier, by day 18 reactor B had already attained a methane composition of 55.3%, which was essentially reactor B's steady-state value (54.8%).  With reactor A,  however, a methane composition of only 45.0% was achieved by day 18. In short, according methane composition data alone, it took far less time for reactor B to arrive at steady state. Thus the merit of the fixed medium in the form of ropes in reactor B could not be dismissed.  However, it should be noted that COD reduction and the  related parameters such as methane yield are more important from an operator's standpoint.  T A B L E 4.2: Average steady-state data summary of start-up period HRT (days) Waste strength (g COD liter- ) Loading Rate (g COD liter- day ) Methane Content (%, v/v) Methane Production Rate (liter CH liter- day- ) Methane yield (liter CH g- COD destroyed) Effluent Characteristics pH VS (g liter- ) VSS (g liter- ) COD (g COD liter- ) Total Soluble BOD (g liter- ) VFA (mg liter- ) 1  1  1  1  1  4  1  4  1  1  A  B  7.35  6.42  8.11  8.11  1.11 + 0.05 59.1 + 0.4  1.27 ± 0.03 54.8 ± 0.2  .. , 0.23 ± 0.02  0.28 ± 0.01  0.34 + 0.03  0.33 + 0.01  7.82 + 0.06 , ,., 3.1 + 0.1 0.3 + 0.1  7.81 + 0.05 2.8 + 0.1 0.2 ± 0.01  ... . 3.08 + 0.16 , . 2.95 + 0.05 0.99  2.67 ± 0.07 2.68 ± 0.09 0.75  61 + 7 48 + 34 0 0  44 ± 8 10 + 6 0 0  ,, 62.1 + 2.0 58.0 + 0.8 60.6  67.1 + 0.9 61.9 + 1.2 70.1  1  1  1  Propionic COD Reduction (%) Total Soluble BOD Reduction (%)  25  Yan et al. (1989a) conducted a start-up study of a UASB which treated cheese whey mesophilically using a 14.5-liter UASB reactor of rather similar configuration. The reactor was operated for 48 days, which were considered the start-up period, at organic loading rates of 0.91 and then 1.97 g COD liter day . -1  -1  The methane  compositions achieved for the two organic loading rates were 56.5% and 48.2%. These numbers were comparable with those obtained in this thesis experiment: at similar organic loading rates of 1.11 and 1.27 g COD liter day for reactors A and B, the -1  -1  corresponding methane compositions of 59.1% and 54.8% have been attained. 2)  Effluent C O D The establishment of the biomass in the reactors was reflected partly in the  consistent lowering of effluent COD. The amount of biomass at a point in time can be estimated by such sludge sample tests as COD, VS, and VSS. Specific discussion pertaining to sludge present in the reactor is found in the session entitled "Reactor Profile Study". As bacteria utilize nutrients in the feed wastewater for maintenance energy and cell material synthesis, the organic strength of the feed decreases. But this decline in organic waste strength will only take place if the bacteria themselves do not get washed out of the reactor excessively and end up in the effluent stream. When excessive sludge washout occurs, even though COD removal is not insignificant, the resulting effluent COD may still be higher than that of the influent. The lack of good settling characteristics of the sludge is common during start-up and contributes to an overexpansion of the sludge bed and hence excessive sludge loss. Both total and soluble effluent COD's showed the same pattern (Figures 4.2 and 4.3) for both reactors. Of special interest is that the effluent COD levels during the first few days were found to be higher than that of the feed. As time progressed, a transition was observed, after which the effluent total COD's decreased steadily to a  26  level of 3000 mg liter- . 1  Similarly the percent C O D reduction (Figures 4.4 and 4.5)  pointed to the same conclusion.  Its pattern is the opposite of that of Figures 4.2 and  4.3. Both total and soluble C O D reductions increased consistently from around -20% to 60%; then they remained relatively constant.  Based on the total-to-soluble-COD ratio  and V S S (to be discussed in a later section), there was excessive sludge washout between days 10 and 15. The negative values also suggested that, at the beginning of the start-up phase, the 5.1 liters of seed sludge slurry probably contained a high concentration of colloidal and soluble C O D , so that, when the reactor was filled up to its capacity, the overall C O D concentration of the mixed liquor was higher than that of the feed.  substantially  Consequently, during the first few days, the effluent  soluble and total COD's were higher than their influent counterparts.  However, over  time, as new feed was introduced, the initially high C O D concentration was gradually "diluted", giving rise to a negative-to-positive turnover. While both reactors display the same pattern in total and soluble C O D , distinct and consistent difference evidences reactor B's superior performance.  the It is  unmistakable from Figures 4.2 and 4.3 that reactor B was consistently lower than reactor A in both total and soluble C O D .  Similarly, reactor B always achieved higher  reduction both in total and soluble C O D (Figures 4.4 and 4.5).  As a whole, each pair  of curves in Figures 4.2 through 4.5 follow each other very closely, looking almost parallel to each other. During steady-state, the effluent total C O D values for A and B were 3.1 and 2.7 g C O D liter- while total C O D reduction values were 62.1% and 67.1%. According 1  to Table 4.2, reactor B's numbers are statistically different and better than those of reactor A . Not only so, the pathways by which the reactors arrived at those values strongly suggested that the ropes did have a positive effect on reactor B.  EFFLUENT COD (TOTAL) 11000-  10000-  9000H  •  Reactor A  •  R«actor B  8000H  0>  7000-  a  o  O  ^  6000-  50004000-  3000-  2000-  — r 20 -  10  15  — r 25  30  TIME (DAY)  FIGURE  —r~ 35  4.2: T o t a l COD v e r s u s Time  — r 40 -  -1  45  -  —i 50  ro  SOLUBLE COO (mg liter")  82  TOTAL COD REDUCTION (%)  62  EFFLUENT COD REDUCTION (SOLUBLE) 80-1  FIGURE  4.5: S o l u b l e COD R e d u c t i o n v e r s u s Time  GO O  3)  Methane Yield Figures 4.6 and 4.7 depict methane yield for the two reactors expressed in liter  CH g- COD day , where COD is added or destroyed . 1  1  5  4  The per-COD-destroyed  methane yield has been preferred and used for this discussion because it reflected the extent to which sludge was being washed out of the reactors. Both reactors showed the same trend in methane yield, the only difference being in timing. The methane yield started off by going through a negative depression. Then recovery in the form of a negative-to-positive turnover was observed and was followed by stabilization (a plateau) which lasted for the remainder of the start-up period. As indicated already, from days 18 to 38, there was a gas leak in reactor A; therefore, Figures 4.6 and 4.7 employed linear interpolation for reactor A during this time interval. The methane yield values for both reactors began slightly negative, -0.18 and -0.23 liter CH g 4  -1  COD day for A and B respectively. 1  Then the methane yield  values continued to fall for both reactors. Reactor B hit its lowest of -0.60 liter CH g~ 4  COD day at day 10; reactor A, however, would not reach its lowest of -4.59 liter CH 1  4  g COD day until day 14. After the reactors had reached their lowest methane yield -1  1  values, they each commenced to recover by going through a negative-to-positive turnover.  Both the COD reduction (Figures 4.4 and 4.5) and methane yield  (Figures4.6 and 4.7) indicate that the turnovers occurred near days 15 and 10 for reactors A and B respectively. The first methane yield values immediately after the turnovers were 0.33 and 1.13 liter CH g- COD day for A and B respectively. 1  1  4  Hereafter, the methane yield values underwent some decrease up to day 18 (down to 0.20 and 0.31 liter CH g- COD day for A and B); then they began to stabilize and 1  1  4  eventually reached the steady-state with methane yield values relatively constant  5  COD destroyed means COD utilized.  l  METHANE YIELD (COD ADDED) 0.45-1  T~  i  i  5  10  15  FIGURE  4.6:  i— 20  r— 25  TIME (DAY)  , 30  1 35  ,  p-  40  45  Methane Y i e l d Based on COD Added v e r s u s Time  METHANE YIELD (COD DESTROYED) 2-i  34  ranging between 0.3 and 0.4 liter CH g- COD day (Table 4.2). Methane yield 1  1  4  values of reactors A and B practically merged. The negative methane yield values observed in the first 15 days were due to relatively large amounts of washed-out sludge in the effluent stream. Washed-out sludge contributed to the COD of the effluent. In effect, COD in the form of washedout sludge was so high that it more than offset COD removed by bacteria, giving rise to negative COD reduction and hence negative methane yield. The unusually large magnitudes of the peak methane yield values (positive and negative) had to do with the definition of methane yield itself. Methane yield is the quotient of CH produced and COD destroyed (or removed), the former being the 4  numerator and the latter the denominator. Therefore, an unusually small negative value of COD destroyed would lead to a large negative value of methane yield (e.g., 4.59 liter CH g COD day for reactor A). Similarly, a very small positive value of -1  1  4  COD destroyed would produce a large positive value of methane yield (e.g., 1.13 liter CH g- COD day for reactor B). 1  1  4  Despite the fact that steady-state methane yield values for the two reactors were virtually the same, when comparing one reactor with the other, two remarks may be made.  First, time needed for recovery from negative methane yield was  shorter for reactor B than for reactor A— 10 days for reactor B and 15 days for reactor A. Second, whereas reactor B experienced a slight negative swing (-0.60 liter CH g- COD day ), reactor A went through a sharp valley (-4.59 liter CH g- COD 1  1  1  4  4  day ). 1  Moreover, after its negative-to-positive turnover, reactor B had achieved a  positive peak of 1.13 liter CH g- COD day before starting to stabilize. 1  4  -1  These  observations all point to the advantages that reactor B had been enjoying because of the fixed medium installed in it. In summary, with the ropes as fixed-medium to enhance attachment area for bacteria, reactor B displayed superior performance in the  35  form of shorter time needed for negative-to-positive turnover to occur, and lessening of variability in methane yield. A methane yield range between 0.30 and 0.33 liter C H g- C O D d a y 1  was  -1  4  reported by Y a n et al. (1989a) for the start-up of their U A S B reactor which treated cheese whey at 35 ° C . Their organic loading rates of 0.91 and 1.97 g COD liter  -1  day  -1  were comparable to those applied to reactors A and B in this study (1.11 and 1.27 g COD liter  -1  day ). -1  It was interesting to note that the corresponding methane yield  values in this study were 0.34 and 0.33 liter C H g 4  - 1  COD day  -1  for the two reactors.  Whereas the reactor Y a n et al. (1989a) operated was producing at 1.37 and 3.25 liter C H liter  -1  4  d a y , reactors A and B produced only 0.23 and 0.28 liter CH liter  (Table 4.2).  -1  0  4  -1  day  -1  Despite the contrast in volumetric methane production between reactors  of the two parties, the methane yield numbers were very close to one another.  In  effect, this observation implies that the theoretical treatment efficiencies in terms of methane yield were the same for the two different sets of reactors utilizing two drastically different wastewaters.  The author did not find literature which specifically  dealt with baker's yeast wastewater treatment during start-up in U A S B reactors which was based on comparable loading regimes.  4)  Volatile Suspended Solids V S S information is useful in that it gives an indication of the concentration of  sludge in the sample being examined.  V S S , however, makes no distinction between  living and dead bacteria. It is beyond the scope of this study to make such distinction. Figure 4.8 depicts the effluent V S S over the entire start-up in which the influent V S S  6  stayed relatively constant at 1.5 g liter . The reactors started off with -1  a V S S concentration in the neighborhood of 0.5 g liter . Next, these initially low V S S -1  6  Both VSS and VS concentrations (g liter ) are based on the the assumption that the density of the sample is near that of water. -1  36  values began to rise and soon (between day 10 and 15) gave way to abrupt peaks of 2.9 and 3.1 g liter for reactors A and B respectively. After the peaks subsided on -1  day 15, VSS levels essentially remained below 0.5 g liter until the close of the start-1  up period. The steady-state VSS values were marginally different: 0.3 and 0.2 g liter , A and B respectively. -1  The VSS behaviors of the two reactors were found to be similar. During the period of start-up, the seeded sludge was allowed to multiply as much as possible. As the sludge concentration increased in the reactor, higher flotation due to increasing gas production was responsible for the lifting and expansion of the sludge bed, and the associated excessive sludge washout especially between days 10 and 15. However, as the bacteria began to adapt to the reactor environment, the expanded sludge bed gradually became compacted leading to less and less sludge washout (Barford, 1988; Wu et al, 1985). The excessive sludge loss common in both reactors was also reflected in Figure 4.9. In the course of the first 10 days, VS levels were consistently higher than that of 7  the feed (6.9 g liter ), implying abundant sludge washout, on which Figures 4.4 -1  through 4.9 agreed. Behaving in an manner opposite to that of COD reduction, the VS graph goes from high to low, the slope of the graph gradually diminishing to about nil (i.e., flat) by day 40. This pattern makes good sense because the consistent lowering of VS implies a continuous growth of the bacterial population, its adaptation to the reactor environment, and its increasing fermentation activity.  Finally, the  establishment of a reasonably stable flat platform in VS signalled the completion of the start-up period. The steady-state VS concentrations were 3.1 and 2.8 g liter , A and -1  B respectively.  VS is total volatile solids, which consists of two components: dissolved and suspended (i.e., VSS).  VOLATILE SUSPENDED SOLIDS  FIGURE  4.8: V o l a t i l e Suspended S o l i d s v e r s u s Time  oo  VOLATILE SOLIDS  ~> 15  FIGURE  1 20  1 —i 25 30 TIME (DAY)  1 35  •  Reoctor A  •  Reactor B  1 40  4 . 9 : V o l a t i l e S o l i d s v e r s u s Time  1 45  -i 50  39  From the vantage point of effluent V S S and V S (Figures 4.8 and 4.9), there was no significant difference between the two reactors before and during the steadystate was established, even though undeniably better performance on reactor B's part was evident in effluent C O D , effluent C O D reduction, and methane yield (Figures 4.2 through 4.7).  5)  Volatile Fatty Acids, p H , and P / A Ratio Figures 4.10 and 4.11 indicate that both reactors began with very high effluent  V F A concentrations in the form of acetic, propionic, iso-butyric, and butyric acids. However, as the biomass grew in concentration leading to increasing digestion activity, these V F A ' s were digested in accordingly greater proportions. Thus, the overall V F A behavior was the consistent lowering of all four V F A ' s throughout the first forty days. From day 42 onward, though, all effluent V F A levels from both reactors were found to converge to their respective steady-state concentrations.  Except that isobutyric and  butyric acids were zero in concentration for both reactors, the respective acetic and propionic acid concentrations for A and B were 61 and 48 mg liter , and 44 and 10 mg -1  liter . -1  In addition, during the steady-state, the propionic acid concentration went lower than that of the acetic acid, and p H rose to between 7.5 and 8.0 (Figure 4.12). Less obvious is that reactor B's V F A levels reached stable conditions  more quickly  reactor A ; that is, by day 35, reactor B's V F A levels were already below 200 mg liter , whereas the same would not happen for reactor A until after 40 days. -1  This  difference can be verified more easily from Figure 4.13 which is the time profile of propionic-to-acetic-acid (P/A) ratio.  As mentioned in the literature review chapter, a  P/A ratio of 1.4 or higher means that the anaerobic process is under stress.  Here  reactor B had its peak at day 22 whereas reactor A reached its peak at day 35.  VOLATILE FATTY ACIDS (Reactor A) -i  1800  1600 4  •  ocetlc  •  propionic  #  Isobutyric  O butyric _  1400-  1200-  1000-  if  >  < CC  800-  O  d <  bJ  600-  CC  400  H  200  A  / v. 20  25  30  35  40  45  50  TIME (DAY)  FIGURE  4.10: V o l a t i l e F a t t y A c i d s v e r s u s Time f o r R e a c t o r A  o  VOLATILE FATTY ACIDS (Reactor B) UOO-i  1200  A  1000-  •  acetic  •  propionic  9  isobutyric  O  butyric  O) £  800-  > CD CC  600-  o ^  400-  \ \  2004  20  25  TIME (DAY)  FIGURE  30  35  40  45  4.11: V o l a t i l e F a t t y A c i d s v e r s u s Time f o r R e a c t o r B  50  EFFLUENT pH  -r 10 -  •  Reoctor A  •  Reactor B  -r 45 -  15  20  FIGURE  25 30 TIME (DAY)  35  4.12: E f f l u e n t pH  40  50  PROPIONIC-ACETIC RATIO  TIME (DAY)  FIGURE  4.13:  Effluent. Propionic-to-acetic  Ratio  44  Reactor B's ability to reach stability more quickly than reactor A can be attributed to positive effects owing to the installation of ropes in reactor B.  B . Chapter Conclusion The important findings and conclusions of the start-up period are presented below: •  The steady-state for the start-up period was reached around day 43 and extended to day 46, the end of the start-up.  •  As indicated by Figures 4.2 to 4.9, the first ten to fifteen days of the start-up were characterized by excessive sludge washout because there was enough washed-out sludge in the effluent to offset the C O D removed by the bacteria. As microorganisms multiplied and as sludge settleability improved, a negativeto-positive turnover in COD removal was experienced by each reactor.  •  It was found that, under similar start-up loading conditions, similar methane yields  (utilization  efficiencies)  could  be  obtained  from  vastly  wastewaters like baker's yeast wastewater and cheese whey.  different  In particular,  methane yield values of 0.34 and 0.33 (at organic loading rates of 1.11 and 1.27 g C O D liter  -1  day ) were achieved in reactors A and B respectively; at -1  similar organic loading rates (0.91 and 1.97 g C O D liter  -1  day ), Yan et al. -1  (1989a) obtained comparable methane yields of 0.30 and 0.33 with a U A S B reactor treating cheese whey at 3 5 ° C . •  With regard to the goals of the start-up period, the performance of each reactor can be determined by evaluating the following: 1) How quickly the reactor recovered from excessive sludge washout (timing of turnover); 2)  •  How soon the reactor reached steady-state.  The advantage of reactor B's fixed-medium in the form of ropes was evident in that, with regard to the Figures 4.1 through 4.9, the negative-to-positive turnover in reactor B always took place sooner than in reactor A .  •  The figures in the "START-UP"  show that, while the two reactors  often  displayed a similar behavior pattern, reactor B invariably reached steady-state  45 more quickly than reactor A. Furthermore, in the course of the start-up period, reactor B was nearly always better than reactor A with respect to methane composition, effluent COD, COD removal, methane yield, effluent VSS and VS, pH, and effluent VFA. •  In some instances, reactor B's steady-state values were not as dramatically different from those of reactor A as had been hoped. An important reason could well be that there had not been enough time for a significantly large amount of biomass to attach to the ropes in reactor B. According to Lo and Liao (1984), it takes 3 to 6 months for biomass to develop on a fixed medium such as acrylic panels. Therefore over a longer period of time, further down the experiment, more substantial advantage in performance should be expected in reactor B.  •  Even though raw baker's yeast wastewater contains a high concentration of sulfate (1,700 to 3,200 mg liter ), and even though a run of the same reactors utilizing feed with sulfate removed was not conducted, loss of treatment efficiency in both reactors was believed to be relatively low due to the following reasons: (1) the pH values of the two reactors were rather near the optimum pH range of 7.5 to 8.0 (Sarner et al., 1988); (2) the COD/S0 = ratio of the feed (over 50 g g ) has always been above 10 g g , which means that natural gas stripping of H S was sufficient to keep H S toxicity down (Lettinga et al., 1985); (3) the seed sludge had already been acclimated to the wastewater prior to being used to seed the reactors; (4) the feed concentration during the start-up period was low (8.0 g COD liter ), which also helped alleviate the sulfate problem (Lettinga et al., 1985). -1  4  -1  -1  2  2  -1  46  V. STEP-UP OPERATION During the start-up period, the sludge in the reactors was allowed to grow and adapt to the system environment. After the start-up, the reactors were ready to take in feed at higher strengths. This new phase of experimentation began in early March of 1988 and terminated at the end of October of the same year. Feed strength was increased stepwise (and hence the name "STEP-UP OPERATION") from about 8 to 58 g COD liter- ; the major step-up feed concentrations 1  were 18, 25, 30, 35, 40, 45, 50, 55, 58 g COD liter- . As indicated earlier, the start1  up feed strength was set at 8 g COD liter . After the start-up, instead of raising feed -1  strength abruptly to, say, 40 g COD liter , a gradual increase was adopted for the -1  following reasons: •  The reactors immediately after the start-up period were specially sensitive to environmental factors such as the organic loading rate. An excessively high organic loading rate would cause too much buoyancy due to the produced biogas and result in a high rate of sludge washout. At this stage of the experiment, special care must be taken to minimize sludge washout; otherwise, stable conditions might be unduly delayed or never reached (Barford, 1988; Wu et al., 1985).  •  The stepwise feed strength increase not only allowed the microorganisms to accustom themselves to the new environment, but also permitted a full view of the performance profile of the reactors over the entire range of the operational settings. Moreover, the researcher had the advantage of locating the optimum setting as well as observing the transient response of the system to the change of the operational parameters. In the case of locating the optimumperformance point, if the feed strength increment was too great, the optimum point might very well fall in the middle of the increment interval; then either the researcher would not be able to detect the presence of such an optimum point, or it would be very hard to determine with reasonable accuracy the specifics of the optimum setting. If in fact an optimum point had been missed, attempt to run the reactors "backwards" (i.e., to run them at a lower feed strength) would most likely not lead to the optimum point of interest because of the phenomenon called hyteresis. Hyteresis is explained in greater detail in a later section, but for now it suffices to say that, in the context of this study, the  47 pathway along which the reactor was operated during the step-up operation would often be different from the pathway followed when the reactor was run with decreasing (step-down) feed strength. A . Results and Discussions •1) Steady-state and Transient Analysis The steady-state definition for the step-up operation period differs from that of the start-up period. Whereas steady state in the start-up period represented the time span in which system parameter variations were within 10%, the steady-state value of a system parameter (e.g., methane composition) in the step-up period was defined as the arithmetic mean of that parameter over the time period in which the operating conditions were kept constant and the reactors were fed with the same batch of feed (that is, same organic loading rate). An average parameter value calculated in this fashion was considered to yield a reasonable steady-state value since a perfectly "horizontal" steady-state would be most unlikely in the UASB reactor, where the amount of sludge and its activity are constantly changing and more dynamic than in batch reactors. For the transient analysis, because of the large number of data points collected in the experiment, it was felt best to work with the constant-organic-loading averages obtained by the method outlined above. (For completeness' sake, however, two sample time plots depicting every data point can be found in Figure 5.0.)  Therefore, the  transient analysis presented in this study was actually based on points which were themselves averages. The effect of this practice was that day-to-day variation within any given constant-loading period was no longer visible.  In effect the transient  analysis was depicting the transient behavior of individual constant-loading averages over the experiment time domain. One would think that there was not much of a difference between the steady-state and transient analyses. However, a fundamental  BIOGAS METHANE COMPOSITION TIME PLOT SO-i  O O CD  i0-\ 0  1 SO  1 100  1 150  ,  ,  ,  200  290  300  TIME (DAY)  BIOGAS METHANE COMPOSITION TIME PLOT »6-i  ME (DAY)  Figure 5.0: Time plot of step-up operation methane composition of reactors A and B  49  difference did exist between the two analyses. The steady-state analysis focused on the average values of the parameters of interest in relation to organic loading rates, since all other parameters were kept constant. The transient analysis, in contrast, was interested in the trend of the same averages in relation to the experiment time. The steady-state and transient results in terms of biogas methane composition (% by volume), methane production (liter CH liter day ), effluent COD (g COD -1  -1  4  liter ), COD reduction (%), and methane yield (liter C H g -1  4  -1  COD day ) are 1  summarized in Table 5.1 and depicted in Figures 5.1 and 5.2. Table 5.1 presents the data chronologically, from day 47 (which is the first day following the end of the startup period) to day 268 which marks the beginning of the last constant-loading period of the entire experiment. Figure 5.1 is based on organic loading rates (g COD liter  -1  day ) sorted in the ascending order, and Figure 5.2 on days of the experiment as the x -1  axis.  All the values used are arithmetic averages for individual constant-loading  periods.  a) Biogas Methane Composition As can be seen in Figure 5.1a, the two reactors displayed a descending pattern in biogas methane composition.  This pattern is in keeping with the fact that, in  general, the biogas methane composition tends to fall with increasing organic loading. Both reactors started out with a methane composition of around 53% (volume basis) at an organic loading rate of 2.3 g COD liter day . -1  -1  However, at organic  loading rates higher than 6 g COD liter day , reactor A's methane composition -1  -1  oscillated around 45% while reactor B's was around 49%. In other words, whereas reactor A experienced a significant drop in methane composition (53% down to 45%), reactor B's methane composition went through little decrease. Furthermore, reactor A's methane composition fluctuated much more than that of reactor B. Reactor B's  EFFLUENT COD  BIOGAS METHANE COMPOSITION •  REACTOR A  •  REACTOR B  50  60  60  fr?  »- 40H  50  O  C/1  O U  O  % *0-\  20  o o  30  c  »  1  2  10  LOADING (g COD l i t e r " day" )  r6  ~l  1  8  10  (a)  (d)  METHANE PRODUCTION  TOTAL COD REDUCTION 80  1.5-,  O XI  z i— o  60  g  O)  40  or  0.5H  o  4  O  O  20  O  -i  8  1  6  10  10  (e)  (b)  METHANE YIELD (COD DESTROYED)  INFLUENT COD 60-, | »_ <P  Q O  <-> O)  40  .If JBR  0.8 0.6  0.4  H  X  20  o  0.2  o  - i — i 8  - 1  10  10  (f) (c) FIGURE 5.1: T r e a t m e n t E f f i c i e n c y v e r s u s O r g a n i c L o a d i n g  TOTAL COD REDUCTION  BIOGAS METHANE COMPOSITION • REACTOR A O REACTOR B  60  80-i  •  REACTOR A  •  REACTOR B  z 60 o i— o 40 3  50H  O UJ  40H  on  Q O CJ  30  100  200  20  fa  300  100  TIME (day)  200  300  (d)  (a)  METHANE YIELD (COD DESTROYED)  METHANE PRODUCTION 1.5-1  | 0.8 Q O O '<* X CJ  o.sA  L.  —I  100  1  1  200  300  0.6 0.4 1-f  •  0.2H  100  (b)  200  300  (e)  EFFLUENT COD  ORGANIC LOADING  60  10  cT 8  40  -o £  20  o  3  100  FIGURE  8 200  (c)  6H  300  4-  N100  (f) 5.2: T r e a t m e n t E f f i c i e n c y v e r s u s T i me  200  300  52  stability was believed to be due to the installed fixed-film structure (Lo et al., 1984; Vega et al, 1988).  T A B L E 5.1: Step-up operation treatment efficiency  51  Day Feed  Effluent COD average COD Reduction C H % 4  B 47 60 74 80 94 102 113 127 139 153 165 178 187 202 211 220 237 260 268  18.6 20.9 19.1 33.1 34.1 33.8 32.8 25.6 40.6 37.2 43.6 43.6 43.6 45.3 56.5 52.1 52.9 57.8 55.5  5.5 7.8 8.3 10.8 12.7 13.5 13.3 12.0 13.6 21.1 26.0 38.3 34.0 30.0 27.9 30.4 33.1 40.6 43.4  B  5.6 70.7 70.0 7.7 62.8 62.9 7.9 56.8 58.8 10.0 67.3 69.6 12.1 62.7 64.6 12.8 59.9 62.3 13.5 59.5 58.9 12.0 53.1 53.3 12.1 66.5 70.3 16.3 43.2 56.1 25.1 40.2 42.3 20.9 12.0 52.1 28.8 21.9 33.8 23.6 33.9 47.8 25.7 50.6 54.5 30.3 41.6 41.8 41.4 37.4 21.6 45.7 29.7 20.9 42.0 21.7 24.3  B 53.1 52.7 51.5 49.4 49.2 51.8 52.7 54.2 53.2 52.3 47.8 36.7 42.9 44.7 44.2 46.6 43.2 45.3 45.8  51.1 51.6 52.9 49.3 48.9 50.4 51.7 52.9 52.1 50.5 49.1 48.9 49.0 49.5 50.1 48.1 47.0 47.3 48.8  Organic Methane Yield Loading Production COD Added B  B  B  0.44 0.46 0.44 0.58 0.75 0.89 0.85 0.73 0.81 0.92 0.95 0.83 0.90 1.12 1.05 1.11 0.85 0.92 0.91  2.3 2.6 0.36 2.6 2.8 0.42 2.7 2.3 0.49 4.1 3.6 0.66 5.8 4.8 0.91 5.2 5.6 0.84 4.3 5.0 0.71 3.6 4.3 0.61 5.6 5.7 0.82 4.8 5.9 0.88 5.9 6.4 0.76 6.2 6.0 0.33 6.6 5.8 0.60 9.4 8.3 0.70 9.1 8.5 0.56 6.2 6.8 0.65 4.8 5.2 0.52 8.3 8.0 0.66 7.8 9.1 0.63  Yield COD Dest A  0.16 0.17 0.16 0.17 0.18 0.19 0.16 0.16 0.16 0.16 0.16 0.16 0.16 0.17 0.17 0.17 0.15 0.15 0.19 0.16 0.13 0.15 0.06 0.14 0.09 0.16 0.08 0.14 0.07 0.13 0.12 0.16 0.11 0.17 0.08 0.11 0.10 0.11  0.24 0.26 0.32 0.24 0.26 0.27 0.28 0.33 0.23 0.43 0.26 0.27 0.45 0.25 0.14 0.26 0.31 0.29 0.43  B 0.26 0.26 0.33 0.23 0.25 0.26 0.29 0.32 0.21 0.29 0.34 0.27 0.43 0.29 0.24 0.41 0.81 0.55 0.49  * Feed and effluent COD expressed in g liter ; COD reduction and methane composition in %; organic loading in g COD liter- day- ; methane production in liter C H liter- day- ; yields in liter C H g- COD day- , either added or destroyed. -1  1  1  1  4  1  1  1  4  The maximum biogas methane composition obtained in the step-up operation phase was 54% (at an organic loading rate of 3.6 g COD liter  -1  day ) and was -1  comparable with that reported by Frostell (1982) who achieved a maximum biogas methane composition of 56% (at an organic loading rate of 22 g COD liter day ) from -1  -1  a laboratory-scale continuously fed anaerobic fluidized bed reactor treating baker's yeast wastewater at 30°C.  Lo et al. (1989), using an anaerobic rotating biological  contactor (ARBC) reactor with an active biomass, achieved a maximum methane composition of 48% at a loading rate of 9.2 g COD liter day . As indicated earlier, -1  -1  53  the maximum methane composition achieved in the start-up period was 59% (at an organic loading rate of 1.1 g COD liter- day ). These figures seem to suggest that 1  1  the maximum biogas methane composition achievable with baker's yeast wastewater is 60%. Based on the actual experiment time, Figure 5.2a shows the transient behavior of the reactors. It can be seen that both reactors oscillated around 50% of methane content for the first 165 days. Thereafter, each reactor took on a different pattern: reactor B's methane composition experienced a slight global drop while going through some local mild oscillation; reactor A, however, began to go down a deep valley and would not start to recover partially until after day 178. It is clear that, as the organic loading began to rise, the increasing stress on the reactors also began to be reflected in the lowering of methane composition, especially after day 168. In particular, when the organic loading rate rose to about 6 g COD liter- day- (day 168), the fixed-medium in 1  1  reactor B started to prove advantageous.  b) Volumetric Methane Production For the same organic loading range of 2.3 to 9.4 g COD liter day , reactor -1  -1  A's methane production rate (based on standard temperature and pressure, STP, 0°C and one atmosphere) ranged between 0.34 and 0.91 liter CH liter- day while that of 1  1  4  reactor B ranged between 0.44 and 1.12 liter CH liter day (Figure 5.1b). -1  -1  4  Based on methane production over the entire experiment, reactor B definitely was better than reactor A. Reactor A's methane production rate rose from 0.36 liter CH liter day at the loading of 2.3 g COD liter day and attained its maximum of -1  -1  -1  -1  4  0.91 liter CH liter day at the loading of 5.8 g COD liter day ; then it dropped -1  1  -1  1  4  abruptly and stayed at around 0.7 liter CH liter day . Unlike reactor A, reactor B's -1  1  4  methane production curve was essentially ascending throughout the whole organic  54  loading range. The maximum methane production rate achieved by reactor B was 1.12 liter CH liter- day at the loading of 8.3 g COD liter- day . 1  1  1  1  4  Obviously,  reactor A had already achieved its maximum volumetric gas production at an organic loading rate (5.8 g COD liter- day ) which was still far from the highest loading rate 1  1  (9.4 g COD liter- day ) imposed in this study. Reactor B, however, did not appear to 1  1  have reached its highest-possible gas production even at the maximum loading applied to it (9.1 g COD liter day ) since it is not clear whether the curve would drop or -1  1  continue to rise. Higher organic loading rates would have to be applied to determine the organic loading rate above which reactor B's gas production would begin to decrease.  Furthermore, whereas reactor A's methane production rate fluctuated  sharply between the loading range of 4 and 7 g COD liter day , reactor B's was -1  1  rather smooth. Only for loading rates higher than 7 g COD liter- day did reactor B 1  1  experience some bumpiness in methane production. The methane production rate trend in Figure 5.2b, aside from the difference in value between the two reactors, is consistent with the fact that methane production rate follows the organic loading rate closely. That is, the methane production rate rises as the loading rises, and vice versa. The exception is the deep valley in reactor A's gas production curve, which represents that period of time (the bottom of the valley is located at day 178 in Figure 5.2b) when rector A is still in the process of adapting to the new higher organic loading rate (6 g COD liter day ). Evidently, the -1  1  additional biomass clung to the ropes enhanced reactor B's biogas production, both quantitatively and qualitatively, and at the same time rendered reactor B more tolerant to organic loading rates higher than 6 g COD liter day . -1  1  By comparison, an ARBC reactor treating baker's yeast wastewater at 35 °C produced only 0.61 liter CH liter day at a comparable loading of 6.5 g COD liter -1  1  -1  4  day (Lo et al, 1988). At a loading of 9.2 g COD liter- day , the same ARBC 1  1  1  55  reactor produced 1.17 liter CH liter day (Lo et al., 1989), as compared to 0.70 and -1  -1  4  0.91 liter CH liter day for reactors A and B respectively at a similar loading. The -1  -1  4  better gas production by reactors A and B at the intermediate loading rates is largely due to the fact that the UASB reactor is able to retain sludge that would otherwise be lost in the effluent, and to minimize the negative effects of shock loading by virtue of continuous feeding. (Bacteria have more time to assimilate the incoming feed when it is continuous rather than batch feeding. It appears that digestion efficiency is higher when continuous feeding is employed dash— Kennedy and van den Berg, 1982.) At loading rates over 9 g COD liter day , both reactors' gas production rates were less -1  -1  than that achieved by the ARBC reactor. A possible explanation is that the ARBC reactor had the advantage possessing a bacteria population that had already been well established prior to the experiment, whereas reactors A and B were being run for the first time and were under much loading stress. Sayed et al. (1987) treated slaughterhouse wastewater using a granular sludge UASB reactor run at 30°C. The wastewater contained 40-50% of coarse suspended matter and a COD-to-BOD ratio of 3 to 4, which was comparable with that of baker's yeast wastewater. At a loading of 6.4 g COD liter day , a methane production rate -1  -1  of 1.11 liter CH liter day was achieved, as compared with 0.9 liter CH liter -1  -1  4  day  -1  4  attained by reactors A and B at 5.8 g COD liter day . While Sayed's result  -1  -1  -1  was relatively close to that achieved by reactors A and B at the loading of about 6 g COD liter day , at an organic loading rate of approximately 10.0 g COD liter -1  -1  -1  day , however, the methane production rate achieved by Sayed's reactor was 1.5 liter -1  CH liter day , much higher than those of reactors A and B ( 0.70 and 0.91 liter -1  1  4  CH liter day respectively). -1  4  -1  Some possible explanations follow.  First, granular  sludge, being more active than the mostly muddy sludge observed in reactors A and B, led to a higher gas output. Second, while similar organic loading rates were applied,  56  the wastewater used in this study was much more concentrated in COD than that of the wastewater treated by Sayed— 8 to 58 g COD liter as compared to 1.5 to 2.2 g -1  COD liter . The UASB reactor is normally used to treat wastewaters of rather low -1  COD concentrations (typically between 1 and 20 g COD liter ), such as municipal -1  sewage wastewater and sugar-beet sap at relatively high hydraulic loading rates (Lettinga et al., 1980 and 1985). Moreover, as mentioned in the literature review chapter, the UASB reactor requires a certain selection pressure (in the form of controlled high hydraulic loading) so as to drive out less healthy sludge and reserve more available nutrient for the larger sludge aggregates to grow more rapidly (Wu et al., 1985; Lettinga et al., 1985). Conceivably, Sayed's better results might be due to a better selection pressure obtained through more vigorous hydraulic loading rates. In this study, however, it has been stated earlier that ensuring stable operation and achieving truly continuous feeding (twenty-four hours a day, seven days a week) to minimize loading shock were the reasons for the relatively low hydraulic loading rate applied throughout the entire experiment (2.0 to 2.5 liter of feed per day).  c) COD Reduction Reactors A and B displayed the same diminishing general trend in COD reduction as indicated by Figures 5.1e and 5.2d.  The overall pattern for the two  reactors is again within expectation: COD removal deteriorates with rising organic loading. It is worth noting that, while reactor B achieved more removal than reactor A from days 139 to 220, the scenario reversed towards the higher end of organic loading (i.e., 8 g COD liter day -1  -1  and up).  In this high loading range, relatively large  amounts of washed-out sludge were observed for reactor B— though to a lesser extent than for reactor A. This excessive sludge washout is thought to be the same sludge  57  washout phenomenon that reactor A had experienced earlier (beginning from day 150); only it is a "lagged" one in the case of reactor B. A careful examination of COD reduction and volumetric gas production shed more light on the time lag observed in reactor B. Figure 5.2b shows that following day 150, reactor A's gas production dropped considerably, but reactor B's gas production climbed drastically in relation to reactor A and amounted to over 1.0 liter CH liter  -1  4  day by day 220. In this experiment, Flotation, and not turbulence, was thought to be -1  the main mechanism responsible for the buoyancy of sludge floes.  Higher gas  production means more flotation of the sludge due to gas bubbles, which results in a higher sludge loss rate (Lettinga et al., 1980 and 1985). Thus, reactor A's drop in gas production effected a lowering in sludge washout (relative to before day 150); in contrast, reactor B experienced a surge of gas production which obviously caused the excessive sludge loss in reactor B. Since baker's yeast wastewater is rather slow to biodegrade, as indicated by its high COD-BOD ratio, the maximum COD reduction achieved in this study (71% at 2.3 g COD liter day ) was still low compared to that of more readily biodegradable -1  -1  wastewaters such as cheese whey, which is very readily biodegradable (Yan et al., 1989a). However, at organic loading rates higher than 6 g COD liter day (after -1  -1  day 150), COD reduction fell below 50% for both reactors; single-stage treatment at this efficiency in this loading range was considered rather unattractive.  Higher  dilution of the original wastewater, recycle of the effluent, and/or longer retention time would be required to achieve desired COD removal.  d) Methane Yield From Figure 5. If, up to organic loading rates of 6 g COD liter— day , the 1  -1  methane yield (based on COD destroyed) for both reactors was mostly bracketed in the  58  range of 0.25 to 0.35 liter CH g COD day . At loading rates higher than 6 g COD -1  1  4  liter day reactor A's methane yield oscillated between 0.15 and 0.45 liter CH g -1  1  -1  4  COD day whereas reactor B's between 0.25 and 0.50 liter CH g- COD day . 1  1  1  4  Clearly, as organic loading increased, contribution to methane yield from reactor B's fixed-medium also began to stand out. Time-wise, the methane yield looked essentially the same for the two reactors for up to day 200 (Figure 5.2e).  After this time, the two reactors began to  differentiate between themselves. Reactor A went through a slight valley and then levelled off towards the end of the experiment.  As to reactor B, instead of going  through a valley as reactor A, it reached a methane yield of 0.81 liter CH g- COD 1  4  day ; then it subsided and nearly merged with reactor A at the very end. 1  By comparison, also treating baker's yeast wastewater form the same source, Lo et al. (1989) reported a methane yield of 0.28 liter CH g COD day at a loading -1  1  4  of 9.1 g COD liter- day . At similar loading rates of 9.4 and 8.3 g COD liter- day 1  1  1  1  (taken from the period starting at day 202), the two reactors achieved methane yields of 0.25 and 0.29 liter CH g- COD day respectively. 1  1  4  Clearly, whereas reactor A  proved to be no better than Lo's batch reactor, the biomass support system indeed had a positive impact on reactor B's methane yield. Furthermore, Yan et al. (1989a), treating cheese whey in a UASB using a similar setup and operating conditions, observed rather consistent methane yield of0.30to0.34 liter CH g COD day for a -1  1  4  loading range of 0.91 to 7.77 g COD liter day . By and large, the results obtained in -1  1  this study were comparable with those of Yan et al. (1989a)— even though cheese whey and baker's yeast wastewater are rather different in nature.  59  e) Volatile Fatty Acids The well-being of the anaerobic reactor can largely be explained by its VFA levels. Therefore by closely following the VFA concentrations of the reactor, one can determine whether digestion is proceeding smoothly or process failure is imminent. As indicated in the "LITERATURE REVIEW", TVFA greater than 2000 mg liter- , acetic 1  acid higher than 800 mg liter , and a P/A ratio greater than 1.4 were reliable methods -1  of predicting the failure of anaerobic process.  Of these criteria, the combination of  acetic acid and the propionic-to-acetic-acid ratio provides the best index for digestion failure prediction. Additionally, long-chain VFA's, butyric and iso-butyric acids, also give useful indication as to the extent of stress an anaerobic reactor is under. Isobutyric acid levels of 5, 5-15, above 15 mg liter  -1  indicate that the reactor is,  respectively, under little or no stress, under much stress and near failure, is failing. VFA data are summarized in Table 5.2.  Up until day 165, TVFA for both  reactors remained below 500 mg liter (Figure 5.3a). From day 165 onward, TVFA -1  levels rose rapidly, especially for reactor A. By day 187 reactor A's TVFA had already gone beyond the 2,000 mg liter level, never to subside again; eventually it -1  exceeded 4,000 mg liter . Reactor B, however, always stayed below the 2,000 mg -1  liter mark throughout the experiment, except towards the very end when the TVFA -1  amounted to 2,500 mg liter . With particular reference to the TVFA failure criterion -1  alone, the following points can be drawn: •  The first 165 days were a period in which both reactors were under little, if any, stress.  •  During the subsequent period, from days 165 to 187, increasing stress on both reactors, especially A, manifested in the form of steep TVFA increase.  •  From day 187 to the end of the experiment was the final period, in which failure began to set in for reactor A which was now characterized by TVFA concentrations well beyond 2000 mg liter and low treatment efficiency. -1  60  TOTAL VFA ^ _ 6000-1  ISOBUTYRIC ACID •  REACTOR A  O  REACTOR B  ^  200-1  £ 4000-1  z  O  O  < j* 2000-  V  '00  OC  o z o o  o z o o  00 200 TIME (DAY)  .  100  (a)  200  H  300  (d)  ACETIC ACID  BUTYRIC ACID  o»  E. z o  IOOO  <  O  z  o o  0+ 0  100  (b)  300  200  PROPIONIC ACID  P/A RATIO  sooo  £  300  4-1  2000-1  •  z  •  VP  o iooo-|  ui o z o 100  200  2H  300  —I  100  1  200  (c) (f) FIGURE 5 . 3 : V o l a t i l e F a t t y A c i d s v e r s u s Time  1  300  61 Reactor B, however, was under a lot of stress but never did approach the point of failure until after day 267. Figure 5.3b shows that, except after day 267, the acetic acid levels of the two reactors were virtually always under 800 mg liter . If failure prediction was solely -1  based on the failure criterion of acetic acid, then the implication was that failure would not come to any of the reactors until after day 267. However, this statement is not in harmony with the preceding discussion on TVFA. The other failure criteria have to be checked before it is possible to make any valid conclusions.  T A B L E 5.2: Volatile fatty acids of the step-up operation Day  Acetic A  47 60 74 80 94 102 113 127 139 153 165 178 187 202 211 220 237 260 267 1  2  118 130 212 215 224 156 56 28 57 106 111 240 806 582 593 482 526 647 1839  1  Propionic Isobutyric  B 96 127 207 225 180 115 72 49 66 87 107 172 566 694 534 384 689 622  A B 26 34 105 54 200 138 138 59 74 49 127 135 22 75 13 31 49 54 127 219 209 189 640 278 1329 363 2045 746 1719 480 1469 581 1119 927 1498 850 945 20551306  A 0 0 3 7 5 10 0 0 1 4  B 0 0 0 3 1 4 2 0 3 10 11 9 54 29 158 26 130 41 115 20 111 20 84 20 8 123 180 166  Butyric A 2 2 0 8 5 18 16 3 1 12 8 183 340 176 51 49 61 197 366  B 0 0 0 4 2 14 2 1 3 9 15 86 61 87 17 38 137 111 101  TVFA A B 146 130 237 181 415 345 368 291 309 232 310 268 94 150 44 81 107 126 248 324 338 322 1117 566 2633 1016 2933 1568 2478 1051 2112 1022 1791 1774 2465 1592 4441 2517  P/A A 0.2 0.8 0.9 0.6 0.3 0.8 0.4 0.5 0.9 1.2 1.9 2.7 1.6 3.5 2.9 3.0 2.1 2.3 1.1  Loading B  0.3 0.4 0.7 0.3 0.3 1.2 1.0 0.6 0.8 2.5 1.8 1.6 0.6 1.1 0.9 1.5 1.3 1.4 1.4  A  2  B  2.3 2.6 2.6 2.8 2.7 2.3 4.1 3.6 5.8 4.8 5.2 5.6 4.3 5.0 3.6 4.3 5.6 5.7 4.8 5.9 5.9 6.4 6.2 6.0 6.6 5.8 9.4 8.3 9.1 8.5 6.2 6.8 4.8 5.2 8.3 8.0 7.8 9.1  All VFA's expressed in mg liter . Units: g COD liter day . -1  -1  -1  The P/A ratio is defined as the ratio of propionic and acetic acids, which are shown in Figures 5.3b, 5.3c, and 5.3f.  Before day 153, P/A ratios for both reactors  were by and large under 1.4. Thereafter, as stress built up, the P/A ratio of reactor A  62  always stayed greater than 1.4. Unlike reactor A, after day 153, reactor B's P/A ratio consistently remained below 1.4 until the termination of the study— though it is rather near 1.4.  Based on the P/A ratio alone, it can be said that, after day 153,  reactor A was under much stress and failure very likely started to set in sometime after day 187— as evidenced by reactor A's ever-increasing P/A ratio (Figure 5.3f). As to reactor B, it never did reach failure because its P/A ratio always under 1.4. Always found in much smaller concentrations than acetic and propionic acids, iso-butyric and butyric acids provide additional information concerning digestion failure.  Since Hill et al. (1987 and 1988) showed that the iso-forms of long-chain  VFA's are particularly useful, the discussion will center around iso-butyric acid (Figure 5.3d); the butyric acid graph (Figure 5.3e) is included here for completeness' sake. The butyric acid levels of the two reactors were mostly below 10 mg liter up to day 165; -1  thereafter, however, it sky-rocketed abruptly, especially for reactor A, to well above the 5-15 mg liter criterion range. Based on the iso-butyric failure criterion, reactor A -1  was well into failure after day 187. Meanwhile, reactor B was just marginally over the 15 mg liter mark in iso-butyric acid, declining slightly towards the end of the -1  experiment. Except after day 267 when the iso-butyric acid went up to 166 mg liter , -1  it is felt that reactor B did not really fail in spite of its iso-butyric acid levels being greater than 15 mg liter . Reactor B was on the "border line". -1  After examining each failure criterion, some conclusions may now be drawn: •  All failure criteria pointed to the same conclusion: the first 153 days of the experiment were marked by stability (low concentrations for all VFA's) which is also confirmed by Figures 5.1 and 5.2 in the previous sections.  •  Except for the acetic failure criterion, all other criteria agreed that, sometime after day 153 and before day 165, stress levels began to increase drastically for both reactors— especially rector A. In the case of the acetic acid, it is conceivable that this acetic acid criterion value (800 mg liter ) varies from waste to waste, and from system to system. In this study, Figure 5.3b -1  63 suggests that the failure acetic acid level could be somewhere below 800 mg liter , possibly around 500 mg liter . If this speculation were true, then it would be hard to explained the reason why there was practically no difference between the two reactors from days 187 to 267. -1  •  -1  Again, except for acetic acid, all criteria indicated that failure began to set in for reactor A after day 187; reactor A's VFA levels exceeded all failure criterion values. For reactor B, all VFA concentrations were lower than the failure criterion values. The exception was iso-butyric acid; it slightly exceeded the criterion value between days 165 and 267. In addition, reactor B's isobutyric acid reached a high of 166 mg liter at the very end. The marginally high iso-butyric levels and the single peak at day 267 (166 mg liter ) were not evidence enough to substantiate the failure of reactor B— since all other failure criteria had not been exceeded. Thus, the best conclusion would be that, after day 165, reactor B experienced much stress and approached failure towards the end of the experiment. -1  -1  •  In summary, the VFA results showed that reactor B performed better than reactor A. As of now, all that can be said about the reason of such superiority on reactor B's part is that the combined (or total) bacterial activity of reactor B was higher than that of reactor A; a look at the reactor's behavior along the height of the reactor (i.e., profile study) will shed further light not only on the performance of each individual reactor but the reason for the difference between them. f)  Sulfate  Toxicity  The raw baker's yeast wastewater used in the experiment contained a high concentration of sulfate (1,700 to 3,200 mg liter ) which encourages sulfate-utilizing -1  bacteria to flourish, competing with methanogens for the same energy sources which are needed in the formation of methane.  Sulfate in wastewater, therefore, tends to  lower the reactor performance (Sarner et al., 1988). Sulfate-reducing bacteria in the wastewater reduce sulfate to sulfide, a very toxic form. However, adverse effects of sulfide in the two reactors during the step-up operation period could be rather insignificant due to the following reasons:  64 •  Dilution certainly helped, especially during the start-up process (Lettinga et al., 1985). The feed was never full-strength. The highest feed strength came near 60 g COD liter , while the typical strength for raw baker's yeast wastewater used in this study ranged from 70 to 100 g COD liter . -1  -1  •  The pH's within the reactors were either within or near the optimal range of 7.5 to 8.0. In this pH range, a good part of sulfide dissociates into HS , a form less toxic to bacteria (Sarner et al., 1988). -  •  The COD/S0 ratio of the feed has always been above 10 g g , which means that natural gas stripping of H S was sufficient to keep H S toxicity to a rather insignificant degree (Lettinga et al., 1985). =  -1  4  2  2  •  The seed sludge had already been acclimated to the wastewater prior to being used to seed the reactors.  •  Sizeable concentrations of bacteria have attached to the reactor wall. Reactor B, particularly, enjoyed the added advantage of more attached biomass through the fixed medium. Fixed biomass has been demonstrated to be much more tolerant to stress and toxic compounds (Lo et al., 1984).  2) Reactor Profile Study The chemical analyses conducted on the daily effluent provided information about the reactor as a whole because the effluent was a daily composite. For benchtop laboratory-scale reactors (e.g., 4-liter cylindrical reactors), the above approach is adequate. However, for larger reactors like the two reactors used in this experiment there was the need of knowing the values of parameters being monitored (e.g. pH) at different locations in the reactors in order to better understand how wastewater is being treated in relation to the location in the reactor. In this part of the study, the interest has been  focused on sludge concentration, pH, COD, and VFA along the  height of the reactors— and thus the name "profile study".  65 a) Sludge Profile and Total Sludge Growth The profile of sludge concentration, expressed in g VSS liter , along the height -1  of the reactor is presented in Figure 5.4.  The general trend shows that the sludge  concentration was much higher at the bottom of the reactor, and it tapered off to some extent and levelled off (i.e., VSS concentration became more or less constant) above 50 cm of reactor height, measured from the bottom. The highest point (above 170 cm) corresponded to the sludge sampling port above the three-phase separator. The thick sludge at the bottom was the sludge bed, and the thinner sludge on top of the first was the sludge blanket. The sludge bed, being muddy in this study, tended to hamper smooth fluid flow causing channeling so that feed material preferentially passed through the cracks in the bed. In contrast, the sludge blanket was better mixed and approached complete mixing in the region of constant concentration (Yan et al., 1989b). The common pattern for both reactors is that, as the organic loading rate increased, the sludge blanket also expanded upwards.  First, as biogas was being  produced, the sludge bed was lifted upwards by the gas bubbles. As more gas was produced, more flotation was created by the gas bubbles, and thus more sludge was lifted upward. Second, when organic loading became too high, the sludge could not digest the incoming wastewater as quickly as it did at lower organic loading rates. If such a high loading regime was prolonged, the sludge will not be able to maintain its vitality, and its settleability would deteriorate as a result. Poorly settled sludge tended to suspend and/or float to the top of reactor.  In this experiment, when poor  settleability occurred, reactor treatment efficiency dropped even though the reactors' sludge-retaining ability might have prevented a good percentage of sludge from being washed out. From the behavior the sludge profile, a record of history of reactor performance could be obtained. At an organic loading rate of 2.6 g COD liter day , reactor A has -1  -1  66  S L U D G E PROFILE 50-,  REACTOR A 40  i—  30-  •  20.9 g COD/liter (DAY 66)  •  32.8 g COD/liter (DAY 116)  •  37-2 _g_C0_D/lite_r (DAY ^59)  O 45.3 q COD/liter (DAY 208) A 52.1 g COD/liter (DAY 231)  (/) CO  >  20  10-  \ 100  REACTOR HEIGHT (cm)  S L U D G E PROFILE  REACTOR B •  20.9 q COD/liter  •  32.8 q COD/liter  • 37.2_g_CO_D/lite_r O 45.3 g COD/liter A 52.1 g COD/liter  too REACTOR HEIGHT (cm)  Figure 5.4:  Sludge profile versus reactor height  67  a well-settled sludge bed (Figure 5.4a). Most sludge concentrated in the first 50 cm of reactor height, measured from the bottom; there was very little sludge in the blanket. At a higher loading of 4.3 g COD liter- day 1  1  (day 116), the bed expanded  considerably so that the blanket concentration rose from about 2 g VSS liter to 12 g -1  VSS liter- . When the loading was 4.8 g COD liter day , the blanket concentration 1  -1  1  reached its peak of 20 g VSS liter at day 159 which corresponded to the time when -1  reactor A's treatment was poorest (also compare with Figure 5.2). During the same period, a large amount of floating sludge collected at the top of the reactor, which resulted in a high sludge concentration at the highest sampling port (26.8 g VSS liter ). By day 208, the highest bed sludge concentration had risen to 43.0 g VSS -1  liter- , an increase of 38%, and the blanket sludge concentration had slightly lowered. 1  The profile at day 231 was almost identical to that of day 208. One thing common to the last two profiles was that no longer was there excessive floating sludge at the top of reactor. It was felt that the reactor was either adapting to the high loading regime, or enough sludge had been lost so that a new "equilibrium" was reached. Ordinarily, when a reactor is subject to a new higher organic loading rate, its gas production increases and is followed by a surge in sludge washout.  If the new operating  conditions are well within the capability of the reactor, adaptation and stabilization should be expected.  This tendency is best observed in Figure 5.2.  As the  microorganisms adapted to the new environmental conditions and as they were lost or produced, the total amount of sludge and its distribution within the reactor changed so that at each sampling time was a new equilibrium. Figure 5.4b shows that, while having a similar overall appearance, reactor B's highest sludge bed concentrations (i.e., concentrations for the lowest sampling port for the five profiles) were generally higher than reactor A's counterparts: 27.6 to 50.2 g VSS liter- for reactor B versus 20.6 to 48.3 g VSS liter- for reactor A. Another 1  1  68  interesting observation was the "time lag" in reactor B as compared with reactor A. It has been noted that reactor A experienced extensive sludge washout observed in the profile of day 159; however, such sludge washout was not observed in reactor B (indicated by the excessive sludge concentration at the top sampling port) until day 208. It was felt that the fixed-film structure in reactor B must have been responsible for such a delay. Since a fixed-film structure promotes the attachment of bacteria (biomass), one normally thinks that less sludge is freely moving and hence washed out of the system.  Similarly, it took longer for reactor B to lose the same amount of  sludge— the reactor was said to be more tolerant to loading stress. The time profile of total sludge, expressed in gram of VSS, in the reactor is shown in Table 5.3. At the beginning of the experiment, each reactor was seeded with 58.3 g VSS. As time went by and the organic loading rate rose, the total amount of sludge in each reactors increased accordingly. There was a steady sludge increase in the two reactors up until day 159 (organic loading rates up to 4.8 and 5.9 g COD liter day for reactors A and B respectively). The total sludge figures for this period -1  -1  are in keeping with the observations made in previous sections (Figures 5.1, 5.2, 5.3). The two reactors were under little or no stress.  However, after day 159, as the  organic loading rate was raised to around 9 g COD liter day , signs of stress in both -1  -1  reactors manifested as a decrease in total sludge. Between days 159 and 208, the total sludge decreased for both reactors indicating that sludge washout was higher than growth so that the net growth was negative. It was clear that the bulk of the sludge washout took place during this same period, when the reactors, especially A, were under much loading stress.  T A B UE 5.3: Sludge profile Sludge in Reactor  Loading Rate  g VSS  g COD liter- day 1  Day  A  B  1 66 116 159 208 231  58.3 86.6 215.0 312.6 227.3 293.3  58.3 78.3 228.1 379.5 299.3 270.3  Sludge Loading 1  A  B  2.6 4.3 4.8 9.4 6.2  2.8 5.0 5.9 8.3 6.8  g COD g- VSS day 1  1  A  B  0.49 0.32 0.25 0.66 0.34  0.57 0.35 0.25 0.44 0.40  Comparing between the reactors, the maximum total sludge of reactor B was always higher than reactor A up until day 231. The higher total sludge in reactor B was one reason why reactor B's methane production was better than that of reactor A. After day 231, the total sludge of reactor B turned out to be lower than that of reactor A. One would expect reactor B to perform less well than reactor A. However, the data presented in Figure 5.2 do not support this rationale. It should be noted that the total sludge parameter does not account for all sludge present in the reactor. In the case of reactor B, it was found that all ropes were covered with thick sludge. Thus, even though the total sludge figure for reactor B at day 231 was less than that of reactor A (270.3 g VSS for A as opposed to 293.3 g VSS for B), the additional sludge attached on the ropes in reactor B probably offset the difference in sludge mass, and was more active and productive than the sludge in reactor A. There is a relation between the total amount of sludge in the reactor at a given time and the organic loading rate that is imposed on the system. This relation is the sludge loading (or food-to-sludge ratio) and is expressed in g COD g  -1  VSS day . 1  According to Wu et al. (1985), there is an optimum value for sludge loading, 0.6 g COD g-1 VSS day-1, at which the growth conditions are most favorable. Based on this  70  optimum sludge loading, it appears that the two reactors were underfed most of the time during the course of the experiment. Except for the single peak sludge loading rates of 0.66 and 0.57 g COD g  -1  VSS day for A and B respectively, reactor A's -1  sludge loading rate ranged between 0.25 and 0.49 g COD g- VSS day , and reactor 1  1  B's between 0.25 and 0.44 g COD g VSS day . However, an examination of Figures -1  1  5.1 to 5.3, it does not seem likely that a higher organic loading rate at the very end of the experiment would lead to better methane yields and system performance. Maybe reactor B would give a higher volumetric methane production, because it was not clear whether it would rise or drop. Presumably, if a program of higher sludge loading and, especially, higher hydraulic loading rates (to impose selection pressure) was initiated right from the start of the step-up period, more granular and active sludge would have been developed, leading to better reactor performance (Wu et al., 1985; Lettinga et al., 1985).  b) pH Profile The pH along the height of the reactor is depicted in Figure 5.5. It can be seen that the profile pH's of both reactors were all well above 7 and mostly between 7.4 and 7.8. In addition, it is noted that pH generally rose with the height of the reactor; that is, the further up it was from the bottom of the reactor, the higher was the pH. This observation is in keeping with the mechanism of anaerobic digestion. Wastewater is degraded more and more up the reactor; in the same way, the pH increases as VFA's are digested and hydrogen utilized to form methane gas. Moreover, there was no abrupt increase or decrease in pH. The pH is an indicator of "well being" of the underlying fermentation process.  From an  oversimplified point of view, anaerobic digestion consists of fatty acid formation and methanogenesis. When there is more fatty acid being formed than it can be converted  pH PROFILE (Reactor A) 8.2  •  DAY 66  •  PAY 116  •  DAY 159  O  DAY 208  A  DAY 231  /  7.8  7.6  /  r  oA""  7.4H  7.2  20  40  •0  80  100  REACTOR HEIGHT  110  M0  160  160  (cm)  (a)  pH PROFILE (Reactor B) 8n  7.B  .-A  7.6H •  7.4  7.2H  20  40  (0  60  100  REACTOR HEIGHT  DAY 66  •  DAY 116  •  DAY 159  O  DAY 208  A  DAY 231  120  (cm)  (b)  FIGURE  5.5: pH v e r s u s R e a c t o r H e i g h t  160  180  72  in methane, VFA accumulation occurs and pH drops. Methane production in this case is the limiting stage. The reverse is also true. When methanogenesis proceeds faster than acidogenesis, little fatty acid is left unconverted to methane; pH rises as a result. In the latter case, acid generation is the bottle neck of the fermentation process. Therefore, basing on the foregoing presentation, the absence of pH stratification (i.e., drastically different pH's within a reactor) in the two reactors indicates that acidogenesis was the limiting stage of the whole of fermentation process. This finding is substantiated by the fact that baker's yeast wastewater consists mostly of hard-todegrade organic matters. In contrast to this observation, Yan et al. (1989b), treating cheese whey (readily degradable), reported the presence of two zones in relation to pH, that is, a distinctively lower pH in the acidogenic zone on the bottom of the reactor and a much higher pH in the methanogenic zone above the first zone.  c) COD Profile The total COD profile based on the five profile samplings is shown in Figure 5.6. There are some important observations to be made. First, in both reactors, the profile curve rises with increasing influent COD concentration.  The feed strength  always increased in the course of the experiment: from 20 to 52 g COD liter for the -1  time span of the five profile samplings. This finding is reasonable because, as feed COD concentration rises, the residual COD increases and hence the profile is expected to shift upward (i.e. increase in COD) and may or may not assume a different configuration. Second, the sludge blanket in each reactor expanded over time. At the time of the first profile sampling (day 66 profile), most of the sludge concentrated on the bottom (the bed) of the reactor leading to high COD concentrations, while the blanket COD concentration was relatively low compared to that of the sludge bed. Sludge  TOTAL COD PROFILE (Reactor A)  E J  20000  •  DAY 15?  O DAY 208 A  DAY 231 20  40  40  00 100 120 REACTOR HEIGHT (em)  140  140  100  (a)  TOTAL COD PROFILE (Reactor B) m  DAY 66  •  DAY 116  •  OAY 159  O DAY 208 A  DAY 231  -A-  «j> 4 0 0 0 0 -  -O-  3 D  20  40  •o  ao too 120 REACTOR HEIGHT (cm)  140  1(0  no  (b)  FIGURE  5.6: T o t a l COD v e r s u s R e a c t o r H e i g h t  74  settleability at this time was good and sludge activity was high. Over time, however— as buoyancy due to gas bubbles became more significant, and as sludge settleability deteriorated due to increased stress— much of the bed sludge became suspended tended to float to the top of reactor. A direct consequence of all this development is that the difference between bed sludge concentration and that of the blanket became less and less significant. In short, towards the end of the experiment, the entirety of each reactor's column was filled with poorly-settled and, very likely, low-activity sludge. The same conclusion can be drawn from the decreasing difference in sludge concentration along the reactor height (Figure 5.4). Another consequence is excessive sludge washout, which was readity verifiable at and after day 159. Total COD includes the COD contributed by the sludge and wastewater, so that it can be higher than feed COD alone. This case is especially true in this experiment because COD removal was relatively low and blanket sludge concentration was high. Figure 5.7 (soluble COD profile) helps explain something subtle about the nature of the wastewater being studied that Figure 5.6 does not readily show. It is clear in Figure 5.7 that all soluble COD profiles are essentially horizontal, as opposed to those of total COD in Figure 5.6. This pattern indicates that there was no substantial COD break down 10 cm above the reactor base. In other words, the bulk of the COD break down took place between the bottom of the reactor and the lowest sampling port. This finding underscores the fact that baker's yeast wastewater is hard to degrade. Since dense sludge was at the bottom of the reactor, a lot of digestion took place there. After the wastewater went past the sludge bed, due to its slow rate of biodegradability, it would not undergo visibly significant degradation in terms of soluble COD for the remaining length (or residence time) of the reactor. In terms of total COD, however, it is evident from Figure 5.6 that most of the time the three-phase separator did separate out substantial non-soluble COD (most likely buoj^ant sludge) from the treated effluent  SOLUBLE COD PROFILE (Reactor A) 40000  30000-  •  DAY 66  O DAY 208  •  DAY 116  A DAY 231  •  DAY 159  SC-4--AA  "A"  20000  — •  20  40  0l0  (0  l tOO  120  140  1*0  1*0  REACTOR HEIGHT (cm)  (a) SOLUBLE COD PROFILE (Reactor B) •  DAY 66  •  DAY 116  •  DAY 159  O DAY 208 30000-  A  20000  A —  #  D« _ __ .-O- *4j-r-^ D  D  D  •  A-  DAY 231  • - -A  B^-S^ -O  10000-  00  FIGURE  19 100 120 REACTOR HEIGHT (cm)  (b) S.7: S o l u b l e COD v e r s u s R e a c t o r H e i g h t  76  overflow (see the total COD numbers at the highest sampling port of the two reactors). It can also be seen that the sludge-retaining capability of the separator became more pronounced as the sludge concentrations increased. The fact that most of digestion took place at the bottom of reactor and that the separator generally was able to remove a significant percentage of non-soluble COD suggests that shortening of the reactor length in the low breakdown region will probably not affect significantly the treatment efficiency of the system.  d) VFA Profile Figures 5.8 and 5.9 depict the VFA profiles for the two reactors. In general, even though reactor B's VFA levels were mostly lower than those of reactor A, the first three profiles (those at day 66, 116, and 159) look similar for the two reactors because of the low concentrations.  VFA profiles at days 208 and 231 are rather  outstanding because of increasing loading stress imposed on the reactors during this period. A common aspect to all VFA graphs is that the profile at day 231 is always lower than that of day 208. It is not hard to figure out the cause of this pattern: the imposed organic loading rate before and at day 231 was lower than the counterpart at day 208. Another observation is that there seems to be more VFA degradation, especially the profiles at day 208, along the reactor height for reactor B than A. Whereas reactor A's profiles tend to be fairly horizontal for all four VFA's, reactor B's profiles show considerable slope particularly near the bottom of the reactor. More active sludge bed and the fixed-film structure are believed to be responsible for such a difference in reactor B. Figures 5.8a and 5.8b shows that reactor A's acetic acid levels are well beyond the suggested failure level of 800 mg liter (Hill et al., 1988) whereas those of reactor -1  PROPIONIC ACID PROFILE (Reactor A)  ACETIC ACID PROFILE (Reactor A) 3000  2000  z o  A  10004  £ •  DAY 66  O  DAY 208  O  DAY 116  A  DAY 231  •  ° A 'SSL  Of  Y  A - A  O  <  A  -A  100  ISO  1000  o z o o  -A  z o o SO  2000  SO  200  w  jf OS  A DAY 231  DAY 159  ISO  1500  °'V -o-»-« ' 0  £  \>  v  1000  z o  z  o  DAY 116  •  PROPIONIC ACID PROFILE (Reactor B)  1300  IOOOH  D  DAY 208  (c)  ACETIC ACID PROFILE (Reactor B)  E  O  100  (a)  0»  DAY 6 6  REACTOR HEIGHT (cm)  REACTOR HEIGHT (cm)  ^  •  <  500  ot  u  u z o  z  500  \  o o  o  SO  100  ISO  REACTOR HEIGHT (cm)  (b)  FIGURE  5.8:  200  30  100  ISO  REACTOR HEIGHT (cm)  (d) A c e t i c and P r o p i o n i c A c i d s v e r s u s R e a c t o r H e i g h t  BUTYRIC ACID PROFILE (Reactor A)  ISOBUTYRIC ACID PROFILE (Reactor A) 600  (c)  «  A  O) £  •  D  A  Y  6  6  •  DAY 116  •  DAY 159  400-  Z  o  DAY 2 0 8  A  DAY 231  o  OC  200-|  z  •  DAY 6 6  o  DAY 2 0 8  •  DAY 116  A  DAY 231  •  DAY 159  O  z o o  •i=5*5-a-rB-a=a-=BI  -o  130 SO 100 REACTOR HEIGHT (cm)  ••••'•-•-ra-a^a— SO  200  i-i—  100 REACTOR HEIGHT ( c m ) ISO  BUTYRIC ACID PROFILE (Reactor B)  ISOBUTYRIC ACID PROFILE (Reactor B) (b) 8 0  T  •  PAY 6 6  o  1000-  DAY 2 0 8 DAY 231  DAY 6 6 DAY 116 DAY 159 500  DAY 2 0 8 DAY  nmm ISO REACTOR HEIGHT (cm)  FIGURE  200  -  o4-aa B « B » B I - B - B - B - B -  soREACTOR  5.9: I s o - and B u t y r i c A c i d s v e r s u s R e a c t o r H e i g h t  ISO HEIGHT ( c m ) 100  231  79  B are slightly over the failure level. Relatively speaking, reactor B is surviving better than reactor A. These results are found to match with those presented elsewhere in this thesis (under "Step-up Operation"). The propionic acid graph is the key to showing the superiority of reactor B over A (Figures 5.8c and 5.8d). Reactor B's propionic acid levels are drastically lower than those of reactor A— about half of those of reactor A. In contrast, whereas reactor A's propionic acid profile is virtually horizontal and is at around 2000 mg liter- , reactor 1  B's go from 1000 mg liter at the bottom of the reactor to below 800 mg liter at the -1  -1  top of reactor. Reactor B is definitely more active than reactor A in digesting propionic acid; the accumulation of VFA's eventually leads to process failure of reactor A (Hill et al, 1988). Long-chain VFA's are equally important for determining reactor health (Figure 5.9). Hill et al. (1988) claimed that iso-butyric acids in excess of 15 mg liter mean -1  impeding digester failure. Based on this figure, reactor A was definitely in the process of failing (over 100 mg liter ) at and after day 208. In turn, reactor B's iso-butyric -1  acid levels did not exceed the criterion value except at and after day 231. However, it should be noted that reactor B's exiting iso-butyric acid level was about 30 mg liter  -1  and, in addition, that some reduction in VFA usually took place between the top sampling port and the effluent collector. In effect, the implication is that the actual iso-butyric acid concentration should be less than 30 mg liter . -1  Indeed, a  concentration of 20 mg liter , from Table 5.3 (day 237), would be a reasonable -1  number. In summary, reactor B was on the "border line" in relation to failure. B . Chapter Conclusion •  The maximum biogas methane composition was 54% (v/v) during the step-up operation phase. A survey of methane compositions of other authors' at  80 similar loading rates suggested that the maximum methane composition achievable with baker's yeast wastewater was around 60%. •  Reactor A had achieved its maximum volumetric gas production of 0.91 liter CH liter day at 5.8 g COD liter day which was still far from the highest loading rate (9.4 g COD liter day ) applied in this study. Reactor B, however, did not appear to have reached its highest possible gas production even at the maximum loading applied to it (9.1 g COD liter day ) since it was not clear whether the methane production curve would drop or continue to rise. -1  -1  -1  -1  4  -1  -1  -1  •  In terms of methane production, additional biomass clung to the ropes and enhanced reactor B's biogas production, both quantitatively and qualitatively, and at the same time rendered reactor B more tolerant to organic loading rates higher than 6 g COD liter day . -1  •  -1  Baker's yeast wastewater is not readily degradable since the highest COD reduction achieved in this study was 71% at an organic loading of 2.3 g COD liter day (at a HRT of about 7 days). This number is low compared to that of cheese whey, which is very easily biodegraded. At organic loading rates higher than 6 g COD liter day (after day 150), COD reduction fell below 50% for both reactors; single-stage treatment at this efficiency in this loading range was considered rather unattractive. -1  -1  -1  •  -1  -1  Even though baker's yeast wastewater rather different than cheese whey, over the organic loading range of 0.91 to 7.8 g COD liter day , the methane yield values of the two reactors was approximately 0.3 liter CH g COD day which was surprisingly similar to the methane yield obtained by Yan et al. (1989a) from cheese whey with a UASB (0.30 to 0.34 liter C H g COD day ). -1  -1  -1  -1  4  -1  4  1  •  Based on Figures 5.1 to 5.3, especially Figure 5.3, the three stages (with respect to stress and failure) that the two reactors went through can be seen as (1) little or no stress in both reactors for the first 153 days; (2) rapidly increasing stress in both reactors (especially in reactor A) from days 153 to 165; and (3) the setting in of failure in reactor A and reactor B's approaching failure from day 165 to the end of experiment.  •  Sulfate effects in the two reactors were found to be not very significant mainly because (1) the pH within the reactors were mostly in the 7.5-8.0 range where sulfate toxicity was minimum; (2) the COD/S0 ratio of the feed had always =  4  81 been above 10 g g , which meant that natural gas stripping of H S was sufficient to keep H S toxicity to a rather insignificant degree (Lettinga et al., 1985); and (3) the seed sludge had already been acclimated to the wastewater prior to being used to seed the reactors. -1  2  2  •  The sludge bed was found to expand with increasing organic loading. This bed expansion manifested in the form of global flattening of the sludge profile curves; that is, the difference in sludge concentration between the sludge bed and the top of reactor diminished over time.  •  A time lag in the peak sludge washout was observed for reactor B in relation to reactor A (Figure 5.4). Whereas reactor A had its peak sludge washout in the profile of day 159, reactor B had its equivalent in the profile of day 208. Even though reactor B's total suspended sludge (VSS) was less than that of reactor A, reactor B still performed better. Reactor B's ropes were thought to be responsible for such a difference.  •  There was no pH stratification in the reactors. Because baker's yeast wastewater is not readily biodegradable, there was no localization of pH as observed in cheese whey by Yan et al. (1989b): the presence of two zones in relation to pH, that is, a distinctively lower pH in the acidogenic zone on the bottom of the reactor and a much higher pH in the methanogenic zone above the first zone.  •  Figures 5.6 and especially 5.7 revealed that the bulk of biodegradation took place in the sludge bed (the lower 40 cm of reactor height).  •  The profile VFA data (Figures 5.8 and 5.9) were in harmony with those of the Step-up operation VFA (Figure 5.3). The profile of day 159 shows that there was little stress. Thereafter, stress manifested in the form of high VFA profiles.  VI.  CONCLUSIONS  Methane production and COD reduction from baker's yeast wastewater are lower compared to those of more easily biodegradable wastewaters such as cheese whey. It appeared that the maximum achievable methane composition for baker's yeast wastewater was around 60% (v/v). At about day 10 and day 14 (during the start-up), reactors B and A respectively experienced the negative-to-positive turnover which signalled that organic removal had prevailed over sludge loss. Because baker's yeast wastewater is hard to degrade, there was no stratification in pH (i.e. acidic layer in the bottom and methane zone above the first). As a result of its slow degradability, baker's yeast wastewater has a much higher buffering capacity comparedtocheese whey. Over the range of feed strengths tried, 25 to 35 g liter (at an HRT of 7 days) appeared to be the optimum as far as overall efficiency was concerned. -1  High levels of sulfate in the wastewater did not significantly affect reactor performance both in the start-up and step-up periods because (1) the seeding sludge had already been acclimated to the wastewater; (2) the COD/S0 ratio was always above 10 g g ; (3) the pH of the reactor mixed liquor was nearly always in the range of 7.5 and 8.0, where sulfate toxicity was minimum; and (4) dilution of the feed material helped alleviate H S effects. =  4  -1  2  It was found that, both in the start-up and step-up operation periods, the two reactors produced methane yields (0.30 to 0.33 liter CH g COD day ) which were comparable to those of a rather different waste like cheese whey (0.30 to 0.34 liter CH g COD day ). -1  -1  4  -1  -1  4  The study revealed (as shown in Figures 5.6 and especially 5.7) that the bulk of biodegradation took place in the sludge bed (the lower 40 cm of reactor height). The study found (as shown in Figures 5.3, 5.6. and 5.7) that (1) little or no stress in both reactors for the first 153 days; (2) rapidly increasing stress in both reactors (especially in reactor A) from days 153 to 165; and (3) the setting in of failure in reactor A and reactor B's approaching failure from day 165 to the end of the experiment.  With the ropes as a fixed-film medium, the hybrid UASB reactor (reactor B) was more tolerant to stress and toxic compounds and consistently performed better than reactor A due to its more active immobilized biomass.  84  VII.  RECOMMENDATIONS  The following recommendations represent areas which did not receive enough attention during the experiment. Hence the author thinks that anyone doing follow-up work for or repeating the present experiment should take these recommendation in to serious consideration. Listed below are the recommendations: •  In order to promote granulation for a quicker start-up and superior treatment efficiency, selection pressure (i.e. hydraulic loading regime) must be applied and other pertinent criteria discussed earlier followed. In the case of low hydraulic retention time, intermittent feed and/or effluent recirculation may be necessary.  •  Based on the optimum sludge loading of 0.6 g COD g VSS day , organic loading rates near or at this level should be experimented to see whether granulation will proceed more quickly than it has been with the present study.  •  Where low flow rates are applied, caution must be taken to prevent clogging in the feed line system. Supernatant obtained by natural gravity method should be used to minimize coarse suspended particles.  •  In order to ensure the same flow rate in both reactors, separate pumps and speed controllers are a must.  -1  -1  VIII. R E F E R E N C E S American Public Health Association (1975). 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Using volatile fatty acid relationships to predict anaerobic digester failure. Transactions ofASAE, 30(2), 496-501. Hill, D.T. & Holmberg, R.D. (1988). Long chain volatile fatty acid relationships in anaerobic digestion of swine waste. Biological Wastes, 23, 195-214. Isa, Z., Grusenmeyer, S., and Verstraete, W. (1986). Sulfate reduction relative to methane production in high-rate anaerobic digestion: Microbiological aspects. Applied and Environmental Microbiology, March, 580-87.  Kennedy, K.J. and van den Berg, L. (1982). Continuous versus slug loading of downflow stationary fixed film reactors digesting piggery waste. Biotechnology Letters, vol.4,2:137-42. Knechtel, J.R. (1978). A more economical method in the determination of chemical oxygen demand. Water Pollution Control, 116, 25-27. Lettinga, G., Van Velsen, A.F.M., Hobma, S.W., De Zeeuw, W., and Klapwijk, A. (1980). Use of the upflow sludge blanket (UASB) reactor concept for biological wastewater treatment, especially for anaerobic treatment. Biotechnology and Bioengineering, 22, 699-734.  86  Lettinga, G., De Zeeuw, W., Hulshoff Pol, L., Wiegant, W. and Rinzema, A. (1985). Anaerobic wastewater treatment based on biomass retention with emphasis on the UASB process.  Proceedings of the fourth international symposium on  anaerobic digestion held in Guangzhou, China, 279-301. Lo, K.V., Liao, P.H. and Bulley, N.R. (1984). Mesophilic anaerobic digestion of screened dairy manure using fixed-film reactors. Symposium papers: Energy from biomass and wastes VIII, 875-99.  Lo, K.V., Liao, P.H., Whitehead, A.J. and Bulley, N.R. (1984). Mesophilic anaerobic digestion of screened and unscreened dairy manure. Agricultural Wastes, 11, 269-83. Lo, K.V. and Liao, P.H. (1985).  High-rate anaerobic digestion of screened dairy  manure. Journal of Agricultural Engineering Research, 32, 349-58.  Lo, K.V. and Liao, P.H. (1990). Anaerobic treatment of baker's yeast wastewater: I. Start-up and Sodium Molybdate addition. Biomass, 21, No. 3, 207-18. Lo, K.V., Chen, A., and Liao, P.H. (1990). Anaerobic treatment of baker's yeast wastewater: II. Sulfate removal experiment. Biomass (in press). Sarner, E., Hultman, B.G. and Berglund, A.E. (1988). Anaerobic treatment using new technology for controlling H S toxicity. 2  Tappi Journal: Anaerobic Treatment,  Feb, 41-5. Sayed, S., Campen, L. van and Lettinga, G. (1987). Anaerobic treatment of slaughterhouse waste using a granular sludge UASB reactor. Biological Wastes, 21,11-28. Schumann, G.E., Stanley, M.A. & Knudsen, D. (1983). Automated total nitrogen analysis of soil and plant samples. Proceedings of Soil Sci. Soc. Amer., 37, 48081. Segretain, C. and Moletta, R. (1987). Potentialities of a methanogenic microbial ecosystem adapted to wine distillery wastewaters to degrade volatile fatty acids. Biological Wastes, 20, 261-71. Vega, J.L., Clausen, E.C., and Gaddy, J.L. (1988). Performance of immobilized cell reactors. Handbook on anaerobic fermentations. Edited by L.E. Erickson and D. Yee-Chak Fung; Marcel Dekker, Inc.; Chapter 21.  87 Wang, Z., Chen, Z. & Qian, Z. (1985). Status quo and prospects on the study of anaerobic disposal for industrial wastewater in China. Proceedings of the Fourth International Symposium on Anaerobic Digestion, Guangzhou, China,  November. Wu, Wei-Min, Hu, Ji-Cui and Gu, Xia-Sheng (1985). Properties of granular sludge in up-flow anaerobic sludge blanket (UASB) reactor and its formation. Proceedings of the 4th International Symposium on Anaerobic Digestion,  Guangzhon, China, 339-51. Yan, J.Q., Lo, K.V. and Liao, P.H. (1989a). Anaerobic digestion of cheese whey using up-flow anaerobic sludge blanket reactor. Biological Wastes, 27, 289-305. Yan, J.Q., Lo, K.V. and Liao, P.H. (1989b). Anaerobic digestion of cheese whey using up-flow anaerobic sludge blanket reactor: III. Sludge and substrate profile. To be published in Biological Wastes.  


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