Microbial culture system

This invention relates to an improvement in the treatment of waste liquor for reduction of the biochemical oxygen demand (BOD) thereof. It is of particular interest in the treatment of difficult effluents such as the spent sulfite liquor resulting from production of pulp by the neutral sulfite process, the bisulfite process or the acid sulfite process, or in any process producing an effluent sufficiently high in biologically degradable dissolved solids that it involves a disposal problem.
Biological treatment is applied to pulp mill waste effluents, but these systems operate on low concentrations of spent liquor because of the toxicity of such liquors, and are generally designed to operate at low concentrations of suspended solids (biomass). In addition the sludge produced settles very slowly and creates problems, usually preventing successful continuous operation. Such systems are generally not very efficient when compared with high rate activated sludge processes operating at a high level of suspended solids (SS). Owing to the complexity of sulfite liquor (SSL) from the sulfite process, it has been assumed hitherto that SSL could not support the strong microbial growth which is essential to a high rate process for reduction of BOD and for a high degree of autolysis.
In accordance with a program of research carried out at the University of Western Ontario in London, Ontario, Canada, we have developed a microbial culture specially adapted for this purpose and have evaluated its performance. A mixed microbial population originally obtained from domestic sewage survived in and became acclimatized to neutral sulfite semi chemical (NSSC) liquor from the Abitibi Paper Company Ltd. plant at Sturgeon Falls, Ontario during more than a year of continuous feeding. Growth was enhanced by the addition of small amounts of nutrients (ammonia and phosphates), by pH control (adding lime or sodium hydroxide,) and by aeration. The culture then was adapted to and has been maintained in undiluted SSL from the digesters of the Iroquois Falls plant, and has provided the inoculum for all the fermentation studies on which the present specification is based. This yeast culture composition appears to have been very stable throughout the relevant period. It has a high degree of resistance to sulfur dioxide and grows well at an acid pH.
The presence of sulfur dioxide appears to be of some importance in maintaining the stability of the culture. Sulfur dioxide is a strong reducing agent and it kills almost all microbes except yeast and fungi of the present type. The air sparging will oxidize SO.sub.2 to SO.sub.3 thus lessening the toxicity while increasing the acidity and thereby discouraging the growth of extraneous populations.
The present invention differs from known activated sludge processes, in that the biomass and suspended solids in the activated sludge fermentor unit are conveyed as foam-solids directly to a unit where the foam is collapsed and the active bio-sludge recovered for recycle to the activated sludge unit. The foam transfer system is used to reduce the SS levels to a point that settling can be accomplished. This method of transfer also contributes to solids control of the reactor and to autolysis.
Foams are produced in the aeration of many wastes, and especially pulp and paper waste. In conventional practice this must be controlled because it is a deterrent to the mass transfer of oxygen, especially if mechanical surface aerators are used. Foam can become a serious nuisance since it may be several feet deep and can literally cover everything, preventing good maintenance and process control. Antifoams and all types of mechanical devices are used to control and collapse such foams. Such antifoams usually decrease the mass transfer of oxygen in the process. In the present invention foaming is an important part of the process as only bio-sludge entrapped in the foam is collected and transferred to a chamber in the clarifier. Sludge is recovered by collapsing the foam and it is observed to rapidly settle to the bottom of the clarifier and may be recycled in whole or part along with a minimum of liquor back to the activated sludge unit.
In a conventional process biosludge is transferred to a clarifier as a liquid, and no attempt is made to recover foam or the solids presentation foam for passage to the clarifier. Wastes which foam can often not be treated by the activated sludge process because of the foaming propensity. This new process, which requires foaming as part of the process, has distinct advantages as it accomplishes the same objectives as a conventional activated sludge process.
The aeration unit will normally be totally enclosed to aid in collection of foam. Also the unit will normally be operated under a moderate positive pressure to facilitate transfer of foam to the clarifier. The process can be conducted in any size unit from a few liters to hundreds of thousands of liters. The prime parameters for a continuous process are retention time of the waste, proper aeration, flotation of the bio-sludge, collapsing of the foam, settling and recovery of sludge, and recycle of such sludge.
An important advantage is that the production of foam is not a problem since it is an integral part of the process. Also, under certain operating conditions and for certain types of waste the bio-sludge generated can be recovered from the clarifier and totally recycled to the aeration unit with subsequent autolysis, and no sludge has to be wasted from the clarifier. It can all be recycled to the activated sludge unit. Thus expensive process equipment required for disposal of excess sludge wastage from the clarifier can be avoided. This problem is so great in the prior art that the conventional activated sludge methods cannot be applied to strong pulp mill waste.
The biological cells and suspended solids in the recycled sludge are efficiently oxidized in the activated sludge unit much as if the chamber were operating as a "biological furnace." Of course, not all the cells are removed from the system in this autolytic-biofurnace, as new cells and catalysts are also synthesized, thus maintaining the system in equilibrium. In test systems studied continuously, they have been operated for 78 days and more without any sludge wastage. The conditions used in such operation are shown separately in several examples.
The present bio-sludge flotation technique is most effective in treating waste which has an inherent tendency to foam. It is also broadly applicable to non-foaming systems to which foaming or flotation agents may be added to induce or sustain the flotation process. Cells become entrapped in the foam and are carried to the surface where they can be removed. It appears that only certain microbes from the aeration vessel are entrapped in the foam and are carried to the clarifier. A foam-activated sludge system operated in this manner has many distinct advantages for treating certain wastes.
It is found that the foam has a lower content of suspended solids (SS) than does the liquid in the fermentor vessel. The suspended solids content, or suspended solids/liquid ratio, of the foam when collapsed may desireably be not more than half that of the fermentor broth. In the usual practice of this invention it will preferably be 1/4 to 1/3, most preferably about 1/3. For example, it has been found that the foam, if "broken" or collapsed into a liquid, contains in one case about 13,000 parts per million suspended solid, compared with the 30 to 50,000 parts per million suspended solids content of the liquid in the fermentor from which the foam was formed. In addition to permitting transfer of liquid from the fermentor vessel with a minimized amount of solids transfer, it has been found that when the foam is broken the suspended solids tend to settle very quickly in the clarifier, thus permitting a relatively high rate of removal of liquid from the fermentor and a more rapid recovery of the bio-sludge for recycle. Thus the foaming step reduces the suspended solids to a level and type that will settle far more rapidly than the suspended solids present in the fermentor medium, which would be the form encountered in a conventional transfer process. In the prior art, the reactor liquid overflow is presented to the clarifier for settling. Any transfer of liquid will reduce the efficiency of the process and should be minimized. However, we do not exclude the possibility of some direct transfer of a small amount of liquid fermentor broth. This may be tolerated so long as it does not adversely affect the settling characteristics of the suspended solids in the clarifier.
The invention was found to be particularly effective in treating the product of biosulfite high yield process. The process involves the treatment of wood chips with a solution of sodium bisulfite (NaHSO.sub.3), and cooking at a high temperature an pressure. The partly cooked soft chips go through the usual blow pit washing and pulp refining steps. The liquid discharge has a pH of 3 to 4.5 and it is called "spent sulfite liquor."
This effluent stream contains small amounts of sulfur dioxide, wood resins, resin acids, high and low molecular weight fatty acids, alcohols, aldehydes, ketones and eugenols, along with large amounts of saccharides and lignosulfonates. The two latter components account for the high biochemical oxygen demand (BOD) and chemical oxygen demand (COD) levels in SSL. No simple economical chemical recovery process is available for these materials. However, the presence of large concentrations of carbohydrates and other organic compounds particularly qualify this type of waste for biological treatment either to remove BOD or to produce valuable products. The sugar components are the main contributors to the high BOD.
The spent liquor which constitutes the substrate or feed for this process may be very high in dissolved solids. It normally has approximately 7 to 11 percent dissolved solids concentration. This is higher than that described previously for biological treatment processes. The prior art generally deals with materials in the area of 3 to 5 percent dissolved solids and lower.
The BOD.sub.5 is a conventional term. It is defined as the amount of oxygen required by living organisms engaged in the utilization and stabilization of the organic matter present in the wastewater. The standard test involves seeding with sewage, river water, or effluent, and incubating for 5 days at 20.degree. C. In the practice of the present invention, some adjustment to the concentration of the SSL may be necessary or desirable to compensate for the wide variations encountered in plant samples of the SSL. Reference may be made to the book "Standard Methods For the Examination of Water & Waste Water", 13th edition--1971--American Public Health Association, Inc.
A continuous treatment process has now been developed for the biodegradation of SSL, capable of removing nearly 90 percent of the biochemical oxygen demand (BOD.sub.5) of typical high yield sulfite mill effluent. The process may be operated under autolytic conditions with no sludge wastage in which part of the energy generated by the cell also dissolves cells. The process developed can be conducted in any size production vessel; however the autolytic process covered herein was conducted in a pilot scale (48 liter) bioreactor system. Engineering specifications for an industrial process design have been calculated to meet the requirements of the 240 ton per day Abitibi-Iroquois Falls Pulp Mill, to provide maximum BOD.sub.5 removal with little or no sludge wastage while operating in the autolytic mode.
However, this SSL treatment process might also be viewed as a potential source of protein; if retention time is reduced to avoid autolysis, wasted sludge which can be a valuable high protein by-product is produced and it can be recovered, dried and utilized in animal feed. The mixed culture system which was developed for this project is a stable, mixed population, long adapted to undiluted SSL medium and apparently not undergoing mutative changes or selective enrichment which could affect its potency. By chemical analysis it is known to resemble yeast grown on carbohydrates, having an amino acid composition typical of high grade feed supplements. It was found to be comparable to other single cell proteins of the yeast type. The continuous reactor studies, therefore, included brief harvesting periods under conditions favourable to excess sludge production, which were found to be compatible with 50-60% BOD.sub.5 removal. Thus the two operating modes could be used, (1) with basically no sludge removal and (2) with high sludge production.
In one continuous fermentation experiment 80% reduction of BOD.sub.5 was achieved with 2.5 days retention time in the aeration vessel. Suspended solids built up to a maximum of 3.3% (w/v) at the midpoint of the two month run, during which no solids were harvested. Chemical analysis of the sludge detected 40% protein with individual amino acid concentrations suggesting potential nutritional value.
The quality of the SSL after biological treatment has shown significant improvement especially with respect to oxygen demand (BOD.sub.5). The microbes removed most of the sugars and other dissolved organic materials with the exception of lignosulfonates. The present process has successfully reduced the total dissolved solids of the incoming SSL, by using these dissolved solids as a substrate for (aerobic) growth in which biomass is generated and carbon dioxide is liberated to the atmosphere. Excess biomass is removed either by autolytic liquefaction and discharge or by harvesting.
SUMMARY OF THE INVENTION
The present invention provides in one aspect, a method for biodegrading a process waste liquor having a propensity to foam comprising aerating and agitating it in a closed fermentation tank, removing foam from the upper part of the fermentor tank, and transferring the foam to a clarifier tank, collapsing the foam in the clarifier tank, collecting the settled sludge, recycling the settled sludge back to the fermentor, and drawing off the treated waste liquor from the clarifier by overflowing it. The process waste liquor may be spent sulfite liquor from a pulp mill.
In another aspect, the present invention provides a method of biodegrading a spent sulfite liquor by an autolytic mixed fungal (yeast and yeast-like) system, comprising the steps of feeding the mixture to a mixed fungal (yeast and yeast-like) inoculated fermentor with agitation and with aeration, resulting in foaming of the mixture, said foam carrying with it fungus and sludge resulting from the fermentation, the suspended solids content of the foam when collapsed being less than the suspended solids content of the fermentor broth, said foam being conducted to a means for separation into a sludge and a clarified effluent, said sludge being recycled to the fermentor vessel.
Nutrient may be added where required. The pH should desirably be mildly acid or neutral. The SSL will normally have a dissolved solids content of 6 to 14%, or preferably 8 to 10%.
The suspended solids content of the foam will normally be not more than half of the fermentor broth.
The suspended solids in the fermentor vessel may desirably be controlled by adjusting the sludge recycling to maintain the suspended solids in the fermentor vessel at not greater than 60,000 parts per million. The degree of recycling and the rate of the feeding of fresh medium will desirably be held at a level at which constant autolysis may be maintained.
Clarification of collapsed foam is effected in the clarifier by underflow of settled sludge and overflow of treated liquor. The fermentation is normally carried out in a closed fermentor, and the aeration air stream provides the means for forcing the foam from the fermentor.
The spent sulfite liquor should contain not more than 1% (W/V) of sulfur dioxide. Some treatment with lime or sodium hydroxide, or boiling or steam stripping may be desirable to achieve thus sulfur dioxide level.
The fermentation will normally be carried out at a temperature in the range of 8.degree. to 40.degree. C., preferably 10.degree. to 35.degree. C., and most preferably 30.degree. to 35.degree. C. A typical fermentor broth biomass may have a suspended solids concentration ranging from 10,000 to 60,000 ppm, preferably 35,000. It may employ a fermentor retention time of 1.5 to 4 days and a clarifier retention time of 0.2 to 2 days. Preferably the fermentor retention time is 2.2 days and the clarifier retention time is 1 day.
The pH in the fermentor is normally maintained between 2 to 8.5, preferably around 3.3.
The dissolved oxygen level in the fermentor is normally not less than 0.3 ppm and preferably between 1.5 to 5 ppm.
In some cases, NH.sub.3 was added to the fermentor broth in a range of 400 to 4,000 ppm and total phosphate added in a range of 400 to 4,000 ppm and with sufficient caustic to maintain an acceptable pH. In a specific case, the NH.sub.3 concentration was 1,330 ppm and phosphate was 1,140 ppm. Preferably the general BOD.sub.5 :N:P ratio is 100:5:1.
As to the foam after collapse, the suspended solids concentration is preferably in the range of 1000 to 30,000 ppm, normally around 12,000 or 13,000 ppm.
In one aspect, the invention provides an apparatus for biodegrading a process waste liquor having a propensity to foam comprising a closed fermentation tank equipped with an agitator, an aerator, an inlet for liquor feed, an inlet for recycled sludge feed, an outlet for removal of foam from the upper part of the fermentor tank, a means for transferring the foam to a clarifier tank, and said clarifier tank being equipped with foam collapsing means, collecting means for settled sludge, means for recycling the biosludge to maintain the suspended solids in the fermentor at the desired level required for operating in the autolytic mode.
In another aspect, this invention provides a method for biodegrading a process waste liquor comprising the steps of exposing the mixed fungal culture system to increasing concentrations of waste liquor until the system becomes acclimatized to waste liquor of a suitable concentration, then treating process waste liquor with the acclimatized fungal culture system, aerating and agitating the mixture in a closed fermentation tank, supplying the fermented mixture to a clarifier tank, collecting settled sludge and recycling all or part thereof to the fermentation tank, and drawing off the treated waste liquor from the clarifier.
The drawing forming a part of this specification shows schematically a method and apparatus adapted to some aspects of the present invention. The drawing shows a feeding tank into which are supplied spent sulfite liquor (SSL), nutrients, and any pH control material required. The SSL will normally contain about 100-500 parts per million (ppm) suspended solids, after gross filtration, mostly in the form of pulp fiber debris. It will frequently also contain about 70,000 to 111,000 ppm of dissolved solids corresponding to 18,000 to 34,000 ppm, (sometimes 28,000 to 33,000), of biochemical oxygen demand (BOD).
An advantage of this invention is that the SSL may be treated either without dilution or with minor dilution as compared with normal treatment processes which involve dilution of the order of 10:1 and consequent process difficulties and apparatus capacity requirements due to the handling of a large volume of liquid.
A preferred procedure involves diluting the SSL to about 24,000 to 25,000 ppm BOD before treating it, as a condition for efficient BOD removal and autolytic operation. That mixture from the feeding tank is pumped to a "fermentor" or digester tank supplied with an air inlet, typically providing air under pressure to the lower part of the tank at a rate of about 0.6 vvm (vvm is volume of air/volume of liquid/minute). Agitation means are provided, such as the propeller shown in the drawing. In a steady state the liquid will contain about 36,000 ppm suspended solids, some of the dissolved solids having been converted to suspended solids. It may have a BOD of 5,000 at the steady state, and the non-biodegradable dissolved solids will still remain at about 66,000. There is a means for collecting the foam resulting from the aeration and agitation and transferring it to the clarifier tank at a point above the liquid level in that tank. The tank in this drawing contains a partition extending below the level of the liquid to retain the foam in one part of the clarifier tank. A slit in the partition permits pressure equalization with the other part of the clarifier tank head. The foam can be broken more quickly by the use of standard techniques known in the art, if necessary. In that other part the treated SSL is drawn off by overflow, and transported out of the system as effluent.
The foam transferred from the fermentor to the clarifier exhibits a suspended solids content much lower than the material in the fermentor, typically around 12,000 ppm. The sludge from the clarifier is pumped through the sludge recycle mechanism back to the fermentor or aeration tank. This sludge typically contains around 36,000 to 45,000 ppm suspended solids. The system appears to provide a relatively quick settling sludge, for sludge densities of this type, which is recycled in accordance with good activated sludge practice, thus assisting in maintaining the autolytic activated sludge system. The effluent overflowing in the clarifier is brown in colour due to the presence of lignaceous materials. It has a BOD of around 4,800 ppm. It can be seen that there has been a considerable reduction in the BOD and dissolved solids, with a net decrease in the volume of the liquid. This is due to the evaporative effect of the off-gas stream. There is typically no production of sludge requiring disposal although there is always a small amount of suspended solids in the effluent from the clarifier.
TREATMENT OF SSL
The characteristics of typical SSL from the pulp mill digesters may be known from the following range of compositions found among filtered samples received from the Iroquois Falls Ontario plant over a period of three years.
______________________________________pH 2.9-4.5BOD.sub.5 20,800-33,900 ppmCOD 80,900-115,200 ppmdissolved Solids 71,500-111,700 ppmNon-Settleable 0-200 ppmSuspended SolidsPortion of total up to 300 ppmBOD.sub.5 associatedwith non-settle-able suspendedsolids______________________________________
Spent sulfite liquor contains sufficient amounts of carbonaceous substrates and essential minerals for a prosperous biological system, but may be found to have insufficient amounts of nitrogen and phosphate under some conditions. As an example, the SSL used in many of these experiments has a chemical analysis as shown.
TABLE______________________________________Mineral Concentration (ppm)______________________________________Ca.sup.++ 190K.sup.+ 125Mg.sup.++ 28Al.sup.+++ 7Fe.sup.++, Fe.sup.+++ 7N (Kjeldahl) 6PO.sub.4.sup.- 6______________________________________
We have found by tests conducted on SSL taken directly from the digesters of six different pulp mills, that the operative range of residual sulfur dioxide concentration was in the range of 0.24 to 0.78% weight/volume.
In the case of one sample of SSL it was found that enrichment with various nitrogen and phosphorus compounds improved the rate of COD (chemical oxygen demand) reduction.
TABLE 2______________________________________Batch studies with 100 ml SSL in 500 ml shake flasksBOD.sub.5 :N:P = 75:5:1 COD reduction (%)Chemicals tested after 7 days of incubation______________________________________NH.sub.4 H.sub.2 PO.sub.4 16.3Ca(NO.sub.3).sub.2 15.1K.sub.2 HPO.sub.4H.sub.3 PO.sub.4 14.5NH.sub.4 OHControl (no chemicals added) 10.2______________________________________
TABLE 3______________________________________BOD.sub.5 AND COD REDUCTION RANGESContinuous reactor study in 8 liter reactorBOD:N:P: = 100:5:1Chemicals BOD.sub.5 Reduction COD, % Reduction______________________________________K.sub.2 PO.sub.4 60-84 15-28KH.sub.2 PO.sub.4+NH.sub.4 OH______________________________________ The ratio of phosphates used: ##STR1##
Table 4 shows a comparison between the results obtainable in the present process, as compared with prior art processes. In this table the following terms are used:
lb BOD/1000 cu ft=lb BOD applied per day, per 1000 cu ft of liquid volume in the aeration tank
lb BOD/lb mass=lb BOD applied per day, per lb SS in the aeration tank
Aeration Period=Retention time of the raw waste water flow in the aeration tank, expressed in hours
Average Return Sludge Rate=Activated sludge returned, as a percentage of the raw waste water influent
SS=suspended solids
The prior art data in Table 4 is taken from Table 11-4, p. 507, Water Supply and Pollution Control, 2nd ed. Int'l Textbook Co., 1971, by Clark, Viessman and Hammer.
TABLE 4__________________________________________________________________________GENERAL LOADING AND OPERATIONAL PARAMETERS FORACTIVATED-SLUDGE PROCESSES BOD LOADING Feed Fermentor Aeration Average Return BOD Removal lb of BOD lb of BOD Period, Sludge Rates, Efficiency,Process 1000 cu ft lb SS hours percent percent__________________________________________________________________________HIGH RATE 100 up 0.5-1.0 2.5-3.5 100 85-90(complete mixing)STEP AERATION 30-50 0.2-0.5 5.0-7.0 50 90-95CONVENTIONAL 30-40 0.2-0.5 6.0-7.5 30 95(tapered aeration)CONTACT 30-50 0.2-0.5 6.0-9.0 100 85-90STABILIZATIONEXTENDED 10-30 0.05-0.2 20-30 100 85-95AERATIONFOAM FLOTATION - 400 0.2 30-70 .gtoreq.30 80-90AUTOLYTIC-(presentprocess data)__________________________________________________________________________
The present microbial system has been identified by taxonomy studies as being a mixture of five fungi being yeast and yeast-like bodies of these five species. The five species have been isolated from the mixed culture system several times under different conditions, e.g. from lyophilized material, repeatedly transferred stock culture, etc. Isolate No. 5 exhibited autolytic activity (in plate culture) and the capability to ferment and assimilate glucose, galactose, maltose and sucrose in liquid culture. Isolate No. 4 was also autolytic and assimilated sugars. The speices were identified as follows:
TABLE 5______________________________________Mixed Culture, Microbial Population NAME AND MORPHOLOGICAL FEATURESISOLATE NO. (Plate Cultures on Agar)______________________________________1 Phialophora jeanselmei (Langeron) Emmons . . . New columns black and yeast-like, changing to woolly green mycelial colonies producing spores in clusters at the tips of short stalks and long tapered phialides without collarettes.2 Phialophora richardsiae (Nannfeldt apud Melin & Nannf.) . . . Velvety brown mycelial colonies producing single spores on flask shaped phialides with conspicuous collarettes.3 Hyalodendron lignicola Diddens . . . Powdery white mycellia colonies with conidiophores bearing branches chains and clusters of spores. Refractile spore scars4 Trichosporon infestans (Moses & Vianna) Ciferri & Redaelli . . . New colonies white and yeast-like, changing to sparsely branched mycelial colonies with clusters of blastospores produced directly from hyphae at the junction of cells, also arthospores produced by fragmentation of hyphae.5 Candida tropicalis (Castellani) Berkhout . . . White, paste-like colonies fringed by mycelia. Blastospores produced in whorls directly from unburdened hyphae at cell junctions. (In liquid culture, abundance of budding ovoid cells and pseudomycelial fragments).______________________________________
Thus the present invention has provided a microbial culture system acclimatized to undiluted SSL and having five principal components, all fungi, which have been identified through isolation and accepted taxonomical procedures as the following:
1. Phialophora jeanselmei (Langeron) Emmons
2. Phialophora richardsiae (Nannfeldt apud Melin & Nannf.) Conant
3. Hyalodendron lignicola Diddens
4. Trichosporon infestans (Moses & Vianna) Ciferri & Redaelli
5. Candida tropicalis (Castellani) Berkout
Specimens of the identified isolates have been deposited in the following culture collections:
______________________________________American Type Culture Collection July 1, 197612301 Parklawn DriveRockville, MarylandU.S.A.1. Accession No. ATCC 20,4822. Accession No. ATCC 20,4833. Accession No. ATCC 20,4844. Accession No. ATCC 20,4855. Accession No. ATCC 20,486Culture CollectionThe University of Western OntarioLondon, OntarioCanada1. Accession No. UWO BE222. Accession No. UWO BE053. Accession No. UWO BE034. Accession No. UWO BE325. Accession No. UWO BE07______________________________________

EXAMPLE 1
In the early stages the ability of the mixed culture system to remove BOD was partially inhibited by the sulfur dioxide in the SSL. By continuous exposure of the mixed culture system to increasing concentrations of SSL it was eventually adapted and acclimatized to the typical levels of sulfur dioxide and dissolved solids present in the undiluted waste. Table 6 shows the initial steps involved in adapting the sewage culture to full strength SSL.
TABLE 6______________________________________Acclimitization of the MixedCulture in Shake Flasks IncubationSteps Culture Medium Time (weeks) Resulting Culture______________________________________1 Stock Culture 10 ml 1 A 20% SSL 90 ml2 Culture A 10 ml 1 B 40% SSL 90 ml3 Culture B 10 ml 1 C 60% SSL 90 ml4 Culture C 10 ml 1 D 80% SSL 90 ml5 Culture D 10 ml 1 Acclimitized 100% SSL 90 ml Culture______________________________________
The microbial system used was obtained from sewage containing the usual broad spectrum of bacteria, protozoa and fungi. It has been acclimatized to media based on spent sulfite liquor from three high-yield sulfite pulp mills. By selective enrichment the mixed culture system has been stabilized and maintained continuously for more than four years. The same five individual cultures have been consistently isolated from repeatedly transferred stock culture and from cultures obtained from freeze-dried and frozen material harvested from the pilot-scale reactor. These five cultures have been positively identified as known fungi; they represent the principal components of the system. Bacteria and protozoa have not been detected in this stable system, and do not appear to have the ability to adapt to the system. They do not contribute to the operation of the present process.
EXAMPLE 2
Foaming capability associated with a high yield sulfite spent liquor is shown in Table 7. These tests were conducted by aerating 200 ml of SSL at 0.188, 0.250 and 3.13 vvm (volume of air per volume of waste liquid, per minute) and measuring the foam generated. This was done by aerating exactly 5 minutes at the designated vvm, then halting the air flow and observing the rate of foam collapse. Time 0 is the moment the air flow is turned off. The foam is measured at intervals until it becomes stable (or up to 30 minutes). The vvm is calculated by dividing the observed air flow rate (ml/minute) by the liquid volume (200 ml in this experiment). For example, with the pressure regulated to give a flow rate of 37.5 ml air/min., and 200 ml of SSL in the column, vvm=37.5/200=0.187. In Table 7 SS means suspended solids.
Table 7 shows that raw SSL and nutrient treated SSL at pH 3.9 and 7.0 respectively produce copious quantities of foam. Fermentation broth of SSL produced less foam at pH 3.0-3.2 but more than adequate quantities to operate the process.
On the basis of tests conducted on raw SSL we infer that the propensity of the formentor broth to foam would not vary significantly over a pH range of 3 to 9. Also the rate of foam collapse remains approximately constant up to about the neutral point, above which it significantly decreases.
TABLE 7__________________________________________________________________________RATE OF COLLASPE OF FOAM Volume of foam in ml at time shown Aeration time in minutesLiquid (vvm) 0 1 2 3 4 5 6 11 12 20 30__________________________________________________________________________"Raw" SSL 0.1875 85 85 85 85 85 85 85 85 25 25 25pH of 3.9 0.2500 125 125 125 125 125 125 125 125 25 25 25and a SS of 0.3125 220 220 220 220 220 220 220 220 30 30 30200 ppmSSL with 0.1875 75 75 75 15 15 15 15 15 12 10 10nutrients 0.2500 120 120 120 15 15 15 15 12 10 10 10pH of 7.0 0.3125 170 120 15 15 15 15 15 15 12 10 10SS of 200 ppmFermentation 0.1875 40 25 7 3 0broth pH of 0.2500 50 30 10 3 03.15 and SS 0.3125 155 100 40 15 5 2 0of 33,300 ppm__________________________________________________________________________
EXAMPLE 3
The mixed culture system used in this example represents a culture system which has been partially adapted to SSL and the typical levels of sulfur dioxide in SSL. This culture could grow in the presence of low levels of sulfur dioxide (0.32%) and demonstrated the potential for adapting to higher levels (0.50%). The capability of the mixed culture system to remove COD and adapt to 0.52% SO.sub.2 is shown in Table 8. At levels of sulfur dioxide above 0.52% the mixed culture system is slightly inhibited but still operates satisfactorily. Levels of 1.0% sulfur dioxide can be expected to be far more inhibiting. This is an upper limit of levels encountered in the production processes. When the mixed culture was adapted to the higher levels of sulfur dioxide (greater than 0.32%) it showed an improved ability to remove the biodegradable organic components present in such a liquor.
TABLE 8______________________________________Tolerance to SO.sub.2Tolerance Limit: Maximum 0.32% SO.sub.2 (w/v) based only on stepwise dilution of SSL, and use of the original partially adapted culture. COD After 10 DaysSSL SO.sub.2, % (w/v) Incubation % Reduction______________________________________Original SSL 0.52 18Diluted SSL (60%) 0.32 29Stripped SSL, 0.32 30boiled 5 hr.______________________________________
EXAMPLE 4
A continuous foam-activated sludge (mixed culture) process was operated in separate experiments in a 14 liter reactor for periods of 5, 6 and 78 days. Only foam-sludge was transferred to the clarifier and all solids were recycled to the activated sludge unit. No sludge wastage was required even when the continuous operation was run for 78 days. The percent removal of BOD and COD are shown in Table 9, with no allowances for increased concentration of effluent arising from aeration evaporation losses.
TABLE 9______________________________________BOD.sub.5 and COD Removal byFoam-Activated Sludge ProcessType of Original Values of Days %Experiment COD, BOD.sub.5 (ppm) Operated Reduction______________________________________Continuous Run BOD.sub.5 24,000 5 75No. 1 COD 100,000 25Continuous Run BOD.sub.5 24,500 6 84No. 2Continuous Run BOD.sub.5 23,000 78 79*No. 3______________________________________ *14 day average
EXAMPLE 5
A continuous foam-activated sludge experiment was conducted for 78 days in which the retention time of waste in the main activated sludge chamber was the main process variable evaluated. The experiment was conducted in a 14 liter CHEMAP reactor operated at an 8 liter capacity. The rate of recycle of sludge from the clarifier was maintained at 1.08 liter/day through the entire experiment. The daily percent BOD removal varied from 55 to 84. Absolutely no sludge wastage was required.
Some of the operating characteristics of the process during that period are summarized in Table 10.
EXAMPLE 6
Some wastes do not contain all the nutrients desired for optimum efficiency in operating an efficient bio-waste treament process. Nutrients required by microbes are well defined in the literature. Sources of nitrogen and phosphorus often must be added to the waste to obtain rapid removal of waste organic compounds.
The levels of nutrients employed in this process are shown in Table 11.
TABLE 10__________________________________________________________________________Effect of Retention Time on Removal of BOD and Soluble Solids(based on SSL analysis before (and after) nutrient addition) BOD.sub.5 Soluble****Portion Duration SSL removal*** solidsof run* of test feed rate Recycle/feed Retention time** % removalday no. days liters/day ratio days before (after) %__________________________________________________________________________5-9 5 2.16 0.50 2.47 58 (61) 1710-18 9 2.16 0.50 2.47 75 (77) 2019-29 11 2.50 0.48 2.23 71 (73) 1553-66 14 2.50 0.48 2.23 77 (79) 2530-52 23 3.00 0.36 1.96 66 (69) 1767-72 6 3.00 0.36 1.96 76 (78) 2173-78 6 3.50 0.31 1.75 58 (61) 15__________________________________________________________________________ *batchwise operation prior to day 5 **calculation of retention time in days (t"): ##STR2## where V = volume of liquid in reactor in liters F = feed rate in liters/day F' = sludge recycle rate in liters/day ***uncorrected for evaporation effects ****raw spend sulfite liquor to system at 8.9% dissolved solids
TABLE 11__________________________________________________________________________Mode of Operation and Nutrients Requirements Added Weight Incubation Ratio % ReductionType of Study (days) Chemicals Added BOD.sub.5 :N:P (gms) COD BOD.sub.5__________________________________________________________________________Batch operation in 7 NH.sub.4 H.sub.2 PO.sub.4 75:5:1 16.3 --500 ml shake flasks 7 Ca(NO.sub.3).sub.2 75:5:1 15.1 --containing 100 ml 7 H.sub.3 PO.sub.4 75:5:1 14.5 --of material NH.sub.4 OH 7 None (control).sup.a 10.2 --Batch operation 4 K.sub.2 HPO.sub.4 2:1 100:5:1.sup.b 15 60(Chemap).sup.c mole KH.sub.2 PO.sub.4 ratio NH.sub.4 OH 7 same same -- 84Continuous 5 same same 25 75operation 6 same same -- 84(Chemap).sup.c 78 same same -- 79.sup.c (nsw).sup.dContinuous 132 same same 28 84.sup.foperation 48 (nsw)liter Reactor 21 same 100:2.5:0.5 -- 66.sup.gcontaining about (nsw)42 l. of material 16 same 100:5:0.5 27 70.sup.h (nsw)__________________________________________________________________________ .sup.a Untreated SSL levels: 6 ppm N, 5 ppm PO.sub.4 .sup.b Equivalent to 1.33 g NH.sub.3, 0.82 g K.sub.2 HPO.sub.4, 0.32 g NH.sub.2 PO.sub.4, along with approximately 2.0 g NaOH per liter of SSL (as needed to adjust to pH 7) .sup.c Fourteen liter "Chemap" (trade mark) reactor containing 8 liters o material .sup.d (nsw) No sludge wastage .sup.e 14 day average .sup.f 11 day average .sup.g 14 day average .sup.h 7 day average
EXAMPLE 7
The following tables 12-14 show segments of the experiments described below, dealing with the 256 days of operation of the 48 liter reactor.
Summary of the 48 Liter Reactor Studies
(1) Days 1-87: start up and harvesting mode experiments
(2) Days 87-219: (132 days) autolytic operation at unchanged chemical addition levels
(3) Days 219-240: (21 days) autolytic operation with no NaOH, half previous NH.sub.3 level and half previous phosphate level
(4) Days 240-256: (16 days) autolytic operation with no NaOH, NH.sub.3 restored to original level, but half phosphate level maintained
TABLE 12______________________________________FEED CHEMICALS REDUCTIONAND BOD.sub.5 ASSIMILATION TRENDContinuous Reactor Study in 48 Liter Reactor with nutrientchemicals added as K.sub.2 HPO.sub.4 ; KH.sub.2 PO.sub.4 ; and NH.sub.4OH. Steady StateSegment of Weight Ratio BOD.sub.5 ReductionPeriod BOD:N:P Range %______________________________________2 100:5:1 80-883 100:2.5:0.5 61-684 100:5:0.5 63-78______________________________________
Periods 3 and 4 cover a time during which additional pilot-scale laboratory studies were made, primarily to examine the feasibility of lowering the chemical requirement of the proposed industrial design. When operated continuously in the autolytic mode, the system could reasonably be expected to require minimal amounts of added nutrients (nitrogen and phosphorus) in the feeding medium since these are not wasted in the form of harvested biomass. Also, a considerable saving in chemical cost could be achieved by eliminating the use of alkali and/or strong acid for neutralization of the SSL feeding medium, as the active culture is known to tolerate a fairly wide pH range.
Accordingly, two final reactor run periods 3 and 4 were made using reduced levels of nutrients in the feed, and omitting the neutralization step. In the first experiment levels of added ammonia and mixed phosphates in the feed were dropped to half their previous values. In the second, the lower level of phosphate was maintained but the ammonia level was restored to the previous higher value. There was no adjustment of feed pH in either experiment, but pH measurements were made after the nutrient additions. All other operating parameters were the same as for the previous optimum autolytic mode. Prior to the final experiments, the reactor had been maintained in this optimum mode without harvesting, although a small increase in the SS level was observed.
The results from these experiments indicate that substantial savings in chemical nutrient costs are possible without excessive loss of BOD removal efficiency.
In addition, for design purposes two sets of temperature change date were recorded for the pilot scale reactor system (during the maintenance period between periods 1 and 2) immediately following the temporary suspension of thermostatic controls. The "air in" and "air out" temperatures were measured by means of thermometers. The unjacketed reactor temperature was seen to decrease by only 5.degree. C. over periods of eight and twelve hours respectively. These tests appear to demonstrate the close balance between energy input and output requirements of the system when operated in the autolytic mode.
TABLE 13 % BOD.sub.5 REMOVAL Suspended CALCULATED (Based Solids on BOD.sub.5 of Feed (SS) ppm pH Dissolved Solids, ppm BOD.sub.5, ppm 24 Hours Previous) Clari- Clari- Clari- Clari- Corrected Portion Added nutrients fier fier fier fierfor of Weight Ratio Day Re- Efflu- Re- Efflu- "Raw" Prep'd Re- Efflu- "Raw" Prep'd Re- Efflu- Ob- Eva- OPERATING DATA FOR Run BOD:N:P No. actor ent Feed actor ent SSL Feed actor ent SSL Feed actor ent served poration FERMENTOR SYSTEM 2 100:5:1 1 30,500 -- 7.0 4.4 -- 72,100 76,900 66,300 -- 21,500 22,000 7,100 -- -- -- Calculated for BOD.sub.5 Loading, .dwnarw. 2 28,000 1,100 .dwnarw. 4.4 3.6 .dwnarw. .dwnarw. 68,700 69,200 .dwnarw. .dwnarw. 6,700 6,400 71 80 295 g/day or 0.65 lb/day (Maximum 3 29,200 -- .dwnarw. 4.8 -- .dwnarw. .dwnarw. 66,000 -- .dwnarw. .dwnarw. 7,000 -- -- -- chemicals 4 28,500 1,500 .dwnarw. 5.3 4.7 .dwnarw. .dwnarw. 66,900 65,600 .dwnarw. .dwnarw. 7,400 6,300 71 81 Calculated BOD.sub.5 Removal, additions 5 28,400 -- .dwnarw. 4.4 -- 70,600 74,400 68,400 -- 23,300 23,900 7,000 -- -- -- 248 g/day or 0.55 lb/day .dwnarw. 6 32,300 2,800 .dwnarw. 3.7 4.4 .dwnarw. .dwnarw. 64,200 65,000 .dwnarw. .dwnarw. 5,700 5,400 77 85 NaOH added 7 32,400 -- .dwnarw. 3.5 -- .dwnarw. .dwnarw. 66,000 -- .dwnarw. .dwnarw. 4,300 -- -- -- Recycle/feed ratio, to adjust 8 28,400 -- .dwnarw. 3.3 -- .dwnarw. .dwnarw. 65,400 -- .dwnarw. .dwnarw. 5,600 -- -- -- F'/F = 0.432 feed pH to 7) 9 29,200 1,600 .dwnarw. 3.0 3.4 .dwnarw. .dwnarw. 64,800 65,100 .dwnarw. .dwnarw. 4,400 4,900 80 86 .dwnarw. 10 30,100 -- .dwnarw. 2.9 -- .dwnarw. .dwnarw. 63,000 -- .dwnarw. .dwnarw. 5,400 -- -- -- Retention Time = 2.23 days .dwnarw. 11 30,200 1,200 .dwnarw. 2.9 3.0 .dwnarw. .dwnarw. 66,200 67,300 .dwnarw. .dwnarw. 5,200 4,300 82 88 .dwnarw. Averages: 29,700 1,600 7.0 3.9 3.8 71,400 75,600 66,000 66,400 22,400 23,000 6,000 5,500 76 84 Aeration = 0.60 v.v.m. 3 100:2.5:0.5 1 46,500 2,500 5.8 2.4 2.4 23,300 24,100 11,000 10,400 57 68 .dwnarw. 2 45,300 1,900 .dwnarw. 2.3 2.4 .dwnarw. .dwnarw. 11,800 11,000 54 67 (minimum 3 45,700 1,500 6.0 2.2 2.4 25,100 26,600 11,000 11,500 52 65 Same as above chemicals 4 44,400 1,300 .dwnarw. 2.2 2.3 .dwnarw. .dwnarw. 11,600 11,900 55 67 addition) 5 44,700 1,700 .dwnarw. 2.2 2.3 24,600 24,000 12,300 11,900 55 67 except .dwnarw. 6 44,400 1,300 6.0 2.2 2.3 .dwnarw. .dwnarw. 12,600 11,800 56 68 (no NaOH) 7 45,500 1,300 .dwnarw. 2.2 2.4 (NO DISSOLVED .dwnarw. .dwnarw. 12,200 10,900 54 67 Calculated BOD.sub.5 Removal .dwnarw. 8 45,600 1,000 .dwnarw. 2.3 2.4 SOLIDS DATA) .dwnarw. .dwnarw. 11,600 10,500 55 68 (based on 66% Average) .dwnarw. 9 45,200 -- .dwnarw. 2.2 -- .dwnarw. .dwnarw. -- -- -- -- = 194 g/day or 0.43 .dwnarw. 10 45,200 1,100 .dwnarw. 2.2 2.4 23,300 24,100 11,200 11,200 53 66 lb/day .dwnarw. 11 44,800 1,000 6.0 2.2 2.3 .dwnarw. .dwnarw. 12,300 12,200 49 63 .dwnarw. 12 45,500 1,200 .dwnarw. 2.4 2.4 .dwnarw. .dwnarw. 13,500 12,700 47 61 .dwnarw. 13 41,000 1,200 .dwnarw. 2.3 2.4 .dwnarw. .dwnarw. 12,800 11,800 51 64 .dwnarw. 14 41,700 700 .dwnarw. 2.3 2.2 .dwnarw. .dwnarw. 12,200 11,800 51 64 .dwnarw. .dwnarw. .dwnarw. .dwnarw. .dwnarw. Averages: 44,700 1,400 6.0 2.3 2.4 24,100 24,700 12,000 11,500 53 66 4 100:5:0.5 1 44,600 1,600 6.8 2.2 2.3 .dwnarw. 23,200 11,900 12,600 46 52 Same as above, .dwnarw. 2 44,500 2,200 .dwnarw. 2.4 2.4 .dwnarw. .dwnarw. 11,400 12,600 46 52 (lowered 3 44,000 1,600 7.6 2.6 2.6 .dwnarw. 23,000 10,400 12,200 47 53 except phosphates, 4 43,400 1,600 .dwnarw. 3.0 3.0 .dwnarw. .dwnarw. 10,200 10,400 55 59 no NaOH) 5 41,500 1,100 .dwnarw. 3.3 3.2 .dwnarw. .dwnarw. 9,800 10,400 55 59 Calculated BOD.sub.5 Removal .dwnarw. 6 -- -- 7.3 -- -- 24,100 24,400 -- -- -- -- (based on 70% Average) .dwnarw. 7 41,900 1,000 .dwnarw. 4.8 4.6 (NO DISSOLVED .dwnarw. .dwnarw. 10,100 10,100 59 63 = 206 g/day or 0.45 .dwnarw. 8 42,800 1,300 .dwnarw. 4.8 4.6 SOLIDS DATA) .dwnarw. .dwnarw. 8,900 10,000 59 63 lb/day .dwnarw. 9 43,300 700 .dwnarw. 4.9 5.0 .dwnarw. .dwnarw. 8,800 9,200 62 Av. 70 66 .dwnarw. 10 43,900 4,000 8.0 5.5 5.4 23,000 23,500 8,300 8,400 66 69 .dwnarw. 11 47,900 1,200 .dwnarw. 6.1 5.7 .dwnarw. .dwnarw. 7,200 7,900 67 70 .dwnarw. 12 49,200 3,200 .dwnarw. 6.5 5.8 .dwnarw. .dwnarw. 7,400 8,500 64 Av. 68 .dwnarw.13 -- -- .dwnarw. -- -- .dwnarw. .dwnarw. -- -- -- 66 -- .dwnarw. 14 53,900 1,100 .dwnarw. 6.6 6.0 .dwnarw. .dwnarw. 6,200 6,400 73 76 .dwnarw. 15 51,200 800 .dwnarw. 6.6 5.8 .dwnarw. .dwnarw. 5,800 6,000 75 78 .dwnarw. Averages: 45,500 1,600 7.4 4.6 4.3 23,600 23,500 9,000 9,600 60 64
TABLE 14______________________________________SUMMARY OF AVERAGES OF DATA FROM BESTPERIODS, THREE LEVELS OF NUTRIENT CHEMICALSIN 48 LITER FERMENTOR SYSTEM PERIOD 2 3 4______________________________________Weight Ratio, BOD.sub.5 :N:P 100:5:1 100:2.5:0.5 100:5:0.5Av. SS, Reactor Broth 29,700 44,700 45,500ppm Clarifier Effluent 1,600 1,400 1,600Av. pH Feed 7.0 6.0 7.4 Reactor Broth 3.9 2.3 4.6 Clarifier Effluent 3.8 2.4 4.3Av. Dissolved "Raw" SSL 71,400 -- --Solids ppm Prepared Feed 75,600 -- -- Reactor Broth 66,000 -- -- Clarifier Effluent 66,400 -- --Av. BOD.sub.5, "Raw" SSL 22,400 24,100 23,600ppm Prepared Feed 23,000 24,700 23,500 Reactor Broth 6,000 12,000 9,000 Clarifier Effluent 5,500 11,500 9,600Av. % BOD.sub.5 Removal, Calc'dA. Uncorrected 76 53 60 (66*)B. Corrected for Evap'n 84 66 64 (70*)Av. Daily BOD.sub.5 Loading, Calc'd 295 g 295 g 295 gAv. Daily BOD.sub.5 Loading, Calc'd 0.65 lb 0.65 lb 0.65 lbAv. Daily BOD.sub.5 Removed, Calc'd 248 g 194 g 206 g*Av. Daily BOD.sub.5 Removed, Calc'd 0.55 0.43 lb 0.45 lb______________________________________ All Periods, Recycle/Feed ratio = F'/F = 0.432 Reactor Retention time = 2.23 days Aeration: = 0.60 vvm *Average BOD.sub.5 removal for final eight days.
EXAMPLE 8
Large Scale Continuous Fermentation
A scaled up, preliminary process design is based on the estimated output of undiluted SSL at the Iroquois Falls pulp mill, 310,000 IG/day, as shown in Table 15. These values were calculated for maximum nutrient levels, period 2 of Example 7.
TABLE 15______________________________________PROCESS DESIGN SUMMARY______________________________________SSL Flow Rate 310,000 IG/dayCOD Loading Rate 310,000 Lb/dayBOD.sub.5 Loading Rate 75,000 Lb/dayDissolved Solids Loading Rate 280,000 Lb/dayK.sub.2 HPO.sub.4 Requirement 1.28 Tons/dayKH.sub.2 PO.sub.4 Requirement 0.50 Tons/dayNH.sub.3 Requirement 2.06 Tons/dayNaOH Requirement 3.10 Tons/dayVolume of Aeration Tank 192,000 Ft.sup.3Depth of Aeration Tank 40-50 FtHead Space of Aeration Tank 3-6 FtOxygen Requirement(a) Based on ultimate BOD 92,500 Lb O.sub.2 /day(b) Based on BOD.sub.5 62,900 Lb O.sub.2 /dayAeration Tank Retention Time 2.23 DaysPower Requirement forDeep Tank Reactor(a) Mixing Requirement 69.5 HP(b) Oxygenation Requirement 1100 HPCooling Water RequirementFor Deep Tank Reactor 5,000 Tons Water/day(Based on 10% evaporation loss)Heating RequirementFor Deep Tank Reactor 158 .times. 10.sup.2 Lb steam/day(Based on 20% evaporation loss) (Saturated, 212.degree. F., one atm)Clarifier Area Requirement 5,200 Ft.sup.2Clarifier Depth 12 FtClarifier Retention Time 1 Day (approx.)______________________________________ Recalculated Chemical Requirements for Period 4 of Example 7. K.sub.2 HPO.sub.4 0.64 tons/day KH.sub.2 PO.sub.4 0.25 tons/day NH.sub.3 2.06 tons/day NaOH none
EXAMPLE 9
A study was made to determine the differences in settling behavior between the fermentor broth and the collapsed foam from the material in the clarifier. It was found that the collapsed foam settled much more rapidly. Table 16 shows the rapid settling of the collapsed foam material compared to undiluted fermentor broth. Even when diluted to the same suspended solids concentration the fermentor broth settled more slowly.
Corresponding 1000 ml samples of collapsed foam and liquid reactor broth were collected during continuous operation of the pilot-scale apparatus in the optimum mode for BOD removal, as set out in Example 7.
Suspended solids levels (SS) were determined in both samples. Settling rate studies for both samples at full strength were made by recording the levels of settled sludge in 1000 ml graduated cylinders at 15 minute intervals for periods up to 150 minutes. Parallel studies were made substituting:
(a) a 1:1 dilution of the collapsed foam
(b) a calculated dilution of the reactor broth having the same SS as the full strength collapsed foam, and
(c) a calculated dilution of the reactor broth having the same SS as the 1:1 collapsed foam (a).
Sludge in the collapsed foam settled much more rapidly than that in the reactor broth. Improved reactor broth settling was obtained by diluting it approximately 3x to the same SS as the collapsed foam. When diluted to SS of about 8000 ppm the settling rates were more nearly in agreement but the solids in collapsed foam still settled much more rapidly.
TABLE 16______________________________________SLUDGE SETTLING RATES IN COLLAPSEDFOAM AND REACTOR BROTH SETTLED CLARI- SLUDGE SUS- SLUDGE FIED SET-SAMPLE PENDED VOLUME ZONE TLINGDESCRIP- SOLIDS ml ml RATETION ppm (30 min.) (30 min.) calculated*______________________________________Collapsed 16,600 970 30 120Foam, fullstrengthCollapsed 8,300 900 100 290Foam, 1:1dilutionReactor 48,400 1,000 0 <2Broth, fullstrengthReactor 16,600 990 10 15Broth, dilutedReactor 8,300 945 55 190Broth, diluted______________________________________ *ml decrease in sludge/hour: calculated from slope of curve from data plotted as sludge volume vs. time elapsed.
COMPARISON WITH OTHER ACTIVATED SLUDGE PROCESSES
Operational characteristics of the autolytic mode which produced maximum BOD removal were calculated in accordance with Metcalf & Eddy, Inc., Wastewater Engineering: Collection, Treatment, Disposal, McGraw-Hill, N.Y., pp. 393-403; and pp. 497-498 (1972) and compared with these of other modifications of the activated sludge process. Several of these known processes claim 85% BOD removal efficiency also, but are restricted to handling much less concentrated waste. The mean cell residence time, .theta..sub.c, is defined by .theta..sub.c =X.sub.m /(.DELTA.X/.DELTA.t).sub.m where X.sub.m is the total biomass in the system and (.DELTA.X/.DELTA.t.sub.m) is the biomass withdrawn daily from the system. This material is wasted as unsettleable solids in the treated effluent. The calculated .theta..sub.c value was 95 days, or from three to twenty times longer than any of the conventional processes including extended aeration (max. 30 days). It is expected that the present process will yield a mean cell residence time higher than 30 days, and in most cases 60 or higher. In a more preferred form it should yield a mean cell residence time of 90 days or higher.
The recycle ratio, Q.sub.r /Q is the ratio of the flow rate of recycled sludge to that of fresh feed. Here the calculated value was 0.43, within the range of 0.25 to 0.50 for the other processes. The food-to-microorganism ratio, U, was 0.23 lb. BOD.sub.5 /lb MLVSS-day, or generally similar to that for other processes with the exception of modified-aeration (U=1.5-5.0). The volumetric BOD loading, however, was calculated to be 1,430 lb BOD.sub.5 /1000 cu. ft. This is ten to one hundred times as high as any of the others possibly excepting the high-rate process (100-1000 lb/cu.ft.). The reactor MLSS was 30,000 mg/liter, generally ten times higher than for conventional treatment processes. Experience has shown that even higher levels, up to 55,000 mg/liter can be tolerated.
The (reactor) hydraulic retention time, V/Q was 2.23 days (54 hours), somewhat longer than average; the maximum cited for the extended aeration process was 36 hours. For the treatment system as a whole, including the clarifier, the hydraulic retention time was calculated to be 3.0 days.
While we have described some forms of our invention, including the best modes known to us for carrying out the invention, the protection afforded to this invention should be limited only by the scope of the appended claims.

Number	Name	Date	Kind
2897148	Laboureur et al.	Jul 1959
3711392	Metzger	Jan 1973

Microbial culture system

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