f/EPA United States Environmental Protection Agency Municipal Environmental Research Laboratory Cincinnati OH 45268 Research and Development EPA-600/S2-81-092 July 1981 Project Summary Chlorine Dioxide for Wastewater Disinfection: A Feasibility Evaluation Paul V. Roberts, E. Marco Aieta, James D. Berg, and Bruce M Chow Chlorine dioxide was compared with chlorine for disinfecting waste- water in laboratory experiments. Chlorine dioxide disinfection was also demonstrated at a full-scale waste- water treatment plant. The criteria compared included coliform kill, in- activation of poliovirus and other indicators, and formation of halogen- ated organic byproducts. Laboratory experiments were con- ducted using mass doses of disinfec- tant and contact time as independent variables. The fractional survival of coliform bacteria was correlated with the project of disinfectant residual * contact time. In general, chlorine dioxide accom- plished a given fractional kill of total coliforms with a smaller product (re- sidual x time) than did chlorine. For a given contact time, the residual re- quired to achieve a given fractional kill of coliforms was 2 to 70 times smaller for chlorine dioxide than for chlorine. Considering both required residual and disinfectant demand, the required doses of the disinfectants were esti- mated to satisfy three assumed coli- form disinfection levels with two types of effluents: conventional acti- vated sludge and filtered, nitrified activated sludge. The required mass doses of the disinfectants were ap- proximately equal for treating con- ventional activated sludge effluent. The required dose of chlorine was approximately 2 to 10 times greater than that of chlorine dioxide for treat- ing filtered, nitrified effluent, depend- ing on the coliform standard. The results of studies conducted at a full- scale plant generally agreed within a factor of two with the predictions from laboratory studies, when com- pared on the basis of the product (residual x time) required to accom- plish a given fractional kill. For the cases likely to be most typical in practice, chlorine dioxide is approximately two to five times as expensive as chlorine for disinfection. On the other hand, chlorine dioxide forms much lower quantities of halo- genated by products and is more ef- fective in inactivating viruses than is chlorine. This Project Summary was devel- oped by EPA's Municipal Environmen- tal Research Laboratory. Cincinnati, OH. to announce key findings of the research project that is fully docu- mented in a separate report of the same title (see Project Report ordering information at the back). Introduction The purpose of this report was to evaluate CI02 as an alternative to con- ventional chlormation for the disinfection of wastewater. The specific objectives were1 1. To assemble and evaluate the available information concerning the chemistry of CIO2 generation and its behavior in aqueous solu- ------- tion, the technology and costs of manufacture, its effectiveness as a disinfectant, and the possible side effects of its use. 2. To establish the dose-effectiveness relationship for CIO2 as a disin- fectant of wastewater after sec- ondary treatment and after various stages of advanced treatment, using the survival of coliform bacteria as a criterion. 3. To compare the effectiveness of CI02 with that of CI2, using a variety of indicators. 4 To demonstrate continuous gen- eration of and disinfection with ClOa to fulfill coliform requirements under conditions representative of wastewater treatment. 5. To prepare a preliminary designfor treatment plants of 0.04, 0.22, 0.44, 2.2, and 4 4 mVs capacity and to estimate the costs of con- struction and operation. 6. To obtain preliminary evidence as to whether the formation of chlori- nated organic byproducts during wastewater disinfection conforms to the results from studies of water disinfection. Procedures and Results In the laboratory, CI02 was generated by reacting NaCI02 solution with H2S04 to produce gaseous CI02, which was purified by passing through a NaCI02 tower before being absorbed into water. The concentration of CI02 in the prepared solution was approximately 2 g/L. In field experiments, CIO2 was generated by continuously mixing NaCI02 solution with either H2SO4, HCI, or CI2 gas in a commercially available reactor system. Chlorine species in the reaction product were determined by a series of methods that entailed measurement of ultraviolet absorbance at 360 mm to determine CIO2; amperometric titration at pH 7 to determine CI02 and CI2; mdometric titration at pH 2 to determine CI02, CI2, and CI02~; lodometric titration in con- centrated acid to determine CI02, CI2, CI02~, and CI03"; and chloride mea- surement by use of the Mercuric Nitrate Method. The sensitivity and precision of the determination are summarized in Table 1. The yields of CI02 using several gen- eration schemes are summarized in Table 2. The yield of CI02 from a con- tinuous generator at full-scale (2 kg CIO2/hour) was higher than the yield observed in a batch process in the Table 1. Sensitivity and Precision of Analyses for the Reaction Yield Study Species Chlorine Dioxide Chlorine Chlorite Clorate Detection Limit, Mol/L 3 x 10~& 5.6 x 70~5 3 x W4 1.8 x W~4 Coefficient of Variation, %* 0.1 0.6 1.7 0.4 precision At Mean Concentration, Mol/L 0.02 0.015 0.013 0.01 ^(Standard deviation divided by mean) * 100 for 5 replicate measurements in distilled water. Table 2. Yield of Chloride Dioxide Type of Generation H2SO* + NaCI02, batch (laboratory) H2S04 + NaCIO2, continuous (field) HCI + NaCI02, continuous (field) Clz + NaCIOz. continuous (field) Ratio of Reactants 1 .7 Mol HzSO* Mol CIOI 2 Mol HzSO* Mol CIO~2 1.4 Mol HCI Mol CIOI 0.52 Mol C/2 Mol CIO~2 Initial Chlorite Cone., M 0.083 1.56 1.35 1.92 Final pH 1.8 2.1 2.2 5.3 Yield, %* 48 51 78.4 ± 4.4 95 + 3.5 n** 1 1 4 2 *Yield as (Mol CIO2 produced/Mot CIO2 feed) •< 100; mean ± standard deviation. **n - Number of trials. laboratory; this is attributed to the higher concentration of NaCI02 used in the full-scale, continuous system. The yield from continuous generation was increased when HCI was substituted for H2SC>4 in the acid-chlorite process. The yield from the chlorine-chlonte process in the continuous generator was 95%, even though a small excess of CI2 (4% above the stoichiometric requirement) was used. Disinfection experiments were carried out using secondary wastewater samples from three plants (Figure 1). The levels of treatment were: conventional acti- vated sludge; nitrified activated sludge; and filtered, nitrified activated sludge. Laboratory disinfection experiments were conducted in a 4-L batch reactor with disinfectant dose levels of 2, 5, and 10 mg/L and contact time levels of 5, 15, and 30 mm as the independent variables in a full factorial design. The density of total cohforms was determined by the membrane filter method; dis- infectant residual concentrations were determined by amperometric titration. The results were correlated as survival ratio, N(t)/N(0), versus the product of residual x contact time (R x t). Typical results from a set of experiments using ClOs to disinfect conventional activated sludge effluent are shown in Figure 2. Full-scale disinfection experiments were carried out at a treatment plant to confirm the reliability of the laboratory data to predict plant performance. Laboratory and field data agreed well for both CI02 and CI2. CIO2 was found to be a more effective disinfectant than CI2 when treating conventional (nonnitrified) activated sludge effluent (Figure 3). This difference was shown to be statistically significant by analysis of variance. When comparing CIOz to CI2 at a given survival ratio, a lesser value of R x t product suffices to achieve a given degree of coliform mactivation when CI02 is used (Figure 3). A similar comparison made for nitrified effluent indicated no appreci- able difference between the two disin- fectants to inactivate coliforms. When these comparisons were made for nitri- fied filtered effluents, however, CI02 was more effective than CI2 based on the same criteria. The costs of disinfection with CIO2 are compared with those of CI2 for six cases corresponding to two levels of pretreat- merit and three total coliform standards ------- Palo Alto WWTP Raw WasTe Primary Treatment Conventional Secondary Sample Point Dublin — San Ramon WWTP Raw Waste Extended Aeration Secondary Treatment with Nitrification Filtration T Disinfection Sample Point San Jose — Santa Clara WWTP Raw Waste Primary Treatment » Conventional Secondary Treatment ^ T1 >am Poi Nitrification Process S ole i it t Filtration |)f| Disinfect/on T ample Sample °oint Point Figure 1. Wastewater treatment plant flow schemes and sampling points for disinfection experiments. (Table 3). Estimates for a 0.44 mVs plant are shown in Table 3; the report presents cost estimates for a range of capacities from 0.04 to 4.4 mVs. The high cost of NaCIOz is responsible for the generally high cost of disinfection with CI02. CI02 offered advantages that compen- sate for its cost being higher than that of chlorine. CI02 was found to be more effective for inactivating inoculated Poliovirus I and natural populations of coliphage than was C\2 in both non- nitrified and nitrified filtered waste- water effluents. ClOa treatment formed no measurable amounts of trihalometh- ane byproducts, whereas Cla treatment formed 0.5 to 5 /jMo\/L of tnhalometh- anes, chiefly chloroform, in experiments using wastewater effluents. Moreover, CIO2 formed negligible amounts of the broader class of halogenated organics measured collectively as total organic halogen (TOX)—less than 10% as much TOX as did chlorine. These advantages of CI02 should be considered, along with the cost-effectiveness comparison based oncoliform kill, to reach decisions on using CI02 as a disinfectant in wastewater treatment. The full report was submitted in ful- fillment of Grant No. R-805426 by Stanford University under the sponsor- ship of the U.S. Environmental Protec- tion Agency. 10' c o N(t)N(0)= [(R x TV1.56Y2 90 "/- = 0.86 * f I I I Mill il i i 11 mil i i 111 ml i i 11 mil Figure 2. 70"1 70° 70 1 702 Residual - Time in mg -mm/L Data correlation for disinfection of conventional activated sludge effluent with chlorine dioxide (laboratory experiments). C-frr2 5/0" I/O-5 Cl 2 as Disinfectant Cl 2 as Disinfectant 10 701 /O Residual - Time in mg -m/n/L Figure 3. Comparison of coliform mactivation by chlorine dioxide and chlorine in conventional fnonmtrified) activated sludge effluent. > US GOVERNMENT PRINTING OFFICE 1981 757-012/7253 ------- Table 3. Summary of Dose Requirements and Costs Type of Effluent Activated Sludge Filtered, Nitrified Activated Sludge Case A B C D E F Total Coliform Standard, N/100 ml 2.2 200. WOO. 2.2 200. WOO. Required Disinfectant Dose, mg/L C/2 CI02 7.89 7.92 2.45 2.90 1.70 2.17 11.15 5.52 2.61 0.60 2.60 0.14 Total Costs, * C/m C/2 0.82 0.58 0.55 0.95 0.63 0.58 3 C/02 8.72 3.43 2.24 6.21 1.11 0.61 * January 1980 costs. 0.44 m3/s plant. Paul V. Roberts, E. Marco A/eta, James D. Berg, and Bruce M. Chow are with the Civil Engineering Department, Stanford University, Stanford, CA 94305 Mark C. Meckes is the EPA Project Officer (see below). The complete report, entitled "Chlorine Dioxide for Wastewater Disinfection: A Feasibility Evaluation," fOrder No. PB 81-213 357; Cost. $14.00, subject to change) will be available only from: National Technical Information Service 5285 Port Royal Road Springfield, VA22161 Telephone: 703-487-4650 The EPA Project Officer can be contacted at. Municipal Environmental Research Laboratory U S. Environmental Protection Agency Cincinnati, OH 45268 United States Environmental Protection Agency Center for Environmental Research Information Cincinnati OH 45268 Postage and Fees Paid Environmental Protection Agency EPA 335 Official Business Penalty for Private Use $300 RETURN POSTAGE GUARANTEED f.i-\i I C i I J-« V 2 3 (> S L-- P a k},,' i ,V'. " c , .,., ,-^ , CillC/' iu It, r,S,b^1 " ------- V-/EPA United States Environmental Protection Agency Municipal Environmental Research Laboratory •* Cincinnati OH 45268 Research and Development EPA-600/S2-81-091 July 1981 Project Summary Wastewater Treatment by Rooted Aquatic Plants in Sand and Gravel Trenches Pamela R. Pope A patented* process developed by the Max Planck Institute (MPI) of West Germany to treat industrial wastes was evaluated as an energy-efficient method to treat municipal waste- water. The major goal was to achieve effluents meeting the U.S. Federal Effluent Standards using this novel biological treatment process that re- quires a minimal amount of mechanical equipment and manpower for normal operation. The Moulton Niguel Water District (MNWD) of Laguna, California, con- structed and operated an earthen trench system using rooted aquatic plants for the treatment of waste- water. Two trenches in series were planted with the reed Phragmites and the bulrush Scirpus, respectively. A 2-month study using convention- al secondary effluent as the trench influent showed the system was not effective for removing nitrogen and phosphorus components. An 11 -month study demonstrated that raw screened wastewater applied to the trench system at a rate not exceeding 95 mVd (25,000 gpd) could be treated to secondary effluent quality. Spatial requirements were about the same as for a septic tank system. This Project Summary was develop- ed by EPA's Municipal Environmental Research Laboratory, Cincinnati, OH, to announce key findings of the research project which is fully docu- *U S Patent 3,770,623, November 6, 1973 mented in a separate report of the same title (see Project Report ordering information at back). Introduction The MPI process utilizes higher aquatic plants, such as reeds and bul- rushes, for the treatment of waste- water The system consists of two earthen trenches, lined with impervious membranes, operated in series. The first, designated as the filter trench, removes coarse suspended solids from the wastewater. The second, desig- nated as the elimination trench, removes dissolved materials from the effluent of the first trench. The MNWD services a residential area, and the wastewater is domestic in nature. The MPI system, as it was installed at the MNWD 3A facility, con- sists of two filter trenches and two elimination trenches. Two species of plants were used—a reed Phragmites communis in the filter trench and a bulrush Scirpus lacustris in the elimina- tion trench. A view of the elimination trench system during construction is shown in Figure 1 Filter Trenches The two filter trenches are each 25 m (75 ft) long, 4 m (12 ft) wide, and 1.3 m (4 ft) deep. They are filled with three layers of gravel—150 mm (6 in.) of 50-mm (2- in.) gravel on the bottom; 225 mm (9 in.) of 19-mm (34-in.) gravel in the middle, ------- Figure 1. Construction of elimination trench. and 75 mm (3 in.) of pea gravel on top. A 75-mm (3-in.) layer of silica sand covers the top. The raw wastewater enters the MNWD 3A facility at the north side of the plant and is passed through a roto- strainer to remove large particles. The screened influent flows down an influent channel and is pumped to the MPI system at a rate of approximately 8.8 to 9.5 X 10~4m3/s(14-15gpm). The influent then flows south through a control valve into the east end of the filter trenches. Every 24 hr the flow is alternated between the two trenches. Each filter trench contains a central 150-mm (6-in.) plastic pipe with an open slit running its entire length; alternating long and short 100-mm (4- in.) plastic pipes extend from it for even dispersion of the influent. The waste- water flows down the central pipe through the extending pipes and onto cement splash pads located directly below. The wastewater percolates through the trench in a vertical filtering action leaving a sludge layer on top. The sand filters out tne suspended solids while the plant system draws moisture and nutrients. Slow drying of the deposited solids occurs, and extensive growth of the plant rootlets and runners aid in degrading the sludge layer on top of the sand. Each trench has a perfor- ated 100-mm (4-in.) plastic pipe extend- ing the entire length of the trench from the surface to the bottom in a "U"- shaped configuration. Flow from the underdrain goes into this pipe and through pipe extensions and a butterfly valve into a sump. This pipe not only transports the flow but allows aeration to the bottom since it has openings to the surface. The sump is a 1.3-m (4-ft) concrete pipe 3.3 m(10ft) in height and is buried 2.6 m (8 ft). A small 0.25-kW (0.33-hp) pump, activated by a float, periodically pumps the flow to the elimination trenches. Elimination Trenches ^ Normally, this process would be « total gravity flow system, with the elimi nation trenches so placed as to facilitate this, but because of site conditions a this location, the elimination trenches had to be constructed 90 m (100 yd north of the filter trenches. The twc elimination trenches are 50 m (150ft long, 4 m (12 ft) wide, and 0.75 m (2.5ft deep. They are divided in the center by e weir designed to allow composite samp- ling in this area and to aid in aeration The filter trench effluent enters twc 150-mm (6-in.) plastic pipes 4 m (12 ft; long set perpendicular to the trenches at the south side. The side facing the trenches is open, and the liquid is allowed to flow out into an area 1.3 m (4 ft) by 4.0 m (12 ft) in a waterfall-like action. This area is filled with 15 mm (5/s in.) gravel held in place by 50- X 100- mm (2- X 4-in.) wood baffles. A later observation (by BWP of New York Inc.) showed that eliminating the baffles reduced the operational problems. The liquid percolates down in a horizontal manner at a level approximately up to 50 mm (2 in.) below the surface of the trenches. The trenches are filled with 15-mm (5/a-in.) gravel with 75 mm (3 in.) of pea gravel on top. The flow passes' through the weir and runs into two standpipes that lead into a sump. The level of the liquid flow is governed by raising or lowering the standpipes. A valve in the bottom of the weir allows periodic draining of the liquid in the lower portions of the trenches. The total retention times for the entire system are estimated to be 6 hr and 8.5 hr at flows of 133 mVd and 95 mVd, respectively. Test of MPI System as a Tertiary Treatment Process Secondary effluent from the MNWD extended aeration plant was introduced to the MPI system on July 1, 1978, at a loading rate of 56 mVd (15,000 gpd); the flow was increased to 95 mVd (25,000 gpd) in August. The analytical results for samples obtained during the time extended aeration effluent was applied to the system are shown in Table 1. Overall removal of BOD5, VSS, and TSS was about 50 percent each month. COD reduction was about 40 percent. Ammonium nitrogen removal of 67 per- cent during August was superior to the 40 percent removal in July. Considera- tion of the NH4-N, N03-N, and N02-N values between the 2 months indicates I ------- Table 1. Tertiary Treatment Results for MPI System, Average Values Item, mg/L MNWD Secondary Filter Trench Effluent Effluent Elimination Overall Trench Effluent Removal, % Flow of 25,000 gpd (95 mVd) BODS TSS VSS COD NHt-N A/02-/V NOz-N TP 15 15 10 58 12 0.8 2.1 11.5 9 8 6 50 8 2 5.5 10 7 7 4 35 6 1.1 7.2 10 53 53 60 39 50 — — 13 nitrification and subsequent denitrifica- tion were more active in the system during the warmer month of August. TKN samples were not collected during this period. The MPI system operated as a tertiary process did not efficiently remove TP. The extended aeration efflu- ent applied to the system was of good quality. The filter trench achieved the greater part of the overall pollutant removals; the elimination trench showed only marginal incremental removal. Test of MPI System as a Secondary Treatment Process Screened raw wastewater was used as the influent tothe MPI system in mid- September at a rate of 56 mVd (15,000 gpd). The flow was increased to 95 mVd (25,000 gpd) in October and 133 mVd (35,000 gpd) in January, remaining at this rate through July. The growth of the bulrush Scirpus in the elimination trench is shown in Figure 2. A thin sludge layer built up and com- pletely covered the filter trenches by the end of October. At this time, the Phragmites had not spread throughout the trenches. Algae also started to grow on the sludge layer and may have con- tributed to later clogging problems. By mid-December, algae covered a large portion of the sludge layer, which was not drying or breaking up as the flow was directed into the alternate trench. The problem occurred equally in both filter trenches. Operation was sus- pended at this time to consider this problem and to harvest the Phragmites from the filter trenches. The Phragmites had turned brown because of unusually cold weather and had begun to lay over because of their mature height and weight. When the sludge layer was skimmed off a little at a time, about 25 mm (1 in.) of sludge was found deposi- ted on the filter media; this sludge layer was wet and becoming septic. Below this was a layer of compacted organic matter and fibers that were black in appearance and felt greasy; this inter- mingled with the sand, formed an almost impermeable layer. If a hole was poked through this layer, the liquid held in the sludge layer immediately drained through the remaining sand. The only solution at this time was to allow the filter trenches to dry after the harvest- ing and then to rake out the semidry top sludge layer carefully. Figure 3 shows the plants after harvesting. Subsequent tests conducted in Long Island, New York, by BWP of New York, Inc., showed that using four parallel filter trenches to allow increased drying time and that draining the filter trenches three times a week minimized this sludge problem. The major objective of this project was to evaluate the MPI system as a low-cost wastewater treatment alterna- tive that would satisfy federal discharge requirements. These requirements are attained if final effluent BOD5 and SS concentrations do not exceed 30 mg/L for 30 days average values, or 85 per- cent overall removal, whichever is more stringent. The fate of nitrogen and phosphorus was also monitored. Table 2 summarizes all the data collected. The system was evaluated for sec- ondary treatment effectiveness for 11 months. For 5 of the months, the flow through the system was 95 m3/d (25,000 gpd) or less; for 6 months, 133 m3/d (35,000 gpd). Secondary treat- ment requirements for BODs and SS were achieved all 5 months at the lower flow SS residuals and percent removals met secondary requirements all 6 months at the higher flow rate; how- ever, the BOD5 requirement was not achieved for 5 of the 6 months. The effluent violated both the concentration and percent removal requirements three times (January, April, and July); the percent removal requirement only was violated twice (May and June). There was little difference in overall COD removal for the two application rates. The NH4-N and Org-N concentration values in the effluent during the periods of 95 mVd application were represen- tative of conventional secondary treat- ment residuals Variations in percent removals were because of fluctuations in influent concentrations. The overall removal of total nitrogen varied from 61 percent in September to 32 percent in March. During application of 133 mVd, the Org-N residuals were about twice the values of the lower flow rate results. During February, a negative removal of Org-N was noted. The overall removal of total nitrogen was much lower than during the 95 mVd application, 18 percent in January to 36 percent in June. Nitrite and nitrate nitrogen concen- trations for all the sample periods show that nitrification did not occur to any significant extent at either of the two flow rates. The MPI system during both the 95 mVd and the 133 m3/d application rates was not effective for total phosphorus removal. During the higher application rate, 2 months (January and June) showed negative removals. The major increment of BODg, SS, VSS, and COD removal occurs at the filter trench, and the elimination trench serves as a polishing process (Table 2). Both trenches in series are necessary for satisfactory treatment. The MPI system operated with raw screened wastewater at an application rate of 95 mVd did achieve secondary effluent quality. Using the trench meas- urements, the spatial requirements of ------- Figure 2. Aquatic plant growth in elimination trench. the MPI system equate to 0.02 mVrrvd (0.5 gpd/ft2). Assuming a per capita wastewater discharge of 378 L (100 gal), the area required is 2 m2/capita(21 ftVcapita). These two values are very similar to spatial requirements of a septic tank system located in a satisfac- tory percolating soil. Several operating problems, expected with new technology development, were experienced during this demonstration study. Many of the same operational problems were encount- ered at the Long Island, New York. Several operating problems, expected with new technology development, were experienced during this demon- stration study. Many of the same opera- tional problems were encountered at the Long Island, New York, installation. Remedial measures applied at Long Island included: 2. Recommend harvesting plants not more than once a year. Frequent harvesting of the plants used in the system promotes extra growth of the root systems and this con- tributes to clogging. 3. If plant growth becomes excessive during the year, individual plants are culled by pulling to thin the growth. This initial assessment of the effi- ciency and spatial considerationsforthe MPI system for secondary treatment indicates it is worthy of further develop- ment. The full report was submitted in ful- fillment of Grant No. R-805279 by the Moulton Niguel Water District under the sponsorship of the U.S. Environmental Protection Agency. 1. Provision for increased area for the filter trenches, thereby allow- ing longer idle times for drying. ------- NT ._, - -f - •% ^ Figure 3. Filter trench after harvest of plants. ------- Table 2. Secondary Treatment Results for MPI System, Average Values in mg/L Sample Location BODs TSS COD NHt-N Org-N NOZ-N N03-N TP Influent Wastewater Filter Trench Effluent Elimination Trench Effluent Overall Removal, Percent Flow of 25,000 gpd (95 mVd) 210 225 405 24 13 0.0 0.1 77 41 179 19 26 20 86 16 88 91 79 33 31 0.4 0.9 13 12 0.1 0.4 12 Flow of 35,000 gpd (133 mVd) Influent Wastewater Filter Trench Effluent Elimination Trench Effluent Overall Removal, Percent 171 68 35 80 181 48 19 89 405 157 93 77 25 21 19 24 17 13 11 35 0.0 0.3 13 0.6 1.2 13 0.3 0.6 13 0 Pamela R. Pope is with the Moulton Niguel Water District, Laguna Niguel. CA 92677. Ronald F. Lewis is the EPA Project Officer (see below). The complete report, entitled "Wastewater Treatment by Rooted Aquatic Plants in Sand and Gravel Trenches," (Order No. PB 81-213241; Cost: $6.50, subject to change) will be available only from: National Technical Information Service 5285 Port Royal Road Springfield, VA22161 Telephone: 703-487-4650 The EPA Project Officer can be contacted at: Municipal Environmental Research Laboratory U.S. Environmental Protection Agency Cincinnati, OH 45268 <, US OOVERNMENTPRINTINGOFFICE IWt -757-012/7203 ------- f **,».,'« i ,4 ------- United States Environmental Protection Agency Center for Environmental Research Information Cincinnati OH 45268 Postage and Fees Paid Environmental Protection Agency EPA 335 Official Business Penalty for Private Use $300 RETURN POSTAGE GUARANTEED Third-Class Bulk Rate LOU V TTLLtr rtFGlUM V FPA ?3t) S OE CHICAGO II ST ------- |