ORANGE COUNTY SANITATION DISTRICT BIOSOLIDS MASTER PLAN TECHNICAL MEMORANDUM 1: OCSD SOLIDS FACILITIES SUMMARY AND DESIGN BASIS

Transcription

1 ORANGE COUNTY SANITATION DISTRICT BIOSOLIDS MASTER PLAN TECHNICAL MEMORANDUM : OCSD SOLIDS FACILITIES SUMMARY AND DESIGN BASIS OCSD PROJECT NO. PS5 0 Black & Veatch Holding Company 205. All rights reserved. Orange County Sanitation District 9 MAY 207 In association with

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3 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Table of Contents Acronym and Abbreviations List... iv.0 Introduction.... Overview....2 References Background and Information Resources Overview Major Planning Documents Planning Studies OCSD Plant Nos. and 2 Solids Processing Overview Overview Review of Existing Facilities at Plant No Review of Existing Facilities at Plant No Current and Future Solids Loadings Mass Balance Model/White Paper Overview Evaluation of Mass Balance Model/White Paper Recommended Loadings for Integration of Loadings in the BMP See Enclosed Flash Drive for Appendices Appendix A TM Figures... A Appendix B OCSD Solids Loading Projections, White Paper... B Appendix C Task.2 White Paper Review Meeting Minutes... C Appendix D QC Review Affidavits... D Select Published Appendices Appendix A TM Figures... A Appendix B OCSD Solids Loading Projections, White Paper... B Final May 9, 207 ii Biosolids Master Plan

4 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis LIST OF TABLES Table. Summary Of Biosolids Master Plan... Table 2. OCSD Completed Solids Handling Facility Related Study Projects Table 3. Summary of Existing Solids Processing and Handling Facilities at Plant No Table 3 2. Primary/Secondary Sludge Blending and Thickening Design Parameters Table 3 3. Digester Design Parameters Table 3 4. Sludge Dewatering Design Parameters Table 3 5. Dewatered Biosolids Cake Storage Silos and Truck Load out Equipment Table 3 6. Plant No. Digester Gas Utilization Equipment... 3 Table 3 7. Digester Gas Equipment Design Parameters... 3 Table 3 8. CenGen Design Capacity by System Table 3 9. Plant No. 2 Solids Handling and Gas Treatment Facilities Table 3 0. Secondary Sludge Thickening and Feed Table 3. Primary Sludge Blending and Anaerobic Digester Design Parameters Table 3 2. Plant No. 2 Digested Sludge Dewatering Equipment Design Parameters Table 3 3. Dewatered Biosolids Cake and Truck Loading Facilities Design Parameters Table 3 4. Plant No. 2 Digester Gas Utilization Equipment Table 3 5. Plant No. 2 Digester Gas Conveyance and Treatment Design Parameters Table 3 6. Pant No. 2 CenGen Design Parameters Table 4. White Paper Detailed Comments... 4 Table 4 2. Recommended Design Loadings for Solids Handling Facilities (Table 7, White Paper) LIST OF FIGURES Figure 3. OCSD s 205 Biosolids Management Summary (Source: 205 Biosolids Management Compliance Report) Figure 3 2. OCSD s Biosolids Production History from January 992 December 205 (Source: 205 Part 503) Figure 3 3. Current and Future Solids Routing for Plant No. (Source: Project SP 4) Figure 3 4. Plant No. Digester Age and Construction Figure 3 5. Plant No. 2 Solids Process Figure 3 6. Plant No. 2 Digester Age and Construction Final May 9, 207 iii Biosolids Master Plan

5 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Acronym and Abbreviations List The following acronyms and abbreviations are used in this document. % Percent AC Alternating current AS Activated sludge BC Brown and Caldwell B&V Black & Veatch Corporation BFPs Belt filter presses BMP Biosolids Master Plan BOD Biochemical oxygen demand BTU British thermal unit BTU/h British thermal unit per hour Cat Ox/SCR Catalytic oxidizer/ selective catalytic reduction CenGen Central Generation System CEQA California Environmental Quality Act CEPT Chemically enhanced primary treatment cf, cu. ft. Cubic feet cfm Cubic feet per minute CFR Code of Federal Regulations CIP Capital Improvement Program cy Cubic yards cy/hr, yd 3 /hr Cubic yards an hour DAF Dissolved air flotation DAFTs Dissolved air flotation thickeners DGCS Digester gas cleaning system DIP Ductile iron pipe District Orange County Sanitation District ea Each EPA Environmental Protection Agency F Degrees Fahrenheit FMP Facilities Master Plan ft Foot, feet gal Gallon gpcd Gallons per capita per day gpm Gallons per minute GWRS Groundwater Replenishment System hp Horsepower HVAC Heating, ventilation, and air conditioning kw Kilowatt kwh Kilowatt hours Final May 9, 207 iv Biosolids Master Plan

6 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis lb/hr Pounds per hour LRBMP Long Range Biosolids Management Plan max Maximum MG Million gallons MGD, mgd Million gallons per day min Minimum NBP National Biosolids Partnership OCSD Orange County Sanitation District PCH Pacific Coast Highway PF Peaking factor Plant No. OCSD Reclamation Plant No. Plant No. 2 OCSD Treatment Plant No. 2 ppd Pounds per day PS Primary sludge psig Pounds per square inch gauge PURPA Public Utility Regulatory Policies Act QA/QC Quality Assurance/ Quality Control SALS Steve Anderson Lift Station SCAQMD South Coast Air Quality Management District scf Standard cubic feet scfm Standard cubic feet per minute SP 4 Gas Facilities Study for Plant Nos. and 2 TF Trickling filter TFSC Trickling filter/solids contact TM Technical memorandum TMs Technical memoranda TPODS Treatment Plant Operational Data Summary TS Total solids TSS Total suspended solids TWAS Thickened waste activated sludge US EPA United States Environmental Protection Agency VSr Volatile solids reduction WAS Waste activated sludge White Paper OCSD Solids Loadings Projection White Paper WS Waste sludge WSS Waste secondary sludge Final May 9, 207 v Biosolids Master Plan

7 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis.0 Introduction. OVERVIEW One of the key goals of the Orange County Sanitation District (OCSD) 203 Five Year Strategic Plan is to recommend future biosolids management options and capital improvements for a 20 year planning period. To meet this goal, OCSD is implementing Project No. PS5 0, Biosolids Master Plan (BMP), to provide a roadmap and framework for sustainable and cost effective biosolids management options. The last biosolids master plan (2003 Long Range Biosolids Management Plan LRBMP) is thirteen years old and requires updating to reflect recently installed facilities and current trends in biosolids management. The BMP is comprised of nine Technical Memoranda (TMs) as shown in Table. This Technical Memorandum No. (TM ) provides a Solids Facilities Summary and Design Basis for Project PS5 0. The purpose of TM is to provide a brief description of the solids handling and gas treatment facilities at OSCD s Reclamation Plant No. (Plant No. ) and Treatment Plant No.2 (Plant No. 2), which will be used as a design basis for other TM s in the BMP. TM is organized in the following manner: Section.0 Introduction: Provides a brief summary of purpose and organization of TM. Section 2.0 Background and Information Resources: Provides a summary of the background information used to develop TM. Table. Summary of Biosolids Master Plan SUMMARY OF BIOSOLIDS MASTER PLAN TM OCSD Solids Facilities and Design Basis TM 2 Review of OCSD s Biosolids Program and Summarize the Current State, Trends, and Outlook for Biosolids Management TM 3 Offsite Biosolids Management Alternatives Evaluation TM 4 Sludge Digestion and Post Dewatering Technologies Evaluation TM 5 High Strength and Organic Waste Co digestion Evaluation TM 6 Capital Improvement Program (CIP) Project Development for Plant No. 2 Solids Handling Facilities TM 7 CIP Project Development for Plant No. Solids Handling Facilities TM 8 Biosolids Management Plan TM 9 AquaCritox Report Review Section 3.0 Plant Nos. and 2 Solids Processing Overview: Provides a description, design parameters, and current operation for each of the major solids handling and gas treatment facilities at Plant Nos. and 2. Process flow diagrams for each major process are provided in Appendix A. Section 4.0 Current and Future Solids Loadings: OCSD prepared a Future Solids Loading White Paper in 206 to project solids loading from the raw sewage influent to OCSD Plants, establish methods to project the solids loadings to the major treatment processes, and set the loading criteria for future solids handling facilities that will be recommended by the BMP. The Future Solids Loading White Paper and solids mass balance diagrams are provided in Appendix B (enclosed Flash Drive) and published as a hard copy at the end of TM. Final May 9, 207 Biosolids Master Plan

8 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District.2 REFERENCES The following background documents are referenced in this TM: Orange County Sanitation District, Facilities Master Plan, December 2009 CH2MHill, Long Range Biosolids Master Plan, Prepared for Orange County Sanitation District, December 2003 Orange County Sanitation District, Asset Management Plan Fiscal Years and 204 5, December 202 Orange County Sanitation District., 205 Treatment Plant Operational Data Summary (TPODS) Black & Veatch, J 02 Strategic Plan Update, Energy Master Plan, Prepared for Orange County Sanitation District, August 2007 Black & Veatch, SP 4 Gas Facilities Study for Plants and 2, Prepared for Orange County Sanitation District, February 205 Orange County Sanitation District, 205 Biosolids Management Compliance Report EPA 40 CFR Part 503, February 206 Final May 9, Biosolids Master Plan

9 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis 2.0 Background and Information Resources 2. OVERVIEW The purpose of this section is to briefly summarize the key references that may impact planning of future biosolids and gas treatment facilities in other BMP TMs. 2.2 MAJOR PLANNING DOCUMENTS OCSD develops planning level documents to evaluate the current state of their facilities and to determine future needs. The primary sources of planning documents for this TM included: the 2009 Facilities Master Plan (FMP), the 2003 Long Range Biosolids Master Plan (LRBMP), and the OCSD Solids Loading Projections White Paper (White Paper). A brief description of each document follows Facilities Master Plan The purpose of the FMP was to identify the capital improvement needs of OCSD through 2030 and to provide the information needed for planning and budgeting those improvements. The FMP implemented the Board approved Level of Service goals from the OCSD Strategic Plan. The Solids Treatment and Gas Handling chapter (Chapter 7.0 in the FMP) provides information on the following subjects that are pertinent to understanding the existing OCSD solids facilities: Descriptions of Plant Nos. and 2 solids treatment and gas handling facilities Operational philosophy for Plant Nos. and 2 solids treatment and gas handling facilities Current performance of facilities Design criteria for facilities Flow projections for facilities Issues and recommendations for facilities Planed upgrades for facilities Long Range Biosolids Management Plan The dynamic regulatory issues, land application ordinances and bans, and public perception challenges prompted the District to develop the LRBMP. The goal was to develop a sustainable, reliable, and economical program for long range biosolids management. The LRBMP included four major elements:. Identify long term potential Southern California Class A biosolids products and product markets. 2. Identify the onsite and offsite facility options for manufacturing marketable products while optimizing the use of the District s facilities necessary in treating wastewater. 3. Develop a flexible implementation plan for positioning the District to be able to participate in multiple markets. Final May 9, Biosolids Master Plan

10 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District 4. Continue to beneficially use biosolids and maintain conformance with the National Biosolids Partnership (NBP) Code of Good Practice. The LRBMP identified findings for the following: () sustainable biosolids product markets, (2) the steps necessary to produce those products, (3) an economic analysis of the product technologies, and (4) an assessment of implementation factors including public perception. It then provided recommendations and implementation guidance to achieve the four objectives identified. The most important message from the plan is to develop a diverse program that relies on multiple merchant facilities. OCSD has successfully implemented many of the recommendations of the 2003 LRBMP, with implementation of some of the recommendations still ongoing OCSD Solids Loading Projections, White Paper OCSD prepared a Solids Loading Projection White Paper in 206 to project solids loading from the raw sewage influent to OCSD Plants, establish methods to project the solids loadings to the major treatment processes, and set the loading criteria for future solids handling facilities that will be recommended by the BMP. The Solids Loading Projection White Paper and solids mass balance diagrams are provided in Appendix B. 2.3 PLANNING STUDIES OCSD s solids handling and gas treatment facilities at Plant Nos. and 2 are routinely upgraded through rehabilitation, repair, and replacement. A list of studies related to solids handling and gas treatment is provided in Table 2. These studies will be referenced when developing other TMs in the BMP related to facilities planning. Table 2. OCSD Completed Solids Handling Facility Related Study Projects PROJECT NO. SP 4 SP 86 PROJECT NAME PROJECT DESCRIPTION PROJECT STATUS Gas Facilities Study for Plant No. and Plant No. 2 Plant No. 2 Digesters and Tunnels Seismic Hazard Evaluation, Risk Analysis and Mitigation Study Conducted evaluation of the existing digester gas facilities and identified upgrading needs. Recommended to replace existing gas compressors and buildings, gas vents on digesters and low pressure gas holders, and gas flare systems. Performed seismic and structural evaluation of the Plant No. 2 digesters. Recommended to replace all digesters ultimately in phases. SP 73 Effluent Reuse Study Identify and evaluate the OCSD treatment plant and conveyance modifications needed to support the Groundwater Replenishment System (GWRS) Final Expansion. Source: PS5 0 Scope of Work, Table 2 Study completed. The design and construction project is scheduled for design in 206 as Project J 24 Gas Facilities Improvements for Plant No. and Plant No. 2. Completed. Completed. Final May 9, Biosolids Master Plan

11 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis 3.0 OCSD Plant Nos. and 2 Solids Processing Overview 3. OVERVIEW OCSD owns and operates Plant No. and Plant No. 2 to treat wastewater from their service area. Wastewater solids are separated from the liquid stream by various unit processes and are thickened prior to treatment. The sludge is then treated through an anaerobic digestion process to create a reuse product referred to as biosolids. Following digestion, the biosolids are dewatered and transported to offsite management sites. Similar solids processing operations are in place at both Plant Nos. and 2. Detailed process schematics are given in Appendix A (enclosed Flash Drive) and published as hard copies at the end of TM. The following provides a brief summary of the existing solids handling and processing. Chemically enhanced primary sludge (PS) is collected from primary sedimentation/clarifier basins and pumped to the digesters. Waste activated sludge (WAS) from the activated sludge (AS) secondary clarifiers is thickened in either dissolved air flotation thickeners (DAFTs) or thickening centrifuges at Plant No., and DAFTs only at Plant No. 2. Trickling filter sludge is conveyed to either the digesters or thickening centrifuges at Plant No.. Trickling filter/solids contact (TFSC) sludge is conveyed with WAS to the DAFTs for thickening at Plant No. 2. The thickened sludge at Plant Nos. and 2 is pumped to the digesters. Each plant digests combined chemically enhanced primary sludge and thickened WAS (TWAS) using mesophilic anaerobic digestion. The digesters at both plants meet United States Environmental Protection Agency (US EPA) requirements for Class B land application of biosolids, which include a minimum 5 day detention time, temperature of 95 0 Fahrenheit (F), and 38 percent volatile solids reduction (VSr). The current VSr at Plant Nos. and 2 is approximately 56 and 57 percent, respectively. From the holding tanks, the biosolids are pumped to dewatering centrifuges, currently under construction. Dewatered biosolids cake is transferred to storage silos using cake pumps at both plants. Dewatered biosolids cake is transferred from the storage silos and hoppers to trucks for offsite reuse/disposal. Composting 46% 24,800 dry meteric tons Landfill 6% 3,420 dry metric tons Land App. Class A/Class B Cake 46% 25,400 dry metric tons OCSD promotes approximately 93 percent beneficial reuse of all the biosolids produced in the treatment process. As shown on Figure 3, that goal was met in 205. Biosolids Figure 3. OCSD s 205 Biosolids Management Summary management options include (Source: 205 Biosolids Management Compliance Report) composting, land application, and landfilling as shown on Figure 3. Final May 9, Biosolids Master Plan

12 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Per OCSD s 205 Biosolids Management Compliance Report, the daily biosolids cake production in 205 was approximately 750 wet tons per day. Figure 3 2 (taken from TM 2) provides a summary of the historical biosolids production at both Plant No. and Plant No. 2. The average total solids (TS) percentages for each plant are listed in the figure. Additional details regarding OCSD s biosolids management are provided in TM 2 and TM 3. Digester gas is collected at each plant in a storage tank, compressed, and discharged into a highpressure gas line, which connects the two plants. The digester gas is used as fuel in the Central Generation System (CenGen) facilities at both plants and excess gas is flared. Neither plant currently has excess gas, so the flares are only used if the generators are out of service. The CenGen facilities produce electricity used in the two plants. Figure 3 2. OCSD s Biosolids Production History from January 992 December 205 (Source: 205 Part 503) 3.2 REVIEW OF EXISTING FACILITIES AT PLANT NO. Plant No. is located in the City of Fountain Valley, California at the corner of Ellis Avenue and Ward Street. A site plan showing locations of the solids processing facilities is provided on Figure in Appendix A. Plant No. receives wastewater flow primarily from the eastern and inland parts of the service area, which consist of residential, commercial, and industrial users. In 205, the average Plant No. influent flow rate was 03 mgd per the TPODS data. The processes at Plant No. include preliminary, chemically enhanced primary treatment (CEPT), and secondary treatment (activated sludge and trickling filters) as well as biosolids treatment and gas recovery. Flow data for Plant No. is provided in the Solids Loading Projection White Paper (see Appendix B). Final May 9, Biosolids Master Plan

13 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis A simplified schematic of the Plant No. solids processing system is provided on Figure 3 3. Centrifuges for thickening and dewatering shown on the figure are currently under construction and are scheduled for completion in 208. MWRP Solids Raw Influent Primary Solids Primary Clarifiers Primary Solids Diversion to Plant No. 2 Trickling Filter Secondary Clarifiers Thickening Centrifuges Activated Sludge Secondary Clarifiers WAS DAF Thickening Legend Existing Discontinued in Future Anaerobic Digestion Digested Sludge Holding Centrifuge Dewatering Cake Storage Truck Loading Figure 3 3. Current and Future Solids Routing for Plant No. (Source: Project SP 4) A summary of the major solids handling and gas treatment facilities at Plant No. is provided in Table 3. Table 3. Summary of Existing Solids Processing and Handling Facilities at Plant No. FACILITIES DAF Thickeners Thickening Centrifuges 3 Digesters and Holding Tanks Dewatering Centrifuges 3 Cake Storage Bins Digester Gas Storage and Compression CenGen Digester Gas Flares NUMBER OF UNITS 6 (to be discontinued) 0 digesters (Nos. 7, 8, 9, 0,, 2, 3, 4, 5 and 6) 2 holding tanks (Nos. 5 and 6) 4 cake storage silos low pressure gas holder 3 gas compressors 8 diameter high pressure gas line connecting Plant Nos. and 2 Three 2,500 kilowatt (kw) gas fueled, combustion engine generators 3 digester gas flares Final May 9, Biosolids Master Plan

14 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District 3.2. Primary/Secondary Sludge Blending and Thickening Plant No. utilizes primary clarifiers to thicken primary sludge via the chemically enhanced primary treatment (CEPT) process. WAS (includes all secondary sludge), sludge from the primary clarifiers, and scum from the secondary clarifiers is sent to the blending facility. Blended sludge is then fed through the thickening centrifuges, after which it is held in wetwells prior to being pumped to the digesters. Alternatively, WAS and secondary scum can still be sent to the DAFTs for thickening prior to digestion. Primary scum is sent directly to the digesters. A process flow schematic for the Plant No. primary/secondary sludge blending and thickening is provided on Figure 2 in Appendix A. Design Parameters A summary of the design parameters for the primary/secondary sludge blending and thickening equipment is provided in Table 3 2. Table 3 2. Primary/Secondary Sludge Blending and Thickening Design Parameters SYSTEM (S) WAS Pumps DESIGN PARAMETERS gallons per minute (gpm), 800 gpm, 400 gpm Primary Sludge Pumps Primary Scum Pumps Secondary Scum Pumps Sludge Blend Tanks Sludge Blend Tank Mixers Dissolved Air Flotation Thickeners System DAF Thickeners (DAFTs) Thickened WAS Pumps Thickening Centrifuge System Thickening Grinders Thickening Centrifuge Feed Pumps 200 gpm, 200 gpm 200 gpm 200 gpm 69,275 gallons (gal) 7.5 horsepower (hp) 00,245 gal 50 gpm 0 hp gpm Thickening Centrifuges 0,000 pounds per hour (lb/hr) ave. (6,000 lb/hr max);,300 gpm ave. (,600 gpm max) Thickened Sludge Wetwells Thickened Sludge Pumps Note: WAS = All secondary sludge gal 650 gpm Current Performance Refer to the White Paper in Appendix B for information on current performance of the DAFTs and expected performance of the thickening centrifuges Anaerobic Digesters There are ten digesters at Plant No.. The digesters utilize a single stage, mesophilic, anaerobic sludge digestion process. Digester Nos. 5 and 6 are currently used as holding tanks for digested Final May 9, Biosolids Master Plan

15 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis sludge prior to sludge dewatering as further described in Section A process flow schematic for the Plant No. digesters is provided on Figure 3 in Appendix A. A summary of the digester construction dates and materials is provided on Figure 3 4. A major rehabilitation of the digesters was completed this year (206) under project P 00. The project included replacement of aging sludge pumping, heating, and other structural, mechanical, electrical and control systems to improve reliability, increase existing treatment capacity, and restore lost volume. The project provided additional capacity to accommodate increased sludge production associated with the expanded secondary treatment (under project P 02). Even with the additional capacity, some primary sludge from Plant No. is currently sent to Plant No. 2 due to inadequate capacity. When the new centrifuge thickening facilities are complete, OCSD will discontinue diversion of primary sludge to Plant No. 2. Final May 9, Biosolids Master Plan

16 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District N Figure 3 4. Plant No. Digester Age and Construction Design Parameters A summary of the design parameters for the digesters and sludge conveyance equipment is provided in Table 3 3. Final May 9, Biosolids Master Plan

17 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Table 3 3. Digester Design Parameters SYSTEM Anaerobic Digesters DESIGN PARAMETERS Available Volume (Including Cone), Dimensions Digester Nos. 7 and 8 million gallons (MG), Diameter = 90, Side Water Height = 30 Digester Nos MG, Diameter = 0, Side Water Height = 30 Total Digester Volume Bottom Sludge Transfer Pumps Digested Sludge Mixing Pumps Heated Sludge Recirculation Pumps Heat Exchangers MG 230 gpm 4,000 gpm; 6,000 gpm 600 gpm British thermal unit (BTU) Current Performance All digesters operate with a sludge mixture that is predominantly primary sludge. The amount of each type of sludge in the mixture is provided in the White Paper mass balance flow sheets (Appendix B). The operating temperatures are maintained in the range of 98 F to 00 F. Refer to the White Paper in Appendix B for additional information on current performance of the digesters Digested Sludge Dewatering Sludge at Plant No. is dewatered using dewatering centrifuges (completion in 208). The dewatering centrifuges are fed digested sludge from two holding tanks (previously Digesters Nos. 5 and 6), which collect digested sludge from the other digesters. Cationic polymer is added to the sludge feed to flocculate solids and enhance dewatering. After dewatering, the sludge cake is pumped to the Cake Storage and Truck Load Out Facilities described in Section A process flow schematic of the Plant No. Digested Sludge Dewatering process is provided on Figure 4 in Appendix A. The new centrifuge facilities are considered existing for this TM. Design Parameters A summary of the Plant No. sludge dewatering equipment design parameters is provided in Table 3 4. Final May 9, Biosolids Master Plan

18 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Table 3 4. Sludge Dewatering Design Parameters SYSTEM DESIGN PARAMETERS Digested Sludge Holding Tanks MG, Diameter = 90, Side Water Height = 30 Digested Sludge Transfer Pumps 640 gpm Dewatering Grinders 0 hp Dewatering Centrifuge Feed Pumps gpm Dewatering Centrifuges 7,000 lb/hr ave. (0,000 lb/hr max);,000 gpm max Dewatered Cake Pumps 50 gpm Current Performance Refer to White paper in Appendix B for information on anticipated performance of the dewatering centrifuges Dewatered Biosolids Cake Storage Silos and Truck Load Out Dewatered biosolids cake is transported from the Thickening and Dewatering Facility to the Solids Storage Facility using dewatered cake pumps. The Solids Storage Facility houses four Cake Storage Silos and one Truck Loading Hopper. The dewatered cake pumps transfer the dewatered biosolids cake to any one of the solids storage silos or directly to the truck loading hopper. Cake from each silo is conveyed through a dedicated pipe to the truck loading hopper via sliding frames and cake silo transfer pumps, which are below each storage silo. A process flow schematic of the Plant No. Dewatered Biosolids Cake Storage Silos and Truck Load Out facilities is provided on Figure 5 in Appendix A. Major Equipment Size and Capacity Table 3 5 provides major equipment size and capacity information for the Dewatered Biosolids Cake Storage Silos and Truck Load Out facilities. Table 3 5. Dewatered Biosolids Cake Storage Silos and Truck Load out Equipment SYSTEM Cake Silo Transfer Pumps Cake Storage Silos Cake Silos Discharger Truck Loading Hopper DESIGN PARAMETERS 50 gpm 4 2,00 cubic feet (cf) (05 28 percent solids) 50 cf (00 28 percent solids) Current Performance Current performance information on the Dewatered Biosolids Cake Storage Silos and Truck Load Out facilities is provided in the White Paper in Appendix B Digester Gas Conveyance and Treatment Digester gas produced in the digesters is compressed, treated, dried, and used as fuel in enginegenerators in the CenGen facilities to produce electric power at both plants. A digester gas transmission line between Plant Nos. and 2 is used to transfer compressed high pressure digester Final May 9, Biosolids Master Plan

19 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis gas between plants. The digester gas at Plant No. is supplemented with natural gas to maximize the output of the engine generators. A steam boiler, fueled with digester gas, is used to meet the plant s heating requirements if the heat recovered from the engine generators is not sufficient. Plant No. digester gas utilization equipment and the capacities of the various units are listed in Table 3 6. Table 3 6. Plant No. Digester Gas Utilization Equipment DIGESTER GAS UTILIZATION EQUIPMENT Engine Generators Number of Units 3 Capacity, each, kw 2,500 Digester Gas Flow Rate, each, cubic feet per minute (cfm) Steam Boiler 60 pounds per square inch gauge (psig) Number of Units Digester Gas Flow Rate, cfm 85 Source: OCSD Data provided to B&V during Project SP 4 All digester gas produced is compressed using two stage reciprocating compressors. The gas is dried by running chilled water from the adsorption chillers through a digester gas to chilled water heat exchanger. Waste gas flares located on the high pressure side of the digester gas system are used to flare digester gas if there is a surplus of gas or issues with downstream equipment. Typically, all digester gas is utilized in the engines or the boiler, and very little is flared. A low pressure gas holder is located on the suction side of the gas compressors. The gas holder provides a storage buffer for the low pressure digester gas system. A process flow schematic of the Digester Gas Conveyance and Treatment equipment is provided on Figure 6 in Appendix A. Under Project SP 4, review of existing digester gas equipment and pipe sizes at both plants resulted in the recommendation to replace the existing gas compressors and building, gas vents on the digesters and low pressure gas holders, and the gas flare systems (to include ability to connect low and high pressure sides of system). This work will be designed and constructed under Project J 24, Digester Gas Facilities Rehabilitation. Design Parameters Digester gas equipment design parameters are provided in Table 3 7. Table 3 7. Digester Gas Equipment Design Parameters SYSTEM Digester Gas Compressors Interplant Gas Line Waste Gas Flares Low Pressure Gas Holder Chilled Water Heat Exchanger Digester Gas Cleaning System Vessels Steam Boiler DESIGN PARAMETERS standard cubic feet per minute (scfm) 8 ductile iron pipe (DIP) ,000 standard cubic feet 6,00 scfm (wet) 360 cf, activated carbon, 2, million British thermal units per hour (BTUh) Final May 9, Biosolids Master Plan

20 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Current Performance The digester gas equipment treats approximately.9 million cf per day of gas Central Power Generation OCSD s CenGen system at Plant No. consists of a dedicated power building that houses three 2,500 kw gas fueled engine generators. The engines are 2 cylinder, four stroke, turbo charged, intercooled Cooper Bessemer model LSVB 2 SGC reciprocating units, which drive Ideal Electric brand electrical generators at 2,470 Volts alternating current (AC). The engine generators were recently retrofitted under Project J to comply with South Coast Air Quality Management District (SCAQMD) Rule 0.2. Emission reduction technology, including a catalytic oxidizer/selective catalytic reduction (Cat Ox/SCR) system post combustion were added along with an emissions control system to each individual engine generator. In addition, a digester gas cleaning system (DGCS) using carbon adsorption was installed upstream of the engines. The CenGen facility at Plant No. operates primarily on digester gas and has a connection to utilize natural gas for power generation. With two generators running, CenGen is able to meet over 60 percent of Plant No. s electrical needs. The system also provides process heat, steam, and chilled water. Heat is recovered off each of the engine generators. Jacket water heat from the engines is transferred to the heat reservoir through heat exchangers. Heat is recovered from the engine exhaust as steam by an exhaust gas heat exchanger. Steam from the engine exhaust heat exchangers and steam boilers provide heat through a steam to hot water converter to the heat reservoir loop. Heat is sent to the digesters for heating the digesters and for building heating. Surplus steam is sent to adsorption chillers, which creates chilled water for administrative building HVAC systems and for digester gas cooling for condensate removal. Waste heat exchangers remove any excess heat from the heat reservoir water using plant water. Auxiliary heat exchangers remove heat from the engine lube oil and after cooler systems. A process flow schematic of the Plant No. CenGen facilities and heat recovery systems is provided on Figure 7 in Appendix A. The CenGen facility at Plant No. is classified as a Small Power Production Facility, which is a qualifying facility under Public Utility Regulatory Policies Act (PURPA) regulations. To qualify for the Small Power Production Facility classification, the plant must utilize a renewable fuel, such as digester gas, for a minimum of 75 percent of the total energy input. Design Parameters Table 3 8 presents a summary of power generation equipment at Plant No., including standby power. Final May 9, Biosolids Master Plan

21 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Table 3 8. CenGen Design Capacity by System SYSTEM Generators Engines Exhaust Heat Recovery Units Jacket Water Heat Exchanger Waste Heat Exchanger Auxiliary Waste Heat Exchangers Waste Heat Exchangers Chilling Cooling Water Heat Exchangers Chillers Supplemental Heat Steam Convertor Deaerator DESIGN PARAMETERS 2,500 kw 2,47 hp 3,843 pounds per hour (lb/hr) steam production 755 gpm 600 gpm 295 gpm 380 gpm 850 gpm million 40 gpm Current Performance Plant No. generates approximately 3.56 million kilowatt hours (kwh) per month on average. 3.3 REVIEW OF EXISTING FACILITIES AT PLANT NO. 2 Plant No. 2 is located in the City of Huntington Beach, CA at the corner of Brookhurst St. and Pacific Coast Highway (PCH). Site plans of the raw sludge facilities and digested sludge facilities are provided on Figure 8 and Figure 9 in Appendix A, respectively. Plant No. 2 receives flow primarily from the western and coastal parts of the service area, which consist of residential, commercial, and industrial users. In 205, the average Plant No. 2 influent flow rate was 85 mgd. A portion of the flow normally tributary to Plant No. 2 can be diverted to Plant No. using the Steve Anderson Lift Station (SALS). Up to approximately 50 mgd can be diverted from the Bushard/Knott Trunkline to SALS for use at GWRS. The processes at Plant No. 2 include preliminary, CEPT, and secondary treatment (high purity oxygen waste activated sludge and trickling filters/ solids contact) as well as biosolids treatment and gas recovery. Flow information for Plant No. 2 is provided in the White Paper (Appendix B). A simplified schematic of the solids processing system is provided on Figure 3 5. Project P2 92 (Planned for completion in 209) will install centrifuges at Plant No. 2 for sludge dewatering due to anticipated increases in solids loading and will replace the dewatering BFPs with dewatering centrifuges, as shown on Figure 3 5. The new dewatering centrifuge facilities are considered existing for this TM. Final May 9, Biosolids Master Plan

22 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Primary Clarifiers A Side Sludge & Scum Primary Clarifiers B Side Sludge Blending Facility Primary Clarifiers C Side Trickling Filter Sec. Clarifiers Activated Sludge Sec. Clarifiers WAS Digesters TWAS DAFT Units Digested Sludge Holding Tanks Centrifuge Dewatering Dewatered Biosolids Cake Cake Storage and Truck Load Out Figure 3 5. Plant No. 2 Solids Process A summary of the major solids handling and gas treatment facilities at Plant No. 2 is provided in Table 3 9. Final May 9, Biosolids Master Plan

23 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Table 3 9. Plant No. 2 Solids Handling and Gas Treatment Facilities FACILITIES DAF Thickeners 4 Digesters and Holding Tanks Dewatering Centrifuges 5 NUMBER OF UNITS 5 digesters (C, D, E, F, G, H, L, M, N, O, P, Q, R, S, T) 2 digesters/holding tanks (I and J) holding tank (K) Cake Storage 2 cake storage bins (A and B) Digester Gas Storage and Compression Central Generation System (CenGen) Digester Gas Flares 3 low pressure gas holder 3 gas compressors 8 diameter high pressure gas line connecting Plant Nos. and 2 5 gas fuel generators steam turbine generator 3.3. Secondary Sludge Thickening and Feed WAS from the activated sludge secondary clarifiers and scum and waste sludge (WS) from the tricking filters and secondary clarifiers is sent to the DAFTs for thickening. See Figure 0 in Appendix A for the detailed process flow diagram. TWAS pumps convey TWAS from the DAFTs to the Digesters as shown on Figure in Appendix A. Design Parameters A summary of the design parameters for the secondary sludge thickening and feed equipment is provided in Table 3 0. Table 3 0. Secondary Sludge Thickening and Feed SYSTEM Activated Sludge System West Secondary Sludge Pump Station, WAS East Secondary Sludge Pump Station, WAS Trickling Filters and Solids Contact System Waste Secondary Sludge Pumps, WSS Scum Pumps Dissolved Air Flotation Thickener System DAFTs Thickened WAS Pumps DESIGN PARAMETERS gpm gpm 720 gpm 80 gpm 55 foot (ft) diameter 345 gpm Current Performance Refer to the White Paper in Appendix B for information on current performance of the DAFTs. Final May 9, Biosolids Master Plan

24 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Primary Sludge Blending and Anaerobic Digesters Plant No. 2 primary sludge is generated from the CEPT process in the primary clarifiers and blended in the Sludge Blending Facility, which was constructed by Project P2 9. This allows blended sludge from all active clarifiers to reach any digester as shown on Figure in Appendix A. Primary sludge is pumped from primary clarifiers to blending tanks, and from these tanks the sludge is pumped to the individual digesters. Digesters are divided into three groups (A, B, and C) with the sludge feed rotating to each of the digesters within the group based on flow to each digester. This approach has allowed even feeding of primary sludge to all digesters and has managed the headloss variations associated with primary sludge pumping. The Plant No. 2 digesters utilize a single stage mesophilic anaerobic sludge digestion process. Digesters I, J, and K are used as holding tanks for digested sludge prior to sludge dewatering. Under Project P2 89, holding tanks I and J were converted into working digesters, while still maintaining the ability to be used as holding tanks. Sludge digesters A and B are no longer in service and will be demolished under the P2 0 Project. All the digesters receive both blended primary sludge and TWAS via separate feed systems. Operating temperatures are maintained in the range of 98 0 F to 00 0 F. See Figures and 2 in Appendix A for detailed process schematics of the digester feed and digested sludge conveyance systems. A summary of the digester construction dates and materials is provided on Figure 3 6. Final May 9, Biosolids Master Plan

25 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis N Figure 3 6. Plant No. 2 Digester Age and Construction Final May 9, Biosolids Master Plan

26 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Project SP 86 analyzed the Plant No. 2 digesters for seismic hazards to determine what mitigation measures would be required. The results of the SP 86 study are as follows: The walls of Digesters P, Q, R, and S, all 05 foot diameter, have seismic deficiencies in bending. The bending deficiencies are due to inadequate vertical reinforcing from the footing to wall connection and continue approximately 2 feet up the wall. Digesters C through O show seismic deficiencies in hoop tension. The hoop tension deficiencies are localized in one particular area; approximately 5 feet below the top of the wall. The wall horizontal hoop reinforcing steel provided at this location is inadequate. Digesters C through M all show footing deficiencies in shear capacity. The thickness of the footing is not adequate to resist the design loading. Note that the shear capacity was calculated using the design concrete compressive strength and concrete typically gains strength with age. Therefore, Digesters I, J, K, L, and M, which have a D/C ration in shear of.08, may be adequate since the current concrete compressive strength may be higher than the original design strength. Further testing would need to be performed to verify this hypothesis. Design Parameters A summary of the primary sludge blending and anaerobic digesters design parameters is provided in Table 3. Table 3. Primary Sludge Blending and Anaerobic Digester Design Parameters SYSTEM Primary Clarifier System Primary Sludge Pumps Primary Scum Pumps Primary Sludge Blending System Primary Sludge Blending Tank (A & B) Sludge Blending Tank Mixing Pumps Anaerobic Digesters DESIGN PARAMETERS 200 gpm 200 gpm 3,370 cf 500 gpm Available Volume (Including Cone), Dimensions Digesters C, D, E, F, G, H.9 MG ea., Diameter = 80, Depth = 32 Digesters L, M, N, O, T.2 MG ea., Diameter = 80, Depth = 33 Digesters P, Q, R, S 2.2 MG ea., Diameter = 05, Depth = 30 Total Digester Volume Digester Feed Pumps Bottom Sludge Transfer Pumps Digested Sludge Mixing Pumps Heated Sludge Recirculation Pumps Heat Exchangers 2.67 MG 695 gpm 7 pumps 6,000 gpm 0,000 gpm 5 pumps 5 pumps Current Performance Refer to the White Paper in Appendix B for information on current performance of the digesters. Final May 9, Biosolids Master Plan

27 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Digested Sludge Dewatering At Plant No. 2, five dewatering centrifuges located in the Dewatering Building will provide dewatered sludge to the Solids Storage Facility. The dewatering centrifuges will be fed digested sludge from Holding Tanks I, J, and K. Mannich polymer solution will be added to the sludge feed to flocculate solids and enhance dewatering. Under normal loading conditions, two or three dewatering centrifuges will be in operation with the remainder as standby. After dewatering, the sludge cake will be transferred to storage bins prior to being loaded into trucks. See Figure 3 in Appendix A for a detailed process schematic of the digested sludge dewatering system. Design Parameters The design parameters for the Plant No. 2 digested sludge dewatering equipment are provided in Table 3 2. Table 3 2. Plant No. 2 Digested Sludge Dewatering Equipment Design Parameters SYSTEM DESIGN PARAMETERS Digested Sludge Holding Tanks (I, J, K).43 MG ea., Diameter = 80, Depth = 33 (I and J are convertible to digesters) Digested Sludge Booster Pump Digested Sludge Transfer Pumps Dewatering Grinders Dewatering Centrifuge Feed Pumps Dewatering Centrifuges Cake Transfer gpm gpm 800 gpm, 3 hp 45 gpm 4200 lb/hr; gpm (design) 5040 lb/hr; gpm (max) 8 gpm (min), 39 gpm (max) Anticipated Performance Refer to the White Paper in Appendix B for information on the anticipated performance of the dewatering centrifuges Dewatered Biosolids Cake Storage Silos and Truck Load Out Dewatered biosolids cake is conveyed from the Dewatering Building to the Solids Storage and Truck Loading Facility using cake transfer pumps. At the Solids Storage and Truck Loading Facility, the cake is discharged into Silos A and B. During truck load out, a sliding frame and a series of screw conveyors convey biosolids cake into the trucks. A process schematic of the Plant No. 2 dewatered biosolids cake storage silos and truck load out is provided on Figure 4 in Appendix A. Design Parameters Table 3 3 provides design parameters for the cake storage and loading facilities. Table 3 3. Dewatered Biosolids Cake and Truck Loading Facilities Design Parameters SYSTEM Biosolids Storage Silos (A & B) Truck Loading Screw Conveyor DESIGN CAPACITY 600 cubic yard (cy) 50 cy/hr (6 per silo) Final May 9, Biosolids Master Plan

28 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Current Performance Information on current performance of the solids storage and truck loading facilities is provided in the White Paper in Appendix B Digester Gas Conveyance and Treatment Digester gas produced in the digesters is compressed, dried, and used to fuel the engine generators to produce electric power. Steam boilers operate on either digester gas or natural gas to meet the plant heating needs when the heat recovered from the engine generators does not meet all the heating needs. Typically, natural gas is used in such cases to allow all digester gas to be used in the engine generators. Plant No. 2 digester gas utilization equipment and the capacities of the various units are listed in Table 3 4. Table 3 4. Plant No. 2 Digester Gas Utilization Equipment DIGESTER GAS UTILIZATION EQUIPMENT Engine Generators Number of Units 5 Capacity, each, kw 3,000 Digester Gas Fuel Consumption, each, cfm Steam Boilers 60 psig Number of Units 2 Digester Gas Fuel Rate, cfm (each) 30 All digester gas produced is compressed using two stage reciprocating compressors. Following the compressors moisture is removed from the gas by cooling the gas using chilled water from chillers and heat exchanger installed in the gas stream. Waste gas flares located on the high pressure side of the digester gas system are used to flare digester gas if there is a surplus of gas or issues with downstream equipment. Typically, all digester gas is utilized in the engines or boilers, and very little is flared. A low pressure gas holder is located on the suction side of the gas compressors. The gas holder provides a storage buffer for the low pressure digester gas system. A process flow schematic of the Digester Gas Conveyance and Treatment equipment is provided on Figure 5 in Appendix A. Under Project SP 4, review of existing digester gas equipment and pipe sizes at both plants resulted in the recommendation to replace existing gas compressors and building, gas vents on the digesters and low pressure gas holders, and the gas flare systems. This work will be designed and constructed under Project J 24, Digester Gas Facilities Rehabilitation. Design Parameters Digester gas conveyance and treatment design parameters for Plant No. 2 are listed in Table 3 5. Final May 9, Biosolids Master Plan

29 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Table 3 5. Plant No. 2 Digester Gas Conveyance and Treatment Design Parameters SYSTEM Low Pressure Gas Holder Interplant Gas Line Digester Gas Compressors Chilled Water Heat Exchanger Waste Gas Flares Steam Boilers Digester Gas Cleaning System Vessels DESIGN 25,000 cf 8 ductile iron pipe (DIP) cfm 3,000 cfm 720 cfm 8.6 million BTUh 3,200 scfm (activated carbon) Current Operation The digester gas equipment treats approximately 2.4 million cf per day of gas Central Power Generation The CenGen system at Plant No. 2 consists of a dedicated Power Building that houses five 3,000 kw gas fueled engine generators and a single,000 kw steam turbine generator. The engines are 6 cylinder, four stroke, turbo charged, intercooled Cooper Bessemer model LSVB 6 SGC reciprocating units, which drive Ideal Electric brand electrical generators at 2,470 Volts AC. The steam turbine, which is powered by thermal energy captured from the waste heat of the engine generator s exhaust, also generates at 2,470 Volts AC. The engine generators were recently retrofitted under Project J to comply with South Coast Air Quality Management District (SCAQMD) Rule 0.2. Emission reduction technology, including a catalytic oxidizer/selective catalytic reduction (Cat Ox/SCR) system post combustion were added along with an emissions control system to each individual engine generator. In addition, a digester gas cleaning system (DGCS) using carbon adsorption was installed upstream of the engines. Heat is recovered off each of the engine generators. Jacket water heat from the engines is transferred to the heat reservoir through heat exchangers. Heat is recovered from the engine exhaust as steam. A steam to hot water converter transfer the heat to the heat reservoir system as required to meet heating loads. Steam boilers operating on natural gas provide supplemental heat through a steam to hot water converter to the hot water reservoir. Waste heat exchangers remove any excess heat from the heat reservoir water using plant water. A process flow schematic of the Plant No. 2 CenGen facilities and heat recovery systems is provided on Figure 6 in Appendix A. As is also the case at Plant No., the CenGen system at Plant No. 2 is classified as a "Small Power Production Facility" under PURPA. Design Parameters Table 3 6 presents a summary of CenGen equipment design parameters at Plant No. 2. Final May 9, Biosolids Master Plan

30 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District Table 3 6. Pant No. 2 CenGen Design Parameters SYSTEM Generators (gas fueled) Engines Generators (steam turbine) Exhaust Heat Recovery Units DESIGN PARAMETERS 3,000 kw 4,66 kw 3,550 pounds per hour (lb/hr) steam production Jacket Water Heat Exchanger 575 gpm jacket water, 80 gpm heating water, 3.2 million BTUh Waste Heat Exchangers 450 gpm heating water, 285 gpm cooling water, 0.28 million BTUh Auxiliary Waste Heat Exchangers 280 gpm heating water, 325 gpm cooling water, 3.24 million BTUh Supplemental Heat Steam Convertor Deaerator Steam million 40 gpm 8,625 lb/hr steam production Current Operation Plant No. 2 generates approximately 4.22 million kwh per month on average. Final May 9, Biosolids Master Plan

31 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis 4.0 Current and Future Solids Loadings 4. MASS BALANCE MODEL/WHITE PAPER OVERVIEW OCSD prepared a Projected Solids Loadings White Paper in 206 to project solids loading from the raw sewage influent to Plant Nos. and 2, establish methods to project the solids loadings to the major treatment processes, and set the design criteria for future solids handling facilities that will be recommended by the BMP. A copy of the White Paper and solids mass balance diagrams are provided in Appendix B. 4.2 EVALUATION OF MASS BALANCE MODEL/WHITE PAPER The Mass Balance Model/White Paper provided by OCSD was reviewed by Black & Veatch. The following general comments were offered: The evaluation is thorough and easy to follow. The underlying assumptions are well documented. Assumptions, peaking factors, and other criteria were identified for further discussion at a meeting held on February 6, 206. During the meeting with OCSD on February 6, 206, Black & Veatch proposed discussion of the items listed in Table 4 to reach a consensus of the assumptions and projections listed in the White Paper. Table 4. White Paper Detailed Comments ITEM QUESTION/COMMENT RESOLUTION Influent per Capita Flow Sludge Yield Rates Peaking Factors (PF) Primary Clarifier Performance Centrifuge Dewatering Performance The White Paper uses 75 gallons per capita per day (gpcd) current, then reducing over the next 20 years to 60 gpcd. Based on discussions with OCSD, the 60 gpcd represents the low end unit value for aggressive water conservation based on other studies. Biosolids production and sludge yield will not be impacted by wastewater flows in the range of gpcd. Sludge yield rates appear to be reasonable compared with B&V s/brown and Caldwell s general experience. Both firms reviewed sludge yield values for previous projects at Plant and Plant 2 and they are compatible with the white paper values. Since the White Paper value are current and based on plant performance data there was consensus to use these rates. Biosolids production and sludge yield will not be impacted by wastewater flows in the range of gpcd. Peaking factors appear to be reasonable compared with the general experience of both B&V and brown and Caldwell. These peaking factors are also close to most of the recent project PFs for Plant and Plant 2. BOD and TSS removal rates in the White Paper were based on chemically enhanced primary treatment. Any change of condition in the future could reduce the removal rate. OCSD commented that CEPT will continue to be used and currently has no plans to modify it. The White Paper uses 28 percent cake solids for centrifuge dewatering for both plants. For evaluation of cake storage requirements and other onsite facilities downstream of the dewatering centrifuges, B&V s/brown and Caldwell recommended assuming 25 percent cake solids as a low end value. The evaluations performed for the BMP using 25 percent cake solids will take place outside of the White Paper evaluation. No changes to White Paper No changes to White Paper No changes to White Paper No changes to White Paper No changes to White Paper Final May 9, Biosolids Master Plan

32 TM : OCSD Solids Facilities Summary and Design Basis Orange County Sanitation District A copy of the minutes from the February 6 meeting is provided in Appendix C. Following the meeting, OCSD made final revisions to the White Paper and this document is provided in Appendix B. 4.3 RECOMMENDED LOADINGS FOR 2035 Table 7 from the White Paper provides the projected loadings for A copy of Table 7 is provided as Table 4 2 on the following page. 4.4 INTEGRATION OF LOADINGS IN THE BMP The projected loadings identified in this TM will provide the basis for evaluation and concept design development for sludge digestion and post dewatering technologies evaluated in TM 4. In addition, these loadings will be projected to estimate biosolids quantities and quality in evaluating offsite biosolids management alternative options and capacities. Finally, the process technologies and offsite biosolids management alternatives will be combined into a series of end to end alternatives and evaluated in TM 4 to develop recommendations to achieve a well coordinated management strategy and master plan. Final May 9, Biosolids Master Plan

33 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Table 4 2. Recommended Design Loadings for Solids Handling Facilities (Table 7, White Paper) PLANT P P2 RESIDUAL DESCRIPTION Primary Sludge Dry Solids (pounds per day [ppd]), and Concentration (% of solids) WAS Dry Solids (ppd), and Concentration (% of solids) Trickling Filter (TF) Sludge Dry Solids (ppd), and Concentration (% of solids) Total Sludge Dry Solids, ppd Primary Sludge Dry Solids (ppd), and Concentration (% of solids) WAS Dry Solids (ppd), and Concentration (% of solids) TF Sludge Dry Solids (ppd), and Concentration (% of solids) Total Sludge Dry Solids, ppd UNITS DESIGN LOADING CRITERIA FOR FUTURE FACILITIES DESIGN LOADING CRITERIA FOR ULTIMATE FACILITIES Annual Average 29,000 44,000 5 day Maximum 350, ,000 Maximum Day 466, ,000 Concentration 4.% 4.% Annual Average 02,000 72,000 5 day Maximum 23, ,000 Maximum Day 64, ,000 Concentration.0%.0% Annual Average 5,000 2,000 5 day Maximum 8,000 5,000 Maximum Day 24,000 20,000 Concentration 2.0% 2.0% Annual Average 408, ,000 5 day Maximum 49, ,000 Maximum Day 654,000,096,000 Annual Average 292, ,000 5 day Maximum 35, ,000 Maximum Day 468, ,000 Concentration 4.5% 4.5% Annual Average 69,000 70,000 5 day Maximum 83,000 84,000 Maximum Day,000 2,000 Concentration 0.32% 0.32% Annual Average 36,000 89,000 5 day Maximum 44,000 07,000 Maximum Day 58,000 43,000 Concentration 0.35% 0.35% Annual Average 397, ,000 5 day Maximum 478, ,000 Maximum Day 637,000,04,000 Note: Used Peaking Factor of.2 for 5 day Maximum, and.6 for Peak Day as recommended by previous studies. Final May 9, Biosolids Master Plan

34 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Appendix A TM Figures The following figures, which have been referenced in TM, are included in Appendix A. Figure = Plant No. Solids Handling Map (Source: OCSD) Figure 2 = Plant No. Primary/Secondary Sludge Blending and Thickening Figure 3 = Plant No. Anaerobic Digesters Figure 4 = Plant No. Digested Sludge Dewatering Figure 5 = Plant No. Dewatered Biosolids Cake Storage Silos and Truck Load Out Figure 6 = Plant No. Digester Gas Treatment and Conveyance Figure 7 = Plant No. CenGen and Heat Recovery Systems (Source: OCSD Planning) Figure 8 = Plant No. 2 Raw Sludge Map Figure 9 = Plant No. 2 Digested Sludge Map Figure 0 = Plant No. 2 Secondary Sludge Thickening and Feed Figure = Plant No. 2 Primary Sludge Blending and Anaerobic Digesters Feed Figure 2 = Plant No. 2 Digested Sludge Conveyance Figure 3 = Plant No. 2 Digested Sludge Dewatering Figure 4 = Plant No. 2 Biosolids Cake Storage and Truck Load Out Figure 5 = Plant No. 2 Digester Gas Treatment and Conveyance Figure 6 = Plant No. 2 CenGen and Heat Recovery Systems (Source: OCSD Planning) May 9, 207 A Biosolids Master Plan

35 SOLIDS HANDLING nel 4 Raw Sludge Piping Primary Scum (PSC) DIGESTED SLUDGE Tun RAW SLUDGE Secondary Scum (PSC) Sludge Diversion Line Trickling Filter Scum (TFSC) Primary Sludge (PS) DIGESTER MIXING PUMPS (4) Pump Room y rk wa BOTTOM SLUDGE Pa St re ed Tunnel 6 6" DS 6" DS 8" BS Digester 4 ne Tunnel 0 Tun n Tunnel 6 3 Tun n el 7 4" DS 8" BS Digester 7 SLUDGE FEED PUMPS l ne Tun 7 2 Digester 9 ne Tun CAKE LOADING PUMPS Feet FOR CLARITY NOT ALL EXISTING SLUDGE PIPING AND EQUIPMENT ARE SHOWN. SEE FACILITY ATLAS FOR MORE DETAIL PIPING ne 5 l Solids Storage Faclity Tun 0 Digested Sludge Sludge Cake GWRS Future Equalization Tanks Bottom Sludge Future Structure 2" SC 2" SC 5 l BELT FILTER PRESSES Structures Tunnel 6 Tunnel Surface Wasting Solids Structures (Digested Sludge) SLUDGE CAKE TRANSFER PUMPS Tunnel 7 Dewatering Building "M" Scum Solids Structures (Raw Sludge) SLUDGE FEED PUMPS 2" SC Tunnel 24 Thickened Waste Activated Sludge (TWAS) Structures 8" DS 8" BS 8" BS SLUDGE CAKE TRANSFER PUMPS 2" SC 4" DS 8" DS 8" BS Cake Transfer Station "C" Pump Room 8" BS 8" DS Waste Activated Sludge (WAS) 6" DS el 8" BS Tunnel 2 8" DS Pump Room Return Activated Sludge (RAS) Pumps Dewatering Building "C" Digester 5 Trickling Filter Sludge Digested Sludge to Dewatering 24" DS BELT FILTER PRESSES 8" DS DIGESTER MIXING PUMPS (2) 8" DS DSO BOOSTER PUMPS (3) 8" DS Pump Room Trickling Filter Scum (TFSC) Sludge Cake 8 DS Digester 0 8" DS Digester 8 Primary Scum Digested Sludge Tunnel 9 8" BS 2 Pumps Bottom Sludge (BS) 8" BS Digester 6 el Barscreens Digested Sludge Piping Tun n DIGESTER SLUDGE TRANSFER PUMPS (3) Digester 3 BOTTOM SLUDGE TRANSFER 4" DS Gas Compressor Building 4 l 8" DS DIGESTER MIXING PUMPS (8) HEATED SLUDGE RECIRCULATION PUMPS (4) 2" BS 8" BS ne Digester Tunnel 7 8" BS 2 el 8" BS Pump Room Tunnel 8 n Tun East Perimeter Road l7 BOTTOM SLUDGE TRANSFER PUMP (2) Grit ó Í Digester 5 TRANSFER d 30" DS 30" DS 8" DS Tun Thickened Waste Activated Sludge (TWAS) 8" DS 2" BS 8" BS Digester 2 Waste Activated Sludge (WAS) 8" DS 6" DS n Tu s ou Re n ma Hu Return Activated Sludge (RAS) Pro ces s La ne HEATED SLUDGE RECIRCULATION PUMPS (2) oa sr e c r Trickling Filter Sludge (TF) Digester 6 BOTTOM SLUDGE TRANSFER PUMP 8" BS Primary Sludge (PS) PS & PS2 8" BS 6" DS 0 Tun 25 ne 7 l OCWD Tunnels 50 Feet Figure - Plant No. Solids Handling Map (Source: OSCD)

36 PRIMARY SCUM PUMPS (7) PRIMARY SLUDGE PUMPS (4) PRIMARY SCUM PRIMARY SLUDGE PRIMARY SCUM/SLUDGE SLUDGE BLEND TANK NO. MIXER NO. THICKENING GRINDERS NO. THICKENING CENTRIFUGE FEED PUMPS NO. THICKENING CENTRIFUGES NO. THICKENED SLUDGE THICKENED SLUDGE WETWELLS NO. THICKENED SLUDGE PUMPS NOS. & 2 TO DIGESTERS (SEE FIGURE 3) TS TS2 THICKENED SLUDGE AS WAS PUMPS (0) WAS MIXER NO. 2 NO. 2 CROSS OVER PIPING NO. 2 NO. 2 NO. 2 NOS. 3 & 4 AS SCUM PUMPS (6) SCUM WAS (ALTER.) SLUDGE BLEND TANK NO. 2 NO. 3 NO. 3 NO. 3 THICKENED SLUDGE THICKENED SLUDGE NO. 3 NOS. 5 & 6 AS SURFACE WASTING PUMPS (6) TF SLUDGE/ SCUM PUMPS (5) SFW SECONDARY SCUM SLUDGE BLEND TANK NO. 3 SFW TO ONLY 3 DAFTS MIXER NO. 3 Figure 2 Plant No. Primary/Secondary Sludge Blending and Thickening DAFTS (6) THICKENING POLYMER FEED THICKENED WAS PUMPS (2) TWAS (ALTER.) THICKENED SLUDGE TO DIGESTERS (SEE FIGURE 3) EXISTING FUTURE AS = ACTIVATED SLUDGE WAS = WASTE ACTIVATED SLUDGE TF = TRICKLING FILTERS SFW = SURFACE TO WASTE DAFTS = DISOLVED AIR FLOATITION THICKENERS TWAS = THICKENED WAS TS = THICKENED SLUDGE

37 SEE FIGURE 2 PRIMARY SCUM/SLUDGE TS TS2 TWAS (ALTER.) TO REMAINING DIGESTERS DIGESTER MIXING AND HEATED SLUDGE RECIRCULATION LOOPS SIMILAR TO DIGESTERS 5 AND 6 DIGESTER MIXING AND HEATED SLUDGE RECIRCULATION LOOPS SIMILAR TO DIGESTERS 5 AND 6 DIGESTED SLUDGE MIXING PUMPS BOTTOM SLUDGE TRANSFER PUMP BOTTOM SLUDGE TRANSFER PUMP TO DIGESTED SLUDGE HOLDING TANKS (SEE FIGURE 4) HEATED SLUDGE RECIRCULATION PUMPS AND HEAT EXCHANGERS BOTTOM SLUDGE TRANSFER PUMPS (2) BOTTOM SLUDGE TRANSFER PUMPS (2) 6 DIGESTER MIXING AND HEATED SLUDGE RECIRCULATION LOOPS SIMILAR TO DIGESTERS 5 AND 6 DIGESTER MIXING AND HEATED SLUDGE RECIRCULATION LOOPS SIMILAR TO DIGESTERS 5 AND DIGESTED SLUDGE MIXING PUMPS Figure 3 Plant No. Anaerobic Digesters

38 DIGESTED SLUDGE HOLDING TANK NO. (DIGESTER 5) DIGESTED SLUDGE TRANSFER PUMPS NO. DEWATERING GRINDERS DEWATERING POLYMER FEED CENTRIFUGE FEED PUMPS DEWATERING CENTRIFUGES DEWATERED CAKE PUMPS NO. NO. DIGESTED SLUDGE NO. NO. DIGESTED SLUDGE FROM DIGESTERS (SEE FIGURE 3) NO. 2 NO. 2 CROSS OVER PIPING NO. 2 NO. 2 NO. 3 NO. 3 DIGESTED SLUDGE HOLDING TANK NO. 2 (DIGESTER 6) NO. 2 NO. 3 NO. 3 DIGESTED SLUDGE CAKE STORAGE AND TRUCK LOAD OUT (SEE FIGURE 5) EXISTING Figure 4 Plant No. Digested Sludge Dewatering FUTURE

39 CAKE STORAGE BYPASS DEWATERED CAKE CAKE STORAGE SILO NO. CAKE STORAGE SILO NO. 2 CAKE STORAGE BYPASS DEWATERED CAKE FROM DEWATERING CENTRIFUGES (SEE FIGURE 4) DEWATERED CAKE CAKE TRANSFER PUMP NO. CAKE TRANSFER PUMP NO. 2 CAKE STORAGE BYPASS CAKE STORAGE SILO NO. 3 CAKE STORAGE SILO NO. 4 CAKE STORAGE BYPASS HOPPER BYPASS TRUCK LOADING HOPPER CAKE TRANSFER PUMP NO. 3 CAKE TRANSFER PUMP NO. 4 TRUCK LOAD OUT Figure 5 Plant No. Dewatered Biosolids Cake Storage Silos and Truck Load Out

40 LDG LDG LOW PRESSURE GAS HOLDER GAS COMPRESSORS CHILLED WATER HEAT EXCHANGER DIGESTER GAS CLEANING SYSTEM VESSELS HDG HDG HDG HDG DIGESTERS, 2, 4, 5, 6 LDG NO. HDG NO. NO. 2 HDG LDG NO. 2 HDG BYPASS TO POLISHING VESSEL DIGESTERS 7, 8, 9, 0, 3 HDG TO ENGINE GENERATORS (SEE FIGURE 7) NO. 3 HDG BYPASS WASTE GAS FLARES LDG DIGESTED SLUDGE HOLDING TANKS (DIGESTERS 5 & 6) LDG BYPASS LDG (ALTER.) HDG STEAM BOILER NOS., 2, & 3 Figure 6 Plant No. Digester Gas Conveyance and Treatment HDG INTERPLANT GAS LINE TO/FROM PLANT NO. 2 LDG = LOW PRESSURE DIGESTER GAS HDG = HIGH PRESSURE DIGESTER GAS

41 JACKET WATER RECIRC. COMBUSTION AIR JACKET WATER RECIRC. ENGINE GENERATOR NO. EXHAUST GAS OCR NO. ELECTRICITY SCR NO. TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. FEED WATER STEAM DEAERATOR CHILLERS CONDENSATE RETURN CONDENSATE RETURN SUPPLEMENTAL HEAT STEAM CONVERTOR HWR HWS CHILLING COOLING WATER HE'S HWR JACKET WATER HEAT EXCHANGER (NOS., 2, & 3) HWR HWR TO DIGESTERS FROM DIGESTERS, BLDGS, ETC. WASTE HEAT EXCHANGERS HWR AUXILLIARY WASTE HEAT EXCHANGERS CLW NO. NG FROM SCG COMBUSTION AIR ENGINE GENERATOR NO. 2 EXHAUST GAS OCR NO. 2 ELECTRICITY SCR NO. 2 TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. 2 NO. CHILLER COOLING WATER STRAINER COOLING WATER (PW) NO. CLW HWR NO. HWR CLW CLW NO. 2 CLW TO/FROM COOL INTAKE AIR, LUBE OIL, ETC. HDG FROM DIGESTER GAS CLEANING SYSTEM (SEE FIGURE 6) NO. 2 NO. 2 NO. 2 HWR COMBUSTION AIR ENGINE GENERATOR NO. 3 EXHAUST GAS OCR NO. 3 ELECTRICITY SCR NO. 3 TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. 3 Figure 7 Plant No. CenGen and Heat Recovery Systems (Source: OCSD Planning) STEAM CWR CWS TO/FROM BUILDINGS AND GAS DRYING HEAT EXCHANGERS OCR = CATALYTIC OXIDIZER SCR = SELECTIVE CATALYTIC REDUCTION CWS = CHILLED WATER SUPPLY CWR = CHILLED WATER RETURN NO. 3 WASTE STREAM CLW = COOLING WATER HWS = HOT WATER SUPPLY HWR = HOT WATER RETURN NG = NATURAL GAS

42 8in TWAS 8in WAS ORANGE COUNTY SANITATION DISTRICT PLANT 2 SYSTEM MAP Solids Handling - DRAFT - RAW SLUDGE LINES Distribution Center J 4in S Trickling Filter Clarifier B Trickling Filter Clarifier A Trickling Filter Clarifier C 6in S RSS Pump Station A 36in Return Secondary Sludge 36in Return Secondary Sludge Sludge Reaeration Solids Contact Reactors RSS Pump Station C Trickling Filter Clarifier D Chemical Building Trickling Filter Clarifier F Trickling Filter Clarifier E RSS Pump Station B Peroxide Facility 3 Trickling Filter A Trickling Filter B Guard Shack Cart Building Operations/ Control Center Trunkline Odor Control (Biotowers -3) Construction Management Complex Future Trickling Filter D Trickling Filter Pump Station Trickling Filter C ± HAZ-MAT Storage Maintenance Building Peroxide Facility City Water Pump Station 2 KV Distribution D 8in PS Primary Clarifier N Primary Clarifier P 6in PS 6in PS in PS Pump Room Pump Room 4in S 6in S Primary Clarifier O Primary Clarifier Q North Scrubber Complex (H-I, M-T) PB D Diversion Structure Influent Metering Structure Primary Treatment Ferric Chloride Facility Grit Handling Building Bar Screen Facility " " " " " " Grit Basins and Primary Splitter Primary Influent Metering Structure Screenings Loading Building Screenings Washing Building Influent Pump Station and Discharge Channel Distribution Center H Central Power Generation Building Headworks Odor Control Facility (Scrubbers -8, Biotowers -3) 2 KV Distribution C Ocean Outfall Booster Pump Station (OOBS) Communications Building Radio Tower Warehouse Polymer Facility Digester S Pump Room Digester R Digester Q Pump Room Digester P D PB C Truck Loading DAFT Gallery & WSSPS Solids Storage Facility Digester L Digester O A Pump Room Digester M SBF Electrical Building Digester T Pump Room 6in PS Pump Ferric Chloride Room Gas Facility Pump Compressor Digester Room Building Digester Gas G (PENN) Storage Tank B DAFT A, B and C Gallery Primary Clarifier M Pump Room Primary Clarifier L Digester IJK Elect Bldg Digester J Digester K Sludge Blending Facility Digester N C Feet 8in PS 0in Waste Secondary Sludge 2in PS Dewatering Building Pump Room 8in PS 8in PS Digester I Digester E Pump Room 6in PS 6in PS Digester H 6in PS Biofilter B 2in WAS Primary Clarifier K Primary Clarifier I 4in PS PB B Boiler Building Digester D Pump Room Digester C Scum Facility Digester F West RAS PS 4in S 6in PS 6in PS Pump Room Polymer Facility 6in PS Pump Room 8in PS 6in PS Gas Flares 36in RAS Secondary Clarifiers A-L Primary Clarifier J Primary Clarifier H Primary Clarifier E Pump Room Primary Clarifier D Primary Clarifier F 0in WAS 22in RAS South Scrubber Complex (U-X) Pump Room Aeration Basins A-H WSSPS-C PEPS Primary Clarifier G East RAS PS HW PB A PDF Building Primary PB A 2KV Plant Water Distribution Pump A Station 2 KV Distribution B HW PB B HW Standby Power Building Gas/Air Emergency Compressor Building Power Building 24in RAS 36in RAS 8in WAS 6in PS Primary Clarifiers A-C EPSA Pump Building EPSA Electrical Building Oxygen Facility 0in PS Stand-By Power Facility 6in PS Surge Tower Digester B Pump Room Digester A 6in PS 8in PS Bleach Station 2in PS Foster Booster Power Building Surge Tower 2 Sodium Bisulfite Facility Plant Water Booster Station (Auxiliary) Peroxide Facility 2 Legend " Barscreen Grit Pump Scum Pump Primary Sludge Pump Return Secondary Pump Return Activated Sludge Pump Waste Activated Sludge Pump Thickened Waste Activated Sludge Pump Waste Sludge Pump Sludge Pump Grit Scum Primary Sludge Return Activated Sludge Thickened Waste Activiated Sludge Waste Activated Sludge Return Secondary Sludge Waste Secondary Sludge Digested Sludge Digester Supernatant Sludge Cake Unknown/Other Sludge Piping ENG.p2structures ENG.p2tun Road edge Parking ENG.p2boundaries Disclaimer: Map prepared by Orange County Sanitation District. This map does not reflect the As-Is condition of the Plant. This map is intended for graphical representation only. No level of accuracy is claimed for the base mapping shown hereon and graphics should not be used to obtain coordinate values, bearings or distances. For an accurate representation of the plant facilities, please reference the appropriate Project drawings. Final Figure 8 - Plant No. 2 Raw Sludge Map Print Date: 0/7/205

43 6in SN ORANGE COUNTY SANITATION DISTRICT PLANT 2 SYSTEM MAP Solids Handling - DRAFT - DIGESTED SLUDGE LINES Distribution Center J Trickling Filter Clarifier B Trickling Filter Clarifier A Trickling Filter Clarifier C RSS Pump Station A Sludge Reaeration Solids Contact Reactors RSS Pump Station C Trickling Filter Clarifier D Chemical Building Trickling Filter Clarifier F Trickling Filter Clarifier E RSS Pump Station B Peroxide Facility 3 Trickling Filter A Trickling Filter B Guard Shack Cart Building Operations/ Control Center Trunkline Odor Control (Biotowers -3) Construction Management Complex Future Trickling Filter D Trickling Filter Pump Station Trickling Filter C ± HAZ-MAT Storage Maintenance Building Peroxide Facility City Water Pump Station 2 KV Distribution D 0in DS Primary Clarifier N Primary Clarifier P Pump Room Pump Room 0in DS Primary Clarifier O Primary Clarifier Q North Scrubber Complex (H-I, M-T) PB D Diversion Structure Influent Metering Structure Primary Treatment Ferric Chloride Facility Grit Handling Building 0in DS Bar Screen Facility " " " " " " Grit Basins and Primary Splitter Primary Influent Metering Structure Screenings Loading Building Screenings Washing Building Influent Pump Station and Discharge Channel Distribution Center H Central Power Generation Building Headworks Odor Control Facility (Scrubbers -8, Biotowers -3) 0in DS 2 KV Distribution C Ocean Outfall Booster Pump Station (OOBS) Communications Building Radio Tower Primary Clarifier M 8in DS Primary Clarifier K Pump Room Primary Clarifier J 0in DS 0in DS Peroxide Facility 2 Warehouse Polymer Facility Digester S Pump Room Digester R Digester Q Pump Room Digester P D PB C Truck Loading 4in SC DAFT Gallery & WSSPS Solids Storage Facility Digester L Digester M Digester O A 4in SC 8in DS Pump Room SBF Electrical Building Digester T Pump Room B Pump Room Primary Clarifier L 0in SC 6in DS 8in SN Digester IJK Elect Bldg Digester J Sludge Blending Facility Digester N Gas Pump Compressor Room Building (PENN) DAFT A, B and C Gallery -999in SC Digester K C Feet 8in DS 4in DS 8in SN Dewatering Building Pump Room 8in DS 0in SN 6in SN 8in DS 8in DS 8in DS Digester I Digester E Pump Room Digester H Digester Gas Storage Tank Primary Clarifier I PB B Boiler Building Digester D Pump Room Digester C Scum Facility Digester F Pump Ferric Chloride Room Facility Digester G Biofilter B 4in DS 6in SN 6in SN West RAS PS 6in SN Polymer Facility Pump Room Gas Flares Secondary Clarifiers A-L Primary Clarifier H Primary Clarifier E Pump Room Primary Clarifier D Primary Clarifier F 8in DS South Scrubber Complex (U-X) Pump Room Aeration Basins A-H WSSPS-C 8in DS PEPS Primary Clarifier G East RAS PS HW PB A PDF Building Primary PB A 2KV Plant Water Distribution Pump A Station 2 KV Distribution B HW PB B HW Standby Power Building Gas/Air Emergency Compressor Building Power Building Primary Clarifiers A-C EPSA Pump Building EPSA Electrical Building Oxygen Facility Stand-By Power Facility Surge Tower Digester B Pump Room Digester A 8in DS Bleach Station Foster Booster Power Building Surge Tower 2 Sodium Bisulfite Facility Plant Water Booster Station (Auxiliary) Legend " Barscreen Grit Pump Scum Pump Primary Sludge Pump Return Secondary Pump Return Activated Sludge Pump Waste Activated Sludge Pump Thickened Waste Activated Sludge Pump Waste Sludge Pump Sludge Pump Grit Scum Primary Sludge Return Activated Sludge Thickened Waste Activiated Sludge Waste Activated Sludge Return Secondary Sludge Waste Secondary Sludge Digested Sludge Digester Supernatant Sludge Cake Unknown/Other Sludge Piping ENG.p2structures ENG.p2tun Road edge Parking ENG.p2boundaries Disclaimer: Map prepared by Orange County Sanitation District. This map does not reflect the As-Is condition of the Plant. This map is intended for graphical representation only. No level of accuracy is claimed for the base mapping shown hereon and graphics should not be used to obtain coordinate values, bearings or distances. For an accurate representation of the plant facilities, please reference the appropriate Project drawings. Final Print Date: 0/7/205 Figure 9 - Plant No. 2 Digested Sludge Map

44 WAS/SCUM/WS TWAS DAFT C TWAS PUMP C2 TO DIGESTERS (SEE FIGURE ) WAS FROM AS SECONDARIES (4) WAS/SCUM/WS TWAS TWAS PUMP C DAFT B TWAS PUMP B2 SCUM FROM TF/SC (7) WAS/SCUM/WS TWAS TWAS PUMP B DAFT A TWAS PUMP A2 TWAS WS FROM TF/SC (3) WAS/SCUM/WS TWAS PUMP A DAFT D Figure 0 Plant No. 2 Secondary Sludge Thickening and Feed TWAS TWAS PUMP D2 TWAS PUMP D WAS = WASTE ACTIVATED SLUDGE TWAS = THICKENED WAS DAFT = DISSOLVED AIR FLOATING THICKENER AS = ACTIVATED SLUDGE TF = TRICKLING FILTERS SC = SECONDARY CLARIFIERS WS = WASTE SLUDGE

45 PRIMARY SLUDGE/SCUM PUMPS (2) SLUDGE BLEND TANK A MIXING PUMPS TWAS = THICKENED WASTE ACTIVATED SLUDGE PS = PRIMAY SLUDGE A A/B TWAS TWAS SLUDGE BLEND TANK B B TWAS TWAS TWAS TWAS DIGESTER FEED PUMPS DIGESTER F PS DIGESTER G DIGESTER N PS DIGESTER O PS DIGESTER T A2 PS PS A DIGESTER FEED SEGMENT A TWAS PS PS TWAS (SEE FIGURE 0) TWAS B2 PS TWAS DIGESTER P TWAS FUTURE TIE TO DIGESTER P DIGESTER Q TWAS FUTURE TIE TO DIGESTERS U & V DIGESTER R PS TWAS DIGESTER S PS B DIGESTER FEED SEGMENT B PS FUTURE TIE TO DIGESTER S PS TWAS TWAS TWAS TWAS FUTURE TIE TO DIGESTERS I & J TWAS C2 DIGESTER H PS PS DIGESTER E DIGESTER L PS DIGESTER M DIGESTER C DIGESTER D PS PS C DIGESTER FEED SEGMENT C PS PS FUTURE TIE TO DIGESTERS I & J Figure Plant No. 2 Primary Sludge Blending and Anaerobic Digesters' Feed

46 HEATED SLUDGE RECIRCULATION PUMPS AND HEAT EXCHANGERS (TYP) DIGESTED SLUDGE MIXING PUMPS (TYP) DIGESTER F DIGESTER G DIGESTER N DIGESTER O DIGESTER T DIGESTER P DIGESTER Q DIGESTER R DIGESTER S TO DIGESTED SLUDGE HOLDING TANKS (SEE FIGURE 3) DIGESTER H DIGESTER E DIGESTER L DIGESTER M DIGESTER C DIGESTER D Figure 2 Plant No. 2 Digested Sludge Conveyance

47 DIGESTED SLUDGE DIGESTED SLUDGE HOLDING TANK (DIGESTER I) DIGESTED SLUDGE DIGESTED SLUDGE BOOSTER PUMP DIGESTED SLUDGE TRANSFER PUMPS NO. DEWATERING GRINDERS CENTRIFUGE FEED PUMPS NO. NO. 2 DEWATERING CENTRIFUGES AND CAKE TRANSFER PUMPS NO. NO. NO. 2 CAKE STORAGE AND TRUCK LOAD OUT (SEE FIGURE 4) NO. 2 DIGESTED SLUDGE FROM DIGESTERS C H, L T (SEE FIGURE 2) DIGESTED SLUDGE HOLDING TANK (DIGESTER J) NO. 2 NO. NO. 2 NO. 3 NO. 3 NO. 3 DIGESTED SLUDGE NO. 4 NO. 3 NO. 4 NO. 4 NO. 3 NO. 5 DIGESTED SLUDGE HOLDING TANK (DIGESTER K) NO. 5 NO. 5 DEWATERING POLYMER FEED DIGESTED SLUDGE Figure 3 Plant No. 2 Digested Sludge Dewatering

48 FROM CAKE TRANSFER PUMPS (SEE FIGURE 3) (PUMP, 2, & 3) (PUMP 3, 4, & 5) BIOSOLIDS CAKE STORAGE SILO A BIOSOLIDS CAKE STORAGE SILO B TRUCK LOAD OUT TRUCK LOAD OUT Figure 4 Plant No. 2 Biosolids Cake Storage and Truck Load Out

49 LDG LOW PRESSURE GAS HOLDER LDG GAS COMPRESSORS DIGESTER GAS CLEANING SYSTEM VESSELS HDG HDG DIGESTERS L, M, J, K, I, D NO. LDG HDG REHEAT HEAT EXCHANGER CHILLED WATER NO. 3 NO. 2 NO. HDG LDG NO. 2 HDG CHILLED WATER HEAT EXCHANGER HDG HDG BYPASS TO POLISHING VESSEL DIGESTERS C, E, F, G, H, N HDG TO ENGINE GENERATORS (SEE FIGURE 6) NO. 3 HDG WASTE GAS FLARES LDG HDG NOS., 2, & 3 DIGESTERS O, P, Q, R, S, T STEAM BOILER STEAM BOILER NO. NO. 2 Figure 5 Plant No. 2 Digester Gas System HDG INTERPLANT GAS LINE TO/FROM PLANT NO. LDG = LOW PRESSURE DIGESTER GAS HDG = HIGH PRESSURE DIGESTER GAS

50 COMBUSTION AIR JACKET WATER RECIRC. JACKET WATER RECIRC. ENGINE GENERATOR NO. EXHAUST GAS OCR NO. ELECTRICITY SCR NO. TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. CONDENSATE RETURN HWR JACKET WATER HEAT EXCHANGER (NOS., 2, 3, 4, & 5) HWR NG FROM SCG HDG FROM DIGESTER GAS CLEANING SYSTEM (SEE FIGURE 5) COMBUSTION AIR ENGINE GENERATOR NO. 2 COMBUSTION AIR ENGINE GENERATOR NO. 3 COMBUSTION AIR ENGINE GENERATOR NO. 4 EXHAUST GAS EXHAUST GAS EXHAUST GAS OCR NO. 2 ELECTRICITY OCR NO. 3 ELECTRICITY OCR NO. 4 ELECTRICITY TO ATMOSPHERE SCR NO. 2 SCR NO. 3 SCR NO. 4 EXHAUST HEAT RECOVERY UNIT NO. 2 TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. 3 TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. 4 STEAM FEED WATER DEAERATOR CONDENSATE RETURN STEAM TURBINE & HEAT EXCHANGER SUPPLEMENTAL HEAT STEAM CONVERTOR COOLING WATER (PW OR GAP) CLW CLW HWS HWS HWR STEAM BOILER/ STEAM CONVERTER HWS HWR HWR WASTE HEAT EXCHANGERS HWR HWR NO. 2 HWS NO. HWR HWR HWR AUXILLIARY WASTE HEAT EXCHANGER (NOS., 2, 3, 4, & 5) CLW TO DIGESTERS FROM DIGESTERS CLW WASTE STREAM TO/FROM COOL ENGINE INTAKE AIR, LUBE OIL, ETC. COMBUSTION AIR ENGINE GENERATOR NO. 5 EXHAUST GAS OCR NO. 5 ELECTRICITY Figure 6 Plant No. 2 CenGen and Heat Recovery Systems SCR NO. 5 TO ATMOSPHERE EXHAUST HEAT RECOVERY UNIT NO. 5 STEAM CLW OCR = CATALYTIC OXIDIZER SCR = SELECTIVE CATALYTIC REDUCTION CWS = CHILLED WATER SUPPLY CWR = CHILLED WATER RETURN CLW = COOLING WATER HWS = HOT WATER SUPPLY HWR = HOT WATER RETURN NG = NATURAL GAS

51 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Appendix B OCSD Solids Loading Projections, White Paper The following is a copy of the Solids Loading Projections, White Paper prepared by OCSD. Projections and assumptions will be used in future TMs. May 9, 207 B Biosolids Master Plan

52 OCSD Solids Loading Projection White Paper Sharon Yin, OCSD Engineering Planning.0 Purpose and Objective The purpose of this White Paper is to project solids loading from the raw sewage influent to OCSD Plants, establish methods to project the solids loadings to the major treatment processes, and set the design criteria for future solids handling facilities that will be recommended by Project PS5-0, Biosolids Master Plan. The 2009 Facilities Master Plan identified the capital improvements needs for OCSD through 2030 and provided planning assumptions, including wastewater flow and loading projections, on which future demands are based. Since the 2009 Facilities Master Plan completed, there are some changed conditions as well as anticipated changes, including raw sewage influent flow decreasing due to water conservation, Irvine Ranch Water District (IRWD) will cease sending sludge flow to OCSD by the end of 207, flow diversion adjustment between Plant and Plant 2 to meet the Groundwater Replenish System (GWRS) Initial Expansion and the future operation changes to be determined by Planning Project SP-73 Effluent Reuse Study to meet the GWRS Final Expansion, and planned increasing Santa Ana Watershed Project Authority (SAWPA) flow. With the opportunity of the upcoming Biosolids Master Plan, which will layout the fate of OCSD s solids handling facilities and biosolids management plan for the next 20-year planning period, this White Paper will capture these changed conditions and anticipated changes, perform solids loading projections and establish a method to project loadings for later projects. 2.0 OCSD Influent Flows and Solids Projection 2. OCSD Influent Sources OCSD serves 2.6 million people in the central and north Orange County, California. The 25- member board of Directors is comprised of one representative from each of the 20 cites, 4 special districts and a representative from the County of Orange. The service area covers total 463 square miles, and is divided into sewer sheds flowing to OCSD s two treatment plants. (see Facilities Master Plan for maps). Through interagency agreements, OCSD receives influent from SAWPA, IRWD, and Urban Runoff within the service area. The influent changes from these agencies will impact the total flows and loadings. Thus the flows from these agencies will be evaluated. Through agreement with Orange County Water District (OCWD), OCSD provide treated secondary effluent to OCWD s GWRS and GAP facilities for reclamation. OCWD send back their microfiltration backwash flow to OCSD treatment process, and the RO reject to OCSD ocean outfall, and provide GAP water to OCSD as cooling and washing water for treatment processes. 2.. Historical Flow and Loadings From 2000 to 206, OCSD yearly average flow has reduced from 240 mgd to the 83 mgd range. Although population in OCSD s service area has been increasing, water conservation has reduced the wastewater generated. The monthly Water Conservation Reports published by P age

53 OCSD Solids Loading Projection White Paper California State Water Resources Control Board indicate the water usage per person has been decreasing. In the Orange County area, the water usage ranges from 40 to 00 gallons per day per person from different water suppliers. Most areas of Orange County use 70 to 80 gallons per day per person. The following chart shows the OCSD historical flow from year 2000 to 206. See Table for the summary of historical flow and loadings. Based on OCSD Source Control records, approximately 6 to 5 mgd are from permitted industrial, light industrial, and commercial facilities. The industrial and commercial flow percentages are relatively low, therefore loading from industrial/commercial will not be discussed separately in the later loading projections IRWD Flow Figure. OCSD Historical Flow In 985, OCSD and IRWD agreed to the formation of District 4, now called Revenue Area 4. IRWD owns and operates its own wastewater collection and treatment plant, Michaelson Water Reclamation Plant, (MWRP) within OCSD service area Revenue Area 4, (RA-4). The agreement allows IRWD to discharge part of their flows up to 5 mgd to OCSD, including their primary and secondary sludge. IRWD reports the estimated sludge flow to OCSD on a yearly basis. The sludge flow is estimated from a 2009 mass balance model created by Carollo. The majority of the IRWD raw sewage flow and sludge are diverted through Harvad Avenue Trunk Sewer (HATS) Diversion to OCSD s Main Street Pump Station and treated at OCSD Plant. Since 985, OCSD and IRWD formed various agreements for diverting additional flows between OCSD and IRWD for the newly development areas. The current flow contribution area agreements are summarized in Attachment OCSD/IRWD Flow Connection Schematic. See 2 P age

54 OCSD Solids Loading Projection White Paper Table 2 - IRWD Historical Flows and Loadings to OCSD. IRWD is currently constructing their new solids handling facility. Once on-line (scheduled for the end of 207), IRWD will stop sending sludge to OCSD. The raw sewage flow along with the IRWD sludge will decrease also because in part the raw sewage is to help scouring the sludge in the collection pipes. Post 207, the remaining flow from the RA-4 area will be mainly raw sewage flows from other IRWD service areas that do not go through HATS diversion. Currently those flows are approximately at 5 mgd. For the flow projection purpose, 5-0 mgd raw sewage flow from IRWD will be added to the future flow projection after 206. The IRWD raw sewage loading strength will be used for solids loadings. See Table 3 - IRWD Flows and Loadings Projection SAWPA Flow The SAWPA agency was developed to protect water quality within the Upper Santa Ana River Basin. To protect Orange County groundwater supplies, through agreement with OCSD, brine water (desalter concentrates) is removed from the Upper Santa Ana River Basin and discharge to OCSD facilities for treatment and disposal. SAWPA began to discharge wastewater to OCSD in 982. Currently, the SAWPA flows contains discharge brines from groundwater desalters and ion exchange plants, treated effluent from the Stringfellow Superfund Site Pretreatment Plant, and municipal wastewater from the member agencies of SAWPA including Inland Empire Utilities Agency, San Bernardino Valley Municipal Water District, Eastern Municipal Water District, and Western Municipal Water District. Per existing agreement between OCSD and SAWPA, SAWPA has purchased 8 million gallons of treatment capacity per day. The agreement allows SAWPA to discharge up to 30 mgd of flow into the Santa Ana River Interceptor (SARI) line. The SAWPA flows are conveyed to OCSD through the SARI line. The SARI Line is part of the OCSD collection system that extends over 90 miles into Riverside and San Bernardino Counties. In Riverside and San Bernardino Counties, the inland portion of SARI, also known as the Inland Empire Brine Line, is owned and operated by the SAWPA. The SARI line also conveys domestic flows from 250,000 residents within OCSD service area in Orange County. See Table 4 - SAWPA Historical Flows and Loadings and Table 5 - SAWPA Flows and Loadings Projection. The SARI flow is tributary to Plant. Currently, all of Plant secondary effluent is being reclaimed at the Groundwater Replenishment Systems (GWRS). Since SARI flow is not permitted to be reclaimed by the California Department of Health, all SARI flow is diverted to Plant 2 through the Interplant Interceptor Urban Runoff OCSD have been collecting and treating Urban Runoff from 9 diversion systems by local agencies within OCSD service areas. During the fiscal year of , the average daily flow was.8 million gallons per day. Under the current policy (Resolution No. 3-09) adopted in June 28, 203, the cities and agencies will be allowed to discharge up to a combined total 3 P age

55 OCSD Solids Loading Projection White Paper urban runoff flow of 0 mgd, without cost to permittees. Most of the urban runoff flows enter sewers line tributary to Plant 2. The historical urban runoff flow are summarized in attached Table 6 - OCSD Historical Urban Runoff Flow. Due to increasingly stricter receiving water quality standards, OCSD has received additional requests to accept urban runoff discharges. Currently the Peter Canyon and the Big Canyon Wash diversions are in planning stage, and under OCSD reviews. These two diversions are projected to add an additional 2 MGD flow to OCSD influent flow. For future projection, up to 0 mgd will be added to the 20-years flow projection. Solids loading contribution is negligible and will not be included in the solids projection OCWD and GWRS Through agreement with OCWD, OCSD provide treated secondary effluent to OCWD s GWRS and GAP facilities for reclamation. OCWD send back their microfiltration backwash flow to OCSD treatment process, and the RO reject to OCSD ocean outfall, and provide GAP water to OCSD as cooling and washing water for treatment processes. GWRS Phase started in operation in The Phase was to taking 00 mgd P secondary effluent to produce 70 mgd tertiary treated production water. OCWD just finished the GWRS initial expansion in 206. Currently approximately 30 mgd P secondary effluent is delivered to GWRS to produce 00 production water. OCWD is anticipating a Final Expansion of GWRS to be completed in The GWRS Final Expansion would require a total flow from OCSD of 70 mgd OCSD secondary effluent to GWRS in order to produce 30 MGD of potable reuse water. Including the GAP water need, total 75 mgd of OCSD secondary effluent will be needed. To support the GWRS Final Expansion, OCSD Planning study SP-73 Effluent Reuse Study evaluated treatment plant and conveyance modifications needed and made recommendations for projects. The goal of the modifications is to bring Plant 2 secondary effluent to GWRS to supplement to Plant secondary effluent. The major Plant 2 process improvements includes headworks improvements to separate the reclaimable flow and the non-reclaimable flows including SARI flow and recycle flows from both Plants, process modifications to use part of primary process and part of Plant 2 Pour Oxygen Activated Sludge (POAS) plant for nonreclaimable flow. Trickling Filter/Solids Contact (TF/SC) plant and rest of the POAS plant will be used for the reclaimable flow. OCWD will built secondary effluent flow equalization tanks and pump station to pump Plant 2 reclaimable secondary effluent to GRWS through an existing OCSD interplant line. Those improvement projects had been approved by both OCSD Board and OCWD Board and are moving forward for design and construction. The flows and solids loadings between OCSD and OCWD are built into the mass balance model presented later in this White Paper. 4 P age

56 OCSD Solids Loading Projection White Paper 2.2 Service Area Population Projection The population projection data are based on Orange County Projection by Center for Demographic Research (CDR). This includes the CDR annual reports data, 2004 CDR special study for OCSD during the 2009 Facilities Master Plan development, 200 CDR population adjustment based on US Census data during the Asset Management Plan development, the 206 CDR special study for the 207 Facilities Master Plan. Based on CDR s 205 Report, OCSD service area population is approximately 2.6 million people. Approximately 2.3 million people reside in areas directly tributary to OCSD Plant and Plant 2. The remaining 0.3 million reside within OCSD Service Area 4, the area of Irvine Ranch Water District (IRWD), that tributary to Michaelson Water Reclamation Plant (MWRP). Figure 2 OCSD Service Area Population Projection Population increased approximately ten percent in the OCSD service area between 2000 and 205, approximately five percent increase in the Plant and Plant 2 tributary areas, and sixty percent increase in MWRP service area. During the next 20 years between 205 and 2035, it is projected that the population directly contribute to Plant and Plant 2 will increase another seven percent, while MWRP service area population will increase twenty one percent, and the total OCSD service area population will increase eight percent. See attached Table 7 - OCSD Service Area Population Summary and Projection, and Table 8 - OCSD Service Area Population in 5yr Increment. 2.3 Flow and Solids Projection For solids loading projection purpose of this White Paper, the influent raw sewage flows were only projected at the annual average level. Peak flows of sludge were based on historical peaking factor at each Plant. 5 P age

57 OCSD Solids Loading Projection White Paper The flows, TSS and BOD loadings are projected by the Per Capita Loading method. Historical loadings per capita per day were calculated by dividing the total loadings by the population tributary to both plants. The loadings used for calculation excluded the loadings from OCSD service area such as SAWPA loading. IRWD loadings and populations are both subtracted from the total loading and population respectively. Future projected loadings are calculated by multiplying the loading per capita per day by the projected population for both plants, and then adding the external loadings including SAWPA and IRWD projected loadings. From 2000 to 206, the calculated influent flow per capita has been decreased from 05 gallons per capita per day (gpcd) to 74 gpcd. For future projection, 75 gpcd is assumed for upper bound annual average flow projection, and one percent decrease per year from 74 gpcd is assumed for lower bound annual average flow projection. Minimum 60 gpcd is assumed based on the sewage flows generated from the basic human daily activities. 0.2 lb per capita per day (ppcd) was used to calculate the future TSS loadings, and 0.9 ppcd was used for BOD loadings. Those are based on the maximum historical yearly average and matching the 2009 Facilities Master Plan assumptions. Total loadings to both plants are calculated without splitting the loading at this step based on the following reasons: () The flow diversion between the two plants make it difficult to estimate the loadings from tributary population to each plant; (2) There are no records for loadings from external sources to each plant. Loading splitting between the two plants will depend on OCSD s operation needs. This will affect the unit treatment capacity analysis. The loadings to each plant will be discussed in the Treatment Process Loading section below. Projected loadings are included in attached Tables 7 through Table Treatment Process Loadings Projection - Mass Balance Model It is critical to project the future loadings to the major liquid stream and solids handling unit treatment process. Unit process loading projection is critical for OCSD to assess the treatment process unit capacity deficiency, to recommend capital improvement projects and to establish design basis. OCSD developed a mass balance model for both plant to project loadings at the major unit processes. The major assumptions are summarized below:. The current treatment process performance parameters are calibrated based on 204 TPODS data. Using 204 data instead of 205 is because that flow diversion between Plant and Plant 2 changed over the year of 205 to accommodate the GWRS initial expansion flow need. 2. A model run results are attached to show the mass balance results of 204 loadings. Table 5 summarized the major assumptions used in the mass balance model and compared the model calculated results verses the plant performance data for validation. 3. Future centrifuge facility performance parameters are based on Projects P-0 and P2-6 P age

58 OCSD Solids Loading Projection White Paper 92 reports. Options included for current belt press or future centrifuge dewatering at both plant. Options included for current DAFT thickening or future centrifuge thickening of secondary sludge at Plant. 4. 0% Microfiltration (MF) backwash flow to OCSD, and 5% of Reverse Osmosis (RO) flow to OCSD ocean outfall based on GWRS past performance data. 5. Plant Water and GAP water usage are based on the past usage data. Assuming both Plant and GAP water will be recycled back to the treatment process after being used as wash water or process cooling water. 6. Plant recycle flows including the DAFT underflow, Belt Press wash water, filtrate (future centrate), are currently being diverted to Plant 2. Based on SP-73 recommendation, Plant recycle flow will continue to be diverted to Plant 2, and join the Plant 2 recycle flow, and the SARI flow to be treated as non-reclaimable flow at one side of Plant 2 AS plant. In the Model, options are included to change the diversion of Plant recycle flow percentage to Plant Plant and Plant 2 both currently are pumping approximately 6 mgd secondary effluent as Plant Water (PW) to various process area as washing water, including belt press washing water of approximately.6 mgd. The Model assumed the wash water to be recycle back to the process. When switching to centrifuge dewatering, assume PW usage will reduce to approximately 5 mgd. 8. The model Includes diverting 0,000 cuft (0.075 mgd) of primary sludge from Plant to Plant 2 during fiscal year of 204. For future projection, once Project P-0 is completed, assume no sludge diversion from Plant to Plant For the flow diversion among the secondary treatment facilities, assuming first fill the trickling filter (TF) capacity because the TF treatment has the lower operation cost. 0. Per OCWD requirement, TF flow will not be more than 25% of the total secondary effluent to GWRS from Plant.. Based on the 204 plant performance, about 3 5 mgd Plant secondary effluent discharges to ocean outfall when the plant s peak flow exceeds current GWRS capacity. For future projection, assume no Plant secondary effluent discharges to ocean with the OCSD flow equalization in operation in 205 if the secondary effluent is less than the GWRS need. If Plant secondary effluent exceed the WGRS need, the excess flow will go to the Ocean Outfall. 2. GWRS Final Expansion flow conditions was built into model for conditions after Plant 2 TF/SC secondary effluent will be pumped to GWRS if Plant secondary effluent is less than the required 70 mgd flow to GWRS, or 75 mgd total to OCWD. 3. For 2070 ultimate condition, assume additional secondary treatment process will be expansion of AS2 Plant at Plant, and expansion of TF/SC Plant at Plant Projection of Loadings for Solids Facilities Design Use the mass balance model, this White Paper projected the future design loadings to solids handling facilities. A few guidelines were considered for the process loading projections:. At minimum, the total treatment capacity at the two Plants needs to be capable to handle 7 P age

59 OCSD Solids Loading Projection White Paper the total raw sewage influent loadings to both Plants. 2. For normal operation, Plant needs to meet the GWRS Initial Expansion flow requirements, but will not take additional flow beyond what is required for the GWRS Initial Expansion. Equality split flows between Plant and Plant 2 could be an option when Plant 2 GWRS Final Expansion improvements completed. 3. At minimum, new facility capacity need to match the capacities of the existing major treatment processes. Per the Director of Engineering-OCSD shall maintain treatment capacity to keep a resilient facility. By using the approach above, this White Paper projected loadings evaluating several conditions using the mass balance model developed. Condition : Use the total projected flows and loadings at design year of 2035 by this White Paper, and assume 25 mgd of influent flow to Plant and remaining goes to Plant 2. This is the future normal operation condition. For solids projection purpose, lower bound flow and associated higher strength TSS and BOD influent was used for worst case loading at Plant. The following are the summary of assumptions for Condition. Total influent flow mgd Plant raw influent 25 mgd Plant 2 raw influent 75 mgd Total TSS Loading 564,000 lb/day Total BOD Loading 496,000 lb/day TSS Strength 340 mg/l BOD strength 300 mg/l Condition 2: Split the total projected flow and loadings at design year of 2035 between the two Plants evenly at 50%. This generate worse loading condition for Plant 2. For solids projection purpose, lower bound flow and associated higher strength TSS and BOD influent was used for worst case loading at Plant 2. The following are the summary of assumptions for Condition 2. Total influent flow mgd Plant raw influent 00 mgd Plant 2 raw influent 00 mgd Total TSS Loading 564,000 lb/day Total BOD Loading 496,000 lb/day TSS Strength 340 mg/l BOD strength 300 mg/l Condition 3: Use the design capacities of the current primary and secondary treatment processes of each Plant, and similar design solids strengths that were used previously. The design capacities and previous solids projections had been reviewed and summarized in Table 6. The following are the summary of assumptions for Condition 3. 8 P age

60 OCSD Solids Loading Projection White Paper Total influent flow mgd Plant raw influent 50 mgd Plant 2 raw influent 44 mgd TSS Strength 270 mg/l BOD strength 250 mg/l Condition 4: Use the ultimate 2070 flow projection by 2009 Master Plan and the previous projection of ultimate major treatment process capacities. This will set the design criteria for space planning for future expansion. Total influent flow mgd Plant raw influent 235 mgd Plant 2 raw influent 235 mgd TSS Strength 270 mg/l BOD strength 250 mg/l The model run results for the above conditions are attached and summarized in Table 6. The projection results are compared to the previous projections for validation. Based on the results, within those four Conditions, the highest solids loadings to Plant happens at Condition, which is the condition that when Plant solids strength reach the 2035 projected strength and flows remain at 25 mgd. Therefore, Condition loadings are recommended as the design loadings to Plant future solids facilities. The loadings at Condition is very close to Plant capacity. This is the reason that Plant should not take more than 25 mgd flow. The highest solids loadings to Plant 2 happens at Condition 3, which is at the current Plant 2 design capacity. Therefore, Condition 3 loadings are recommended as the design loadings to Plant 2 future solids facilities. Table 7 summarized the recommended design loadings for future solids handling facilities. Annual average loadings are projected from the mass balance model. The peaking factors are based on historical operation data and previous projections. The primary and secondary sludge concentration are based on the current operation data. paper 9 P age

61 OCSD Solids Loading Projection White Paper Attachments 0 P age

62 OCSD Solids Loading Projection White Paper P age

63 Table - OCSD Historical Flow and Loading Summarization OCSD Solids Loading Projection White Paper P+P2 Total Flow mgd P+P2 Total TSS lb/day P+P2 Total BOD lb/day Year P Flow mgd P2 Flow mgd P TSS mgd P2 TSS mg/l P BOD mg/l P2 BOD mg/l P TSS lb/day P BOD lb/day P2 TSS lb/day P2 BOD lb/day ,65 53, , , , , ,574 65, , , , , ,037 55, ,7 297, , , ,73 78, , , , , ,38 95, , , , , ,08 90, , , , , ,945 88, ,065 25, ,00 439, ,452 85, , , , , ,8 84,77 272, , ,48 434, , , , , ,60 460, ,6 204, , , , , ,53 206,747 39, , , , , ,5 34, , , , ,895 27,875 36, , , , , ,387 36,4 24, , , ,737 26,62 292, , , , ,65 238,753 90, , ,865 44, , , ,254 86, , , , ,384 8,764 9, ,40 44, , , ,288 94, , , , ,04 269,582 95, ,06 443, ,86 260, ,495 75, ,3 435, ,450 32, ,663 8, ,3 493,895 2 P age

64 Main Street Meter Reading Table 2 - IRWD Historical Flows and Loadings to OCSD Other IRWD/OCSD Areas Flow MWRD Sludge Flow RA4 Raw Sewage FLow Total Net RA4 Flow to OCSD MWRP Sludge TSS OCSD Solids Loading Projection White Paper IRWD Raw Sewage TSS (mg/l) RA4 Raw Sewage TSS Total Net RA4 TSS to OCSD (lb/day) MWRP Sludge BOD IRWD Raw Sewage BOD (mg/l) RA4 Raw SewageBOD Total Net RA4 BOD to OCSD (lb/day) Year (mgd) 2 (mgd) 3 (mgd) 4 (mgd) 5 (mgd) 6 (lb/day) 7 (lb/day) 8 (lb/day) 7 (lb/day) , ,64 36,980 6,507 98,74 28, , ,447 4,206 7, ,8 30, , ,649 42,807 9, ,789 32, , ,469 44,885 9, ,788 34, , ,553 53,726 20, ,484 4, , ,605 58,645 2, ,468 45, , ,32 56,237 22, ,845 43, , ,26 62,76 23, ,380 47, , ,290 56,57 23, ,8 43, , ,967 67,958 35, ,543 43, , ,235 7,505 26, ,643 33, , ,46 67,959 27, ,222 32, , ,449 69,263 26, ,859 33, , ,405 70,855 30, ,064 36, , ,597 64,380 35, ,346 4, , ,390 68,324 24, ,869 30, , ,90 80,950 36, ,8 48,908 Notes:. Flows after 2003 are summarized from OCSD Gallonge report. Flows prior to 2003 are from previous data from IRWD. 2. Main Street Flume Meter Reading - includes IRWD raw sewage, IRWD sludge, and urban runoff flows. 3. Other IRWD/OCSD Area Flows - Calculated flows includes raw sewage flows from IRWD service areas that not included in the Main Street Meter Reading, deducted the flows from OCSD service areas that contribute to IRWD system. Negative numbers indicated that more flow from OCSD to IRWD than flows from IRWD to OCSD. 4. IRWD Sludge - includes the primary and secondary treated sludge from IRWD. The sludge flow are included in the Main Street Meter reading 5. Total RA4 Raw Sewage to OCSD - Calculated flows including all the raw sewage flows from IRWD service area deducted the flows from OCSD service are to IRWD. 6. Total Net RA4 Flow to OCSD - Calculated flow including the net raw sewage and sludge flows from IRWD to OCSD deducted the flows from OCSD service area to IRWD. 7. IRWD Raw sewage TSS and BOD loadings after 2008 are calculated from the strength in the IRWD annual report to OCSD Finance. Data prior to 2008 are from previous information from IRWD. 8. IRWD sludge TSS and BOD loadings prior to 2008 are from the Mass Balance Model results from in the annual report from IRWD to OCSD Finance. Data prior to 2008 are by calculation from recorded TSS and BOD strength and flow. 3 P age

65 OCSD Solids Loading Projection White Paper Table 3 - IRWD Flows and Loadings Projection MWRD RA4 Raw Sewage Total Net MWRP IRWD Raw RA4 Raw Total Net RA4 TSS MWRP Sludge IRWD Raw Sewage RA4 Raw Total Net RA4 BOD Sludge Flow FLow RA4 Flow to Sludge TSS Sewage TSS Sewage TSS to OCSD BOD BOD SewageBOD to OCSD Year (mgd) (mgd) 2 OCSD (mgd) (lb/day) (mg/l) 3 (lb/day) 4 (lb/day) (lb/day) (mg/l) 3 (lb/day) 4 (lb/day) , ,927 74,927 37, ,093 49, , ,502 44,502 8, ,64 30, ,03 4, ,56 3, ,73 4, ,723 3, ,386 5, ,34 4, ,07 6, ,930 4, ,786 6, ,572 5, ,533 7, ,243 6, ,33 8, ,942 6, ,28 9, ,67 7, ,979 9, ,432 8, ,868 20, ,225 9, ,797 2, ,053 20, ,767 22, ,96 20, ,780 23, ,86 2, ,838 24, ,755 22, ,944 25, ,735 23, ,098 27, ,756 24, ,304 28, ,822 25,822 Notes:. Assume IRWD solids facility will start at end of Based on assumtion of population growth in the RA4 area contribute to OCSD sewer system 3. Based on the current TSS and BOD strength and future strength increase due to water conserwation 4 P age

66 OCSD Solids Loading Projection White Paper Table 4 - SAWPA Historical Flows and Loadings Year SAWPA Flow (mgd) SARI Flow (mgd) TSS (mg/l) TSS (lb/d) BOD (mg/l) BOD (lb/d) , , , , , , , , , , ,33 39, ,06 7 0, , , ,272 9, , , ,42 8 7, , , , , ,59 4 3, , , , , , ,60 Notes: Flows after from fiscal year of are from OCSD Gallonage report. BOD and TSS concentration from Source Control Sampling records. Flow and concentration prior to was from previous study reports. Table 5 - SAWPA Flows and Loadings Projection Year Flow (mgd) TSS (mg/l) TSS (lb/d) BOD (mg/l) BOD (lb/d) , , , , , , ,3 50 5, , , , , , , , , , , , , , , ,6 50 8, , , , , , , , , ,90 50, ,48 50, , ,50 Notes: Flow Projection are based on SAWPA draft flow projection Future BOD and TSS concentration used are based on the assumption that the flows from the desalters will remain the dominate contribution with the possibility of some future high strength industrial waste contribution. 5 P age

67 OCSD Solids Loading Projection White Paper Table 6 - OCSD Historical Urban Runoff Flow Year Flow (mgd) Year Flow (mgd) P age

68 OCSD Solids Loading Projection White Paper Table 7 - OCSD Service Area Population Summary and Projection Year OCSD Plants Tributary Areas Population MWRP (IRWD SA4) Totoal OCSD Service Area Population ,4,709 9,47 2,333, ,48,763 99,930 2,348, ,55, ,822 2,364, ,62,03 28,09 2,380, ,68,22 227,809 2,396, ,74, ,94 2,42, ,80, ,592 2,427, ,87, ,557 2,443, ,94,84 264,848 2,459, ,200, ,477 2,474, ,206, ,456 2,490, ,26, ,005 2,505, ,226,75 293,626 2,520, ,236, ,322 2,535, ,247,2 303,092 2,550, ,257, ,939 2,565, ,268,779 34,732 2,583, ,280,22 32,676 2,60, ,29, ,772 2,620, ,303, ,025 2,639, ,34, ,438 2,657, ,322, ,205 2,669, ,330,322 35,03 2,68, ,338,34 354,863 2,693, ,346,37 358,755 2,705, ,354, ,690 2,77, ,359,90 364,74 2,724, ,365, ,663 2,73, ,37,09 367,59 2,738, ,376, ,66 2,745, ,382, ,69 2,752, ,387,68 370,752 2,757, ,39,987 37,335 2,763, ,396,87 37,99 2,768, ,40, ,505 2,774, ,406, ,09 2,779, ,42,05 373,207 2,785, ,47, ,323 2,790, ,423,78 373,439 2,796, ,428, ,555 2,802, ,434, ,67 2,808,023 Note: 2000 data are from 2009 Facility Master Plan, which was based on 2004 CDR. 2000, 2005 and 200 data are from , and Asset Management Plan, which was based on 200 CDR. 205, 2020, 2035 and 2040 data are from CDR projection requested by Planning in 206. The population in the years between the five years interval were calculated assuming constant growth rate. Table 8 - OCSD Service Area Population in 5yr Increment Tributary Area OCSD Plant Subtotal 2,4,709 2,74,067 2,206,434 2,257,325 2,34,368 2,354,329 2,382,358 2,406,504 2,434,352 MWRP (IRWD SA 4) 9,47 237,94 284, , , , ,69 373,09 373,67 Service Area Total 2,333,26 2,42,008 2,490,890 2,565,264 2,657,806 2,77,09 2,752,527 2,779,595 2,808,023 7 P age

69 OCSD Solids Loading Projection White Paper Table 9 - Historical Flow Aalaysis Total (P+P2) Flows from Tributary Areas Population = (P+P2) Recorded FLows - SAWPA Flow - RA4 Raw Sewage and Sludge Flows - Urban Runoff flow FLow Gallon Per Capita per Day (gpcd) = Total (P+P2) Flows from Tributaty Area Population/Total (P+P2) Tributary Areas Population Year Population Flow, mgd OCSD Total Serviuce Area Population P+P2 Tributary Area Population Flow from Tributary Area Population P+P2 RA4 Raw MWRP Urban Year P Recorded P2 recorded Total SAWPA Sewage Sludge Runoff ,333,26 2,4, ,348,693 2,48, ,364,364 2,55, ,380,40 2,62, ,396,02 2,68, ,42,008 2,74, ,427,582 2,80, ,443,257 2,87, ,459,032 2,94, ,474,90 2,200, ,490,890 2,206, ,505,590 2,26, ,520,377 2,226, ,535,252 2,236, ,550,24 2,247, ,565,264 2,257, ,583,5 2,268, min. 74 max. 06 Avg. 9 calculated gpcd 8 P age

70 OCSD Solids Loading Projection White Paper Table 0 - Future Flow Projection Future (P+P2) Flows Projection = Flow projection from Tributary Area Population + SAWPA Flow Projection + RA4 Raw Sewage and Sludge Flows Projection + Urban Runoff flow Projection Future Projection use 75 gdpc for upper bound of average OCSD influent flow, and use current 74 gpcd with % decrease every year for lower bound flow. Minimum of 60 gpcd is used for lower bound flow considering the basic human daily need. Year Projected Population OCSD Total Serviuce Area Population P+P2 Tributary Area Population Lower Bound gpcd Used gpcd Upper Bound gpcd Projected Flow, mgd Lower Bound Upper Bound Tributary Area Tributary Area Flow Flow Lower Bound Total Projected Flow Upper Bound Total Projected Flow RA4 Raw MWRP Urban Year SAWPA Sewage Sludge Runoff 207 2,60,888 2,280, ,620,395 2,29, ,639,034 2,303, ,657,806 2,34, ,669,544 2,322, ,68,335 2,330, ,693,77 2,338, ,705,072 2,346, ,77,09 2,354, ,724,084 2,359, ,73,67 2,365, ,738,268 2,37, ,745,388 2,376, ,752,527 2,382, ,757,99 2,387, ,763,322 2,39, ,768,736 2,396, ,774,60 2,40, ,779,595 2,406, P age

71 Table - Historical TSS Loading Aalaysis OCSD Solids Loading Projection White Paper Total (P+P2) Loadings from Tributary Areas Population = (P+P2) Recorded Loadings - SAWPA Loading - RA4 Raw Sewage and Sludge Loadings Loading Pounds Per Capita per Day (ppcd) = Total (P+P2) Loadings from Tributaty Area Population/Total (P+P2) Tributary Areas Population Year Population TSS, lb/day Year OCSD Total Serviuce Area Population P+P2 Tributary Area Population P Recorded P2 recorded P+P2 Total SAWPA RA4 Raw Sewage MWRP Sludge Loading from Tributary Area Population calculated ppcd ,333,26 2,4,709 83, ,065 45,00,63 3,64 23,86 402, ,348,693 2,48,763 74, , ,226 4,685 5,447 25, , ,364,364 2,55,543 79,8 272,299 45,48,634 4,649 28,58 395, ,380,40 2,62,03 93, , ,60 4,997 6,469 28,46 408, ,396,02 2,68,22 83,6 298,668 48,784 0,374 24,553 29,73 44, ,42,008 2,74,067 93,53 39,844 53,358 24,33 27,605 3, , ,427,582 2,80,990 99,940 34,592 54,532 24,06 23,32 32, , ,443,257 2,87, ,895 36, ,364 25,88 28,26 33,95 435, ,459,032 2,94,84 222,225 36,4 538,636 23,272 23,290 33,28 458, ,474,90 2,200, , ,959 52,696 35,079 9,967 57,99 48, ,490,890 2,206, ,65 90, ,865 28,42 0,235 6, , ,505,590 2,26, , ,254 59,028 20,359 6,46 6, , ,520,377 2,226,75 272,637 8, ,40,982 8,449 60,84 373, ,535,252 2,236, , , ,830 2,59 6,405 64,450 44, ,550,24 2,247,2 285, , ,06 9,528 5,597 58,783 48, ,565,264 2,257, ,86 228, ,3,79 7,390 60, , ,583,5 2,268, , , ,3 0,334 3,90 67, , min. 0.6 max. 0.2 Avg P age

72 Table 2 - Future TSS Loading Projection Using 0.2 ppcd OCSD Solids Loading Projection White Paper Future Total (P+P2) Loadings = Total (P+P2) Loadings from Tributary Areas Population Projection + SAWPA Loading Projection + RA4 Raw Sewage and Sludge Flows Projection Year Projected Population Used ppcd Projected TSS, lb/day Projected TSS Strength, mg/l OCSD Total Projected Loading from Conc. at Lower Conc. at Upper Serviuce Area P+P2 Tributary Tributary Area RA4 Raw Bound Projected Bound Projected Year Population Area Population Used ppcd Population SAWPA Sewage MWRP Sludge Total Loadings Flow Flow 207 2,60,888 2,280, ,845 2,00 2,927 62, , ,620,395 2,29, ,24 2,730 3,502 3, , ,639,034 2,303, ,632 3,494 4,03 0 5, ,657,806 2,34, ,07 4,3 4, , ,669,544 2,322, ,69 4,845 5, , ,68,335 2,330, ,368 5,379 6, , ,693,77 2,338, ,046 5,93 6, , ,705,072 2,346, ,726 8,25 7, , ,77,09 2,354, ,409 8,90 8, , ,724,084 2,359, ,58 9,633 9, , ,73,67 2,365, ,756 20,383 9, , ,738,268 2,37, ,933 2,6 20, , ,745,388 2,376, ,3 2,970 2, , ,752,527 2,382, ,295 22,88 22, , ,757,99 2,387, ,305 24,05 23, , ,763,322 2,39, ,37 25,465 24, , ,768,736 2,396, ,33 26,90 25, , ,774,60 2,40, ,348 28,48 27, , ,779,595 2,406, ,366 30,024 28, , P age

73 Table 3- Historical BOD Loading Aalaysis OCSD Solids Loading Projection White Paper Total (P+P2) Loadings from Tributary Areas Population = (P+P2) Recorded Loadings - SAWPA Loading - RA4 Raw Sewage and Sludge Loadings Loading Pounds Per Capita per Day (ppcd) = Total (P+P2) Loadings from Tributaty Area Population/Total (P+P2) Tributary Areas Population Year Population BOD, lb/day Year OCSD Total Serviuce Area Population P+P2 Tributary Area Population P Recorded P2 recorded P+P2 Total SAWPA RA4 Raw Sewage MWRP Sludge Loading from Tributary Area Population calculated ppcd ,333,26 2,4,709 88,072 25,04 439,3 6,398,74 6, , ,348,693 2,48,763 85, , ,424 3,934 3,8 7, , ,364,364 2,55,543 84,77 249, ,673 6,946 2,789 9,59 393, ,380,40 2,62,03 204, , ,402 7,363 4,788 9,686 4, ,396,02 2,68,22 204, ,78 467,37 7,780 2,484 20,234 44, ,42,008 2,74, , , ,692,07 24,468 2,52 42, ,427,582 2,80, ,5 252, ,624 0,890 20,845 22,82 398, ,443,257 2,87,700 27, ,9 485,785 0,024 24,380 23, , ,459,032 2,94,84 227,387 24, ,943 9,822 20,8 23,090 45, ,474,90 2,200,433 26,62 225, ,335 0,87 8,543 35,23 388, ,490,890 2,206, , ,74 44,494 7,88 7,643 26, , ,505,590 2,26, ,457 86, ,363 5,930 5,222 27, , ,520,377 2,226,75 249,384 9,839 44,222 4,87 6,859 26, , ,535,252 2,236, ,282 94, ,547 3,97 5,064 30,976 44, ,550,24 2,247,2 248,04 95,32 443,353 3,46 5,346 35, , ,565,264 2,257, ,549 75, ,605 3,388 6,869 24,054 40, ,583,5 2,268,779 32,250 8, ,3 3,60 2,8 36,790 44, min. 0.7 max Avg P age

74 Table 4- Future BOD Loading Projection Using 0.9 ppcd OCSD Solids Loading Projection White Paper Future Total (P+P2) Loadings = Total (P+P2) Loadings from Tributary Areas Population Projection + SAWPA Loading Projection + RA4 Raw Sewage and Sludge Flows Projection Year Projected Population Used ppcd Projected BOD, lb/day Projected BOD Strength, mg/l OCSD Total Projected Loading from Conc. at Lower Conc. at Upper Serviuce Area P+P2 Tributary Tributary Area RA4 Raw Bound Projected Bound Projected Year Population Area Population Used ppcd Population SAWPA Sewage MWRP Sludge Total Loadings Flow Flow 207 2,60,888 2,280, ,240 5,004 2,093 37, , ,620,395 2,29, ,408 5,304 2,64 8,000 47, ,639,034 2,303, ,572 5,622 3, , ,657,806 2,34, ,730 5,963 3, , ,669,544 2,322, ,245 6,86 4, , ,68,335 2,330, ,76 6,408 4, , ,693,77 2,338, ,280 6,630 5, , ,705,072 2,346, ,800 7,589 6, , ,77,09 2,354, ,323 7,879 6, , ,724,084 2,359, ,383 8,80 7, , ,73,67 2,365, ,446 8,493 8, , ,738,268 2,37, ,5 8,87 9, , ,745,388 2,376, ,578 9,54 20, , ,752,527 2,382, ,648 9,508 20, , ,757,99 2,387, ,562 0,044 2, , ,763,322 2,39, ,478 0,60 22, , ,768,736 2,396, ,395,209 23, , ,774,60 2,40, ,35,84 24, , ,779,595 2,406, ,236 2,50 25, , P age

75 OCSD Solids Loading Projection White Paper Raw Influent Primary Treatment Secondary Treatment DAFT Thickening Slusdge Digestion Digested Sludge Dewatering 204 TPODS Data Mass Model Assumption/Results 204 TPODS Data Mass Model Assumption/Results Flow(mgd) BOD (mg/l) TSS (mg/l) VSS/TSS Ratio (%) BOD removal Rate (%) TSS removal Rate (%) Effluent BOD (mg/l) Effluent TSS (mg/l) Primary Sludge Flow (mgd) 0.60* Primary SludgeTSS (mg/l)) 4,00 4,000 44,800 45,000 Primary Sludge to Plant 2 (cuft/d) 0,000*** 0,000 Primary Sludge to Digesters (lb/day) 205,52 205,538 26, ,327 P AS/P2 AS Plant Influent Flow (mgd) Influent BOD (mg/l) Influent TSS (mg/l) Effluent BOD (mg/l) Effluent TSS (mg/l) Sludge Yield (lb TSS generated/lb BOD removed) 0.83 ** **.0 WAS Flow (mgd) WAS TSS (mg/l) 9,460 0,000 3,260 3,200 WAS TSS (lb/d) 29,747 35,225 49,2 39,77 P AS2 Influent Flow (mgd) Influent BOD (mg/l) 7 42 Influent TSS (mg/l) Effluent BOD (mg/l) 4.0*** 4.0 Effluent TSS (mg/l) 4.2*** 4.0 Sludge Yield (lb TSS generated/lb BOD removed) WAS Flow (mgd) WAS TSS (mg/l) 8,840 0,000 WAS TSS (lb/d) 3,702 40,075 P TF/ P2 TF-SC Influent Flow (mgd) Influent BOD (mg/l) 4*** Influent TSS (mg/l) Effluent BOD (mg/l) Effluent TSS (mg/l) Sludge Yield (lb TSS generated/lb BOD removed) Waste Sludge Flow (mgd) 0.08*** Waste Sludge TSS (mg/l) 20,000*** 20,000 3,506 3,500 Waste SludgeTSS (lb/d) 3,400 3,777 40,340 30,559 Influent Flow (mgd) TWAS TSS (mg/l) 46,000 46,000 56,900 57,000 TWAS Flow (mgd) TWAS (lb/d) 57,546 75,300 45,60 68,822 Capture Rate (%) Digester Influent Flow (mgd) Influent TSS (mg/l) 40,00 40,38 46,246 47,6 Influent TSS (lb/d) 277, , ,700 36,49 VSS reduction rate (%) Influent Flow (mgd) Influent Solids (mg/l) 2,900 22,56 27,200 27,0 Influent Solids (lb/d) 62,555 62,4 36,09 8,736 Cake thickeness (% solids) Capture rate (%) Cake Production (wet ton/day) * Sludge pumped to digesters. Excluded the sludge to Plant 2. ** Formula on MSO indicated the yield recorded were based on VSS generated/bod removed *** No data recorded on TPODS. Numbers are estimated from MSO data. Number in color blue are used as input assumptions in the mass Balance model. Table 5 - Mass Balance Validation Plant Plant 2 24 P age

76 OCSD Solids Loading Projection White Paper Table 6 - Future Loading Projection Summary Previous Projections Projection by This White Paper P Primary (P33, P-37) Secondary (P-76, P-82, P-02) Solids Facilities (P-0) Ultimate Capacity w/future Expansion Ultimate Capacity w/future Expansion Ultimate Capacity w/future Expansion Condition Flow and solids strength w/25 mgd to P Condition Flow and strength w/50% flow to each Plant Condition 3 - Match Existing Flow Capacity and Design Solids Strength Condition 4 - Ultimate Plant Capacity Current Capacity Current Capacity Current Capacity Treatment Process Annual Average Capacity (mgd) Annual Average Influent Capacity (mgd) Raw Influent BOD (mg/l) Raw Influent TSS (mg/l) Primary Sludge Production (lb/day) 243,678 34,39 294, , , , ,9 440,365 WAS Sludge Production (lb/day) 06,600 48,700 76,000 36,000 0,08 75,274 05,7 7,29 TF Sludge Production (lb/day) 8,900 8,900 3,300 4,700 4,046 3,447,2,659 Total Sludge Production at Current Capacity(lb/day) 369, , ,727 32, ,203 Total Sludge Production at Ultimate Capacity(lb/day) 508, , ,35 P2 Primary Ultimate Capacity w/future Expansion Secondary (P2-42-2, P2-74, P2-90) Ultimate Capacity w/future Expansion Solids Facilities (P2-89, P2-9,P2-92) Ultimate Capacity w/future Expansion Condition Flow and solids strength w/75 mgd to P2 Condition Flow and strength w/50% flow to each Plant Condition 3 - Match Existing Flow Capacity and Design Solids Strength Condition 4 - Ultimate Plant Capacity Current Capacity Current Capacity Current Capacity Treatment Process Annual Average Capacity (mgd) Annual Average Influent Capacity (mgd) Raw Influent BOD (mg/l) Raw Influent TSS (mg/l) Primary Sludge Production (lb/day) 234, , ,00 95,43 249,272 29, ,776 WAS Sludge Production (lb/day) 88,000 83,400 30,645 46,848 68,524 69,937 TF/SC Sludge Production (lb/day) 38,60 95,400 46,800 32,02 38,742 35,774 88,239 Total Sludge Production at Current Capacity(lb/day) 355, , , , ,70 Total Sludge Production at Ultimate Capacity(lb/day) 558,700 63, P age

77 OCSD Solids Loading Projection White Paper Table 7 - Recommended Design Loadings for Solids Handling Facilities Design Loadings for Ultimate Solids Design Loadings for Future Solids Handling Facilities Handling Facilities ( for Space Planning Purpose) Annual Average 29,000 44,000 Primary Sludge Dry Solids (ppd), 5-day Maximum 350, ,000 and Concentration(% of solids) Maximum Day 466, ,000 Concentration 4.% 4.% Annual Average 02,000 72,000 WAS Dry Solids (ppd), and 5-day Maximum 23, ,000 Concentration(% of solids) Maximum Day 64, ,000 P Concentration.0%.0% Annual Average 5,000 2,000 TF Sludge Dry Solids (ppd), and 5-day Maximum 8,000 5,000 Concentration(% of solids) Maximum Day 24,000 20,000 Concentration 2.0% 2.0% Annual Average 408, ,000 Total Sludge Dry Solids, ppd 5-day Maximum 49, ,000 Maximum Day 654,000,096,000 Annual Average 292, ,000 Primary Sludge Dry Solids (ppd), 5-day Maximum 35, ,000 and Concentration(% of solids) Maximum Day 468, ,000 Concentration 4.5% 4.5% Annual Average 69,000 70,000 WAS Dry Solids (ppd), and 5-day Maximum 83,000 84,000 Concentration(% of solids) Maximum Day,000 2,000 P2 Concentration 0.32% 0.32% Annual Average 36,000 89,000 TF Sludge Dry Solids (ppd), and 5-day Maximum 44,000 07,000 Concentration(% of solids) Maximum Day 58,000 43,000 Concentration 0.35% 0.35% Annual Average 397, ,000 Total Sludge Dry Solids, ppd 5-day Maximum 478, ,000 Maximum Day 637,000,04,000 Note: Used Peaking Factor of.2 for 5-day Maximum, and.6 for Peak Day as recommended by previous studies. 26 P age

78 OCSD Solids Loading Projection White Paper Plant - Liquid Process Mass Balance (204 Loadings) DAFT UNDERFLOW FLOW (mgd) = 0.7 FLOW (GPM) = 49 TSS (mg/l) = 64 VSS (mg/l) = 5 CENGEN COOLING WATER 2 MGD TSS (lb/d) = 377 VSS (lb/d) = 30 MF BACKWASH AS INFLUENT FLOW (mgd) = 38 BOD (mg/l) = 32 TSS (mg/l) = 78 RAW INFLUENT PRIMARY INFLUENT VSS (mg/l) = 62 AS EFFLUENT COMBINED Flow (mgd) = 96 Flow (mgd) = 99 PRIMARY EFFLUENT SECONDARY INFLUENT BOD (lb/d) = 4,945 FLOW (mgd) = 37.6 SECONDARY EFFLUENT MF INFLUENT MF BACKWASH MF EFFLUENT/RO INFLUENT BOD (mg/l) = 30 BOD (mg/l) = 306 Flow (mgd) = 98 Flow (mgd) = 07 TSS (lb/d) = 24,6 BOD (mg/l) = 4.5 FLOW (mgd) = 09 FLOW (mgd) = 93 FLOW (mgd) = 9 FLOW (mgd) = 84 TSS (mg/l) = 356 TSS (mg/l) = 35 BOD (mg/l) = 54 BOD (mg/l) = 42 VSS (lb/d) = 9,689 TSS (mg/l) = 4.0 BOD (mg/l) = 6.8 BOD (mg/l) = 6.8 BOD (mg/l) = 50 BOD (mg/l) = 2 BOD (lb/d) = 248,98 BOD (lb/d) = 252,089 TSS (mg/l) = 88 TSS (mg/l) = 82 VSS (mg/l) = 3.2 TSS (mg/l) = 6.8 TSS (mg/l) = 6.8 TSS (mg/l) = 50 TSS (mg/l) = 2 TSS (lb/d) = 285,028 TSS (lb/d) = 288,938 VSS (mg/l) = 7 VSS (mg/l) = 66 BOD (lb/d) =,4 BOD (lb/d) = 6,97 BOD (lb/d) = 5,287 BOD (lb/d) = 3,89 BOD (lb/d) =,397 VSS (lb/d) = 242,274 VSS (lb/d) = 245,597 BOD (lb/d) = 26,045 BOD (lb/d) = 27,44 ACTIVATED SLUDGE PLANT NO. (P-82) TSS (lb/d) =,255 TSS (lb/d) = 6,29 TSS (lb/d) = 5,307 TSS (lb/d) = 3,90 TSS (lb/d) =,397 VSS/TSS= 85% VSS/TSS= 85% TSS (lb/d) = 72,234 TSS (lb/d) = 73,63 VSS (lb/d) =,004 VSS (lb/d) = 57,788 VSS (lb/d) = VSS/TSS Ratio 80% OCWD GWRS RAW SEWAGE HEADWORKS & VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS GWRS PRODUCT WATER 7 MGD INFLUENT MICROFILTRATION REVERSE OSMOSIS INFLUENT PRIMARY CLARIFIERS PUMP STATION BOD Removal = 50% TSS Removal = 75% lbs TSS Yield / lb BOD Removed = 0.90 VSS/TSS Ratio 80% RO DISCHARGE TO OCEAN OUTFALL 3 MGD SOLIDS FROM CHEM FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) OCSD GREEN ACRES 5 MGD Dose (mg/l) = 20 TSS (lb/d) = 6,03 MISCELLANEOUS PROCESS WASH WATER FLOW POLYMER SOLIDS AS WAS PW PS 0.3 MGD FLOW (mgd) = 2.7 Dose (mg/l) = 0.2 FLOW (mgd) = MGD (BECOME WASHWATER) GAP WATER FROM OCWD BOD (mg/l) = - TSS (lb/d) = 60 TSS (mg/l) = 0,000 TSS (mg/l) = - VSS (mg/l) = 8,000 BOD (lb/d) = 0 TSS (lb/d) = 35,225 TSS (lb/d) = 0 VSS (lb/d) = 28,80 SECONDARY EFFLUENT TO OCEAN OUTFALL 5 MGD VSS (lb/d) = 0 Dry Solids.00% PRIMARY SLUDGE VSS/TSS Ratio 80% Note: Secondary effluent to ocean include TF effluent rejected by GWRS plus flow loss during the diurnal peak (roughly 3-5 mgd). FLOW (mgd) = 0.68 AS2 INFLUENT.6 MGD RECYCLE FLOW TO P BOD (mg/l) = 22,9 FLOW (mgd) = 45 BELT PRESS WASHING WATER FLOW (mgd) = 0.00 TSS (mg/l) = 4,000 Dry Solids Conc.= 4.% BOD (mg/l) = 42 FLOW (GPM) = 0 VSS (mg/l) = 32,800 TSS (mg/l) = 82 AS2 EFFLUENT TSS (mg/l) = DIV/0! BOD (lb/d) = 26,045 VSS (mg/l) = 66 FLOW (mgd) = 44.5 VSS (mg/l) = DIV/0! TSS (lb/d) = 232,876 VSS/TSS Ratio= 80% BOD (lb/d) = 53,435 BOD (mg/l) = 4.0 TSS (lb/d) = - VSS (lb/d) = 86,30 TSS (lb/d) = 30,873 TSS (mg/l) = 4.0 VSS (lb/d) = - VSS (lb/d) = 24,698 VSS (mg/l) = 3.2 VSS/TSS RATIO 70% BOD (lb/d) =,485 ACTIVATED SLUDGE PLANT NO. 2 (P-02) TSS (lb/d) =,485 VSS (lb/d) =,88 VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS lbs TSS Yield / lb BOD Removed = 0.80 RETURN ACTIVATED SLUDGE (RAS) AS2 WAS FLOW (mgd) = 0.48 TSS (mg/l) = 0,000 VSS (mg/l) = 8,000 TSS (lb/d) = 40,075 VSS (lb/d) = 32,060 Dry Solids.00% VSS/TSS Ratio 80% TF EFFLUENT FLOW (mgd) = 27 BOD (mg/l) = 4.7 TSS (mg/l) = 5.5 TF INFLUENT VSS (mg/l) = % Note: GWRS only take TF EF up to 25% of toal SE FLOW (mgd) = 27 TRICKLING FILTER (P-76) BOD (lb/d) = 3, mgd (AS EF + AS2 EF + TF EF)*25% BOD (mg/l) = 42 TSS (lb/d) = 3,480 0 mgd If TF EF less than 25%, 0 mgd to ocean outfall TSS (mg/l) = 82 TRICKLING VSS (lb/d) = 2,784 VSS (mg/l) = 66 TRICKLING FILTER VSS/TSS Ratio 80% BOD (lb/d) = 32,06 FILTERS SECONDARY TSS (lb/d) = 8,524 CLARIFIERS VSS (lb/d) = 4,89 lbs TSS Yield / lb BOD Removed = 0.60 COMBINED WAS PRIMARY SLUDGE FLOW (mgd) = 0.90 FLOW (mgd) = 0.08 TSS (mg/l) = 0,000 BOD (mg/l) = 22,9 VSS (mg/l) = 8,000 TSS (mg/l) = 4,000 TSS (lb/d) = 75,300 TRICKLING FILTER SLUDGE VSS (mg/l) = 32,800 VSS (lb/d) = 60,240 FLOW (mgd) = 0.08 BOD (lb/d) = 4,806 TSS (mg/l) = 20,000 TSS (lb/d) = 27,355 VSS (mg/l) = 6,000 VSS (lb/d) = 2,884 TSS (lb/d) = 3,777 VSS (lb/d) =,022 Dry Solids 2.00% TO PLANT 2 VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 27 P age

79 OCSD Solids Loading Projection White Paper Plant - Solids Process Mass Balance (204 Loadings) BLENDED CENTRIFUGE INFLUENT POLYMER FLOW THICKENED SLUDGE DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 0.00 ACTIVE (lb/d)= - FLOW (mgd) = 0.00 FLOW (mgd) = 0.88 FLOW (mgd) = 0.88 ACTIVE (lb/d)= - SOLIDS (LB/D) = - FLOW (GPM) = 0 ACTIVE (gpd)= - FLOW (GPM) = 0 FLOW (GPM) = 60 FLOW (GPM) = 60 ACTIVE (gpd)= - CAKE WET TONS = - TSS (mg/l) = DIV/0! FLOW(gpm)= - TSS (mg/l) = 60,000 TSS (mg/l) = 40,38 TSS (mg/l) = 22,56 FLOW(gpm)= - CAKE (CF/D) = - VSS (mg/l) = DIV/0! VSS (mg/l) = 48,000 VSS (mg/l) = 32,0 VSS (mg/l) = 4,28 CAKE (CFM) = - TSS (lb/d) = - TSS (lb/d) = - TSS (lb/d) = 294,222 TSS (lb/d) = 62,4 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = - VSS (lb/d) = - VSS (lb/d) = 235,378 VSS (lb/d) = 03,566 LB/CF PRIMARY SLUDGE VSS/TSS RATIO 80% FLOW (mgd) = 0.60 TSS (mg/l) = 4,000 CENTRIFUGE DIGESTER CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS TRUCK LOADOUT VSS (mg/l) = 32,800 0% 00% CO-THICKENNING CENTRIFUGE DIGESTER 0% 00% 394 WET TONS/DAY TSS (lb/d) = 205,52 CAKE THICKENESS 28% 463 CY/DAY VSS (lb/d) = 64,47 PRODUCT SOLIDS CONCENTRATION 6% WORKING VOLUME CUFT 2,577,540 COLIDS CAPTURE RATE 97% COLIDS CAPTURE RATE 95% CENTRATE INCLUDE POLYMER HRT 2.9 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 5,000 POLYMER DOSE 5 lb/dt FLOW (mgd) = 0.00 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 0.00 HRT (DAYS) 4. EMULSION POLYMER FLOW (GPM) = 0 SOLIDS (LB/D) = 57,538 PERCENT ACTIVE 40% FLOW (GPM) = 0 PERCENT ACTIVE 40% TSS (mg/l) = DIV/0! (HRT need 6-7 days for at least sub-class B) CAKE WET TONS = 394 FINAL DILUTION 0.2% TSS (mg/l) = DIV/0! FINAL DILUTION 0.2% VSS (mg/l) = DIV/0! CAKE (CF/D) = 2,503 POLYMER DENSITY 8.59 lb/g TSS (lb/d) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = - CAKE (CFM) = 8.7 VSS (lb/d) = - CAKE SPECIFIC WEIGHT 63 VSS/TSS RATIO 80% LB/CF COMBINED WAS FLOW (mgd) = 0.90 DAFT WAS INFLUENT BELT PRESS WASH WATER.6 MGD BELT-PRESS DEWATERING TSS (mg/l) = 0,000 CENTRIFUGE DAFT FLOW (mgd) = 0.90 THICKENED WAS VSS (mg/l) = 8,000 0% 00% FLOW (GPM) = 627 FLOW (mgd) = 0.20 TSS (lb/d) = 75,300 TSS (mg/l) = 0,000 FLOW (GPM) = 36 CAKE THICKENESS 20.0% VSS (lb/d) = 60,240 VSS (mg/l) = 8,000 TSS (mg/l) = 46,000 COLIDS CAPTURE RATE 97% TSS (lb/d) = 75,300 VSS (mg/l) = 36,800 WSAH WATER.6 MGD VSS (lb/d) = 60,240 TSS (lb/d) = 74,924 FILTRATE VSS (lb/d) = 59,939 FLOW (mgd) = 0.79 VSS/TSS RATIO 80% FLOW (GPM) = 545 DAFT (WAS THICKENNING) TSS (mg/l) = 744 TSS (lb/d) = 4,872 TRICKLING FILTER SLUDGE PRODUCT SOLIDS CONCENTRATION 4.6% FLOW (mgd) = 0.08 COLIDS CAPTURE RATE 99.5% TSS (mg/l) = 20,000 CENTRIFUGE DIGESTER VSS (mg/l) = 6,000 0% 00% TSS (lb/d) = 3,777 TOTAL WASTE FLOW VSS (lb/d) =,022 DAFT UNDERFLOW FLOW (mgd) = 2.4 FLOW (mgd) = 0.7 FLOW (GPM) = 657 FLOW (GPM) = 49 TSS (mg/l) = 245 TOTAL RECYCLE FLOW RECYCLE FLOW TO P TSS (mg/l) = 64 TSS (lb/d) = 4,872 FLOW (mgd) = 2.4 FLOW (mgd) = 0.00 VSS (mg/l) = 5 FLOW (GPM) = 657 FLOW (GPM) = 0 TSS (lb/d) = 377 TSS (mg/l) = 264 TSS (mg/l) = DIV/0! VSS (lb/d) = 30 VSS (mg/l) = 85 VSS (mg/l) = DIV/0! VSS/TSS RATIO 80% TSS (lb/d) = 5,249 TSS (lb/d) = - VSS (lb/d) = 3,674 VSS (lb/d) = - VSS/TSS RATIO 70% VSS/TSS RATIO 70% P P2 DAFT Underflow 0% 00% TO AS INFLUENT RECYCLE FLOW TO P2 FLOW (mgd) = 2.4 FLOW (GPM) = 657 TSS (mg/l) = 264 VSS (mg/l) = 85 TSS (lb/d) = 5,249 VSS (lb/d) = 3,674 VSS/TSS RATIO 70% 28 P age

80 OCSD Solids Loading Projection White Paper Plant 2 - Liquid Process Mass Balance (204 Loadings) RAW INFLUENT PRIMARY INFLUENT Flow (mgd) = 02 Flow (mgd) = 5 PRIMARY EFFLUENT AS PLANT INFLUENT AS EFFLUENT BOD (mg/l) = 230 BOD (mg/l) = 29 Flow (mgd) = 4 FLOW (mgd) = 54 FLOW (mgd) = 52.9 TSS (mg/l) = 37 TSS (mg/l) = 322 BOD (mg/l) = 88 BOD (mg/l) = 88 BOD (mg/l) = 4.0 BOD (lb/d) = 95,656 BOD (lb/d) = 20,462 TSS (mg/l) = 8 TSS (mg/l) = 8 TSS (mg/l) = MGD GAP WATER FROM OCWD TSS (lb/d) = 269,666 TSS (lb/d) = 309,26 BOD (lb/d) = 84,85 BOD (lb/d) = 40,033 BOD (lb/d) =,765 P OUTFALL EFFLUENT VSS (lb/d) = 229,26 VSS (lb/d) = 259,574 TSS (lb/d) = 77,282 TSS (lb/d) = 36,75 PURE OXYGEN ACTIVATED SLUDGE PLANT TSS (lb/d) = 2,427 6 MG 8 MG VSS/TSS= 85% PW RAW SEW RAW SEWAGE HEADWORKS & INFLUENT AERATION BASINS SECONDARY CLARIFIERS TOTAL OCEAN OUTFALL 23 MG PUMP STATION INFLUENT INFLUENT PRIMARY CLARIFIERS BOD Removal = 60% TSS & VSS Removal = 75% lbs TSS Yield / lb BOD Removed =.0 COMBINED P2 SECONDARY EFFLUENT FLOW (mgd) = 0.08 P RECYCLE FLOW TO P2 SOLIDS FROM CHEM FLOW (mgd) = 2 BOD (mg/l) = 22,9 FLOW (mgd) = 2.39 FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) BOD (mg/l) = 4.8 TSS (mg/l) = 4,000 FLOW (GPM) = 657 Dose (mg/l) = 8 TSS (mg/l) = 7.6 VSS (mg/l) = 32,800 TSS (mg/l) = 264 TSS (lb/d) = 5,32 BOD (lb/d) = 4,469 BOD (lb/d) = 4,806 VSS (mg/l) = 85 POLYMER SOLIDS AS WAS TSS (lb/d) = 7,098 TSS (lb/d) = 27,355 TSS (lb/d) = 5249 Dose (mg/l) = 0.2 FLOW (mgd) =.49 VSS (lb/d) = 2,884 VSS (lb/d) = 3674 TSS (lb/d) = 70 TSS (mg/l) = 3,200 VSS (mg/l) = 2,720 P RECYCLE FLOW TO P2 TSS (lb/d) = 39,668 VSS (lb/d) = 33,77 Dry Solids 0.32% PRIMARY SLUDGE VSS/TSS Ratio 85% P2 RECYCLE FLOW PLUS PW/GAP WASHWATER FLOW (mgd) = 0.66 P PRIMARY SLUDGE DIVERSION FLOW (mgd) = 0.60 BOD (mg/l) = 22,976 FLOW (GPM) = 7359 TSS (mg/l) = 45,000 Dry Solids Conc.= 4.5% TSS (mg/l) = 78 VSS (mg/l) = 33,300 VSS/TSS Ratio= 74% VSS (mg/l) = 54 BOD (lb/d) = 26,277 TF/SC EFFLUENT TSS (lb/d) = 6857 TSS (lb/d) = 247,327 FLOW (mgd) = 59 VSS (lb/d) = 4800 VSS (lb/d) = 83,022 BOD (mg/l) = 5.5 TSS (mg/l) = 9.5 BOD (lb/d) = 2,704 TRICKLING FILTER (P2-90) TSS (lb/d) = 4,67 TF/SC INFLUENT FLOW (mgd) = 60 TRICKLING TRICKLING BOD (mg/l) = 88 FILTERS FILTER TSS (mg/l) = 8 /SOLIDS SECONDARY BOD (lb/d) = 44,52 CONTACT CLARIFIERS TSS (lb/d) = 40,53 lbs TSS Yield / lb BOD Removed = 0.85 COMBINED SECONDARY SLUDGE FLOW (mgd) = 2.53 TSS (mg/l) = 3,324 VSS (mg/l) = 2,753 TSS (lb/d) = 70,227 TF/SC WSS VSS (lb/d) = 58,65 FLOW (mgd) =.05 TSS (mg/l) = 3,500 VSS (mg/l) = 2,800 TSS (lb/d) = 30,559 VSS (lb/d) = 24,448 Dry Solids 0.35% VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 29 P age

81 OCSD Solids Loading Projection White Paper Plant 2 - Solids Process Mass Balance (204 Loadings) DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 0.80 FLOW (mgd) = 0.80 ACTIVE (lb/d)= - SOLIDS (LB/D) = - FLOW (GPM) = 558 FLOW (GPM) = 558 ACTIVE (gpd)= - CAKE WET TONS = - TSS (mg/l) = 47,6 TSS (mg/l) = 27,0 FLOW(gpm)= - CAKE (CF/D) = - VSS (mg/l) = 35,805 VSS (mg/l) = 5,754 CAKE (CFM) = - TSS (lb/d) = 36,49 TSS (lb/d) = 8,736 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 240,024 VSS (lb/d) = 05,60 LB/CF PRIMARY SLUDGE FLOW (mgd) = 0.66 TRUCK LOADOUT TSS (mg/l) = 45,000 CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS 40 WET TONS/DAY VSS (mg/l) = 33,300 DIGESTER 0% 00% TSS (lb/d) = 247,327 CAKE THICKENESS 28% VSS (lb/d) = 83,022 WORKING VOLUME CUFT 2,620,32 (I,J,K as holders) COLIDS CAPTURE RATE 97% HRT 24.4 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 28,000 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 0.0 HRT (DAYS) 2.2 DAFT WAS INFLUENT (Need at least 8 days for Class B) SOLIDS (LB/D) = 76,284 PERCENT ACTIVE 40% FLOW (GPM) = 0 FLOW (mgd) = 2.53 CAKE WET TONS = 40 FINAL DILUTION 0.2% TSS (mg/l) = DIV/0! FLOW (GPM) = 759 THICKENED WAS CAKE (CF/D) = 2,79 POLYMER DENSITY 8.59 lb/g TSS (lb/d) = - TSS (mg/l) = 3,324 FLOW (mgd) = 0.4 CAKE (CFM) = 8.8 VSS (mg/l) = 2,753 FLOW (GPM) = 0 CAKE SPECIFIC WEIGHT 63 TSS (lb/d) = 70,227 TSS (mg/l) = 57,000 LB/CF VSS (lb/d) = 58,65 VSS (mg/l) = 47,20.6 MGD COMBINED SECONDARY SLUDGE TSS (lb/d) = 68,822 BELT PRESS WASH WATER FLOW (mgd) = 2.53 VSS (lb/d) = 57,002 BELT-PRESS DEWATERING TSS (mg/l) = 3,324 DAFT (WAS THICKENNING) VSS (mg/l) = 2,753 CAKE THICKENESS 22.0% TSS (lb/d) = 70,227 COLIDS CAPTURE RATE 97% VSS (lb/d) = 58,65 PRODUCT SOLIDS CONCENTRATION 5.7% WASH WATER.6 mgd COLIDS CAPTURE RATE 98.0% FILTRATE FLOW (mgd) = 0.7 DAFT UNDERFLOW FLOW (GPM) = 492 FLOW (mgd) = 2.39 TSS (mg/l) = 923 TOTAL RECYCLE FLOW FLOW (GPM) = 659 TSS (lb/d) = 5,452 FLOW (mgd) = 4.70 TSS (mg/l) = 7 FLOW (GPM) = 3262 VSS (mg/l) = 58 TOTAL WASTE FLOW TSS (mg/l) = 75 TSS (lb/d) =,405 FLOW (mgd) = 2.3 VSS (mg/l) = 23 VSS (lb/d) =,63 FLOW (GPM) = 603 TSS (lb/d) = 6,857 TSS (mg/l) = 283 VSS (lb/d) = 4,800 TSS (lb/d) = 5,452 VSS/TSS RATIO 70% 30 P age

82 OCSD Solids Loading Projection White Paper Plant - Liquid Process Mass Balance - Condition DAFT UNDERFLOW FLOW (mgd) = MGD PUMPED FROM P2 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! VSS (mg/l) = DIV/0! CENGEN COOLING WATER 2 MGD TSS (lb/d) = 0 VSS (lb/d) = 0 MF BACKWASH AS INFLUENT FLOW (mgd) = 56 BOD (mg/l) = 29 TSS (mg/l) = 74 COMBINED P SECONDARY EFFLUENT RAW INFLUENT PRIMARY INFLUENT VSS (mg/l) = 59 AS EFFLUENT AND PUMPED Flow (mgd) = 25 Flow (mgd) = 28 PRIMARY EFFLUENT SECONDARY INFLUENT BOD (lb/d) = 60,844 FLOW (mgd) = 55.8 P2 TF/SC EFFLUENT to OCWD MF INFLUENT MF BACKWASH MF EFFLUENT/RO INFLUENT BOD (mg/l) = 300 BOD (mg/l) = 297 Flow (mgd) = 27 Flow (mgd) = 44 TSS (lb/d) = 34,830 BOD (mg/l) = 4.5 FLOW (mgd) = 75 FLOW (mgd) = 70 FLOW (mgd) = 7 FLOW (mgd) = 53 TSS (mg/l) = 340 TSS (mg/l) = 336 BOD (mg/l) = 49 BOD (mg/l) = 34 VSS (lb/d) = 27,864 TSS (mg/l) = 4.0 BOD (mg/l) = 5.3 BOD (mg/l) = 5.3 BOD (mg/l) = 35 BOD (mg/l) = 2 BOD (lb/d) = 32,750 BOD (lb/d) = 37,72 TSS (mg/l) = 85 TSS (mg/l) = 77 VSS (mg/l) = 3.2 TSS (mg/l) = 5.3 TSS (mg/l) = 5.3 TSS (mg/l) = 35 TSS (mg/l) = 2 TSS (lb/d) = 354,450 TSS (lb/d) = 359,389 VSS (mg/l) = 68 VSS (mg/l) = 6 BOD (lb/d) = 2,096 BOD (lb/d) = 7,745 BOD (lb/d) = 7,524 BOD (lb/d) = 4,97 BOD (lb/d) = 2,552 VSS (lb/d) = 30,283 VSS (lb/d) = 305,48 BOD (lb/d) = 58,86 BOD (lb/d) = 6,43 ACTIVATED SLUDGE PLANT NO. (P-82) TSS (lb/d) =,863 TSS (lb/d) = 7,72 TSS (lb/d) = 7,49 TSS (lb/d) = 4,939 TSS (lb/d) = 2,552 VSS/TSS= 85% VSS/TSS= 85% TSS (lb/d) = 89,847 TSS (lb/d) = 92,399 VSS (lb/d) =,490 VSS (lb/d) = 7,878 VSS (lb/d) = VSS/TSS Ratio 80% OCWD GWRS RAW SEWAGE HEADWORKS & VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS GWRS PRODUCT WATER 30 MGD INFLUENT MICROFILTRATION REVERSE OSMOSIS INFLUENT PRIMARY CLARIFIERS PUMP STATION BOD Removal = 50% TSS Removal = 75% lbs TSS Yield / lb BOD Removed = 0.90 VSS/TSS Ratio 80% RO DISCHARGE TO OCEAN OUTFALL 23 MGD SOLIDS FROM CHEM FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) OCSD GREEN ACRES 5 MGD Dose (mg/l) = 20 TSS (lb/d) = 20,850 MISCELLANEOUS PROCESS WASH WATER FLOW POLYMER SOLIDS AS WAS PW PS 0.3 MGD FLOW (mgd) = 3.3 Dose (mg/l) = 0.2 FLOW (mgd) = MGD (BECOME WASHWATER) GAP WATER FROM OCWD BOD (mg/l) = - TSS (lb/d) = 209 TSS (mg/l) = 0,000 TSS (mg/l) = - VSS (mg/l) = 8,000 BOD (lb/d) = 0 TSS (lb/d) = 5,0 TSS (lb/d) = 0 VSS (lb/d) = 40,809 SECONDARY EFFLUENT TO OCEAN OUTFALL 0 MGD VSS (lb/d) = 0 Dry Solids.00% PRIMARY SLUDGE VSS/TSS Ratio 80% FLOW (mgd) = 0.85 AS2 INFLUENT 0 MGD RECYCLE FLOW TO P BOD (mg/l) = 22,43 FLOW (mgd) = 60 BELT PRESS WASHING WATER FLOW (mgd) = 0.00 TSS (mg/l) = 4,000 Dry Solids Conc.= 4.% BOD (mg/l) = 34 FLOW (GPM) = 0 VSS (mg/l) = 32,800 TSS (mg/l) = 77 AS2 EFFLUENT TSS (mg/l) = DIV/0! BOD (lb/d) = 58,86 VSS (mg/l) = 6 FLOW (mgd) = 59.4 VSS (mg/l) = DIV/0! TSS (lb/d) = 290,600 VSS/TSS Ratio= 80% BOD (lb/d) = 67,046 BOD (mg/l) = 4.0 TSS (lb/d) = - VSS (lb/d) = 232,480 TSS (lb/d) = 38,380 TSS (mg/l) = 4.0 VSS (lb/d) = - VSS (lb/d) = 30,704 VSS (mg/l) = 3.2 VSS/TSS RATIO 70% BOD (lb/d) =,982 ACTIVATED SLUDGE PLANT NO. 2 (P-02) TSS (lb/d) =,982 VSS (lb/d) =,585 VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS lbs TSS Yield / lb BOD Removed = 0.80 RETURN ACTIVATED SLUDGE (RAS) AS2 WAS FLOW (mgd) = 0.60 TSS (mg/l) = 0,000 VSS (mg/l) = 8,000 TSS (lb/d) = 50,070 VSS (lb/d) = 40,056 Dry Solids.00% VSS/TSS Ratio 80% TF EFFLUENT FLOW (mgd) = 30 BOD (mg/l) = 4.7 TSS (mg/l) = 5.5 TF INFLUENT VSS (mg/l) = % Note: GWRS only take TF EF up to 25% of toal SE FLOW (mgd) = 30 TRICKLING FILTER (P-76) BOD (lb/d) = 3, mgd (AS EF + AS2 EF + TF EF)*25% BOD (mg/l) = 34 TSS (lb/d) = 3,867 0 mgd If TF EF less than 25%, 0 mgd to ocean outfall TSS (mg/l) = 77 TRICKLING VSS (lb/d) = 3,094 VSS (mg/l) = 6 TRICKLING FILTER VSS/TSS Ratio 80% BOD (lb/d) = 33,523 FILTERS SECONDARY TSS (lb/d) = 9,90 CLARIFIERS VSS (lb/d) = 5,352 lbs TSS Yield / lb BOD Removed = 0.60 COMBINED WAS PRIMARY SLUDGE FLOW (mgd) =.2 FLOW (mgd) = 0.00 TSS (mg/l) = 0,000 BOD (mg/l) = 22,43 VSS (mg/l) = 8,000 TSS (mg/l) = 4,000 TSS (lb/d) = 0,08 TRICKLING FILTER SLUDGE VSS (mg/l) = 32,800 VSS (lb/d) = 80,865 FLOW (mgd) = 0.08 BOD (lb/d) = - TSS (mg/l) = 20,000 TSS (lb/d) = - VSS (mg/l) = 6,000 VSS (lb/d) = - TSS (lb/d) = 4,046 VSS (lb/d) =,237 Dry Solids 2.00% TO PLANT 2 VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 3 P age

83 OCSD Solids Loading Projection White Paper Plant - Solids Process Mass Balance Condition BLENDED CENTRIFUGE INFLUENT POLYMER FLOW THICKENED SLUDGE DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 2.5 ACTIVE (lb/d)= 2,536 FLOW (mgd) = 0.77 FLOW (mgd) = 0.77 FLOW (mgd) = 0.77 ACTIVE (lb/d)= 5,39 SOLIDS (LB/D) = 206,380 FLOW (GPM) = 490 ACTIVE (gpd)= FLOW (GPM) = 535 FLOW (GPM) = 535 FLOW (GPM) = 535 ACTIVE (gpd)= 69.2 CAKE WET TONS = 369 TSS (mg/l) = 22,669 FLOW(gpm)= 02.5 TSS (mg/l) = 60,000 TSS (mg/l) = 60,000 TSS (mg/l) = 33,20 FLOW(gpm)= 25.0 CAKE (CF/D) =,57 VSS (mg/l) = 8,35 VSS (mg/l) = 48,000 VSS (mg/l) = 48,000 VSS (mg/l) = 2,20 CAKE (CFM) = 8.0 TSS (lb/d) = 405,727 TSS (lb/d) = 385,44 TSS (lb/d) = 385,44 TSS (lb/d) = 22,763 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 324,582 VSS (lb/d) = 308,353 VSS (lb/d) = 308,353 VSS (lb/d) = 35,675 LB/CF PRIMARY SLUDGE VSS/TSS RATIO 80% FLOW (mgd) = 0.85 TSS (mg/l) = 4,000 CENTRIFUGE DIGESTER CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS TRUCK LOADOUT VSS (mg/l) = 32,800 00% 0% CO-THICKENNING CENTRIFUGE DIGESTER 00% 0% 369 WET TONS/DAY TSS (lb/d) = 290,600 CAKE THICKENESS 28% 0 CY/DAY VSS (lb/d) = 232,480 PRODUCT SOLIDS CONCENTRATION 6% WORKING VOLUME CUFT 2,577,540 COLIDS CAPTURE RATE 97% COLIDS CAPTURE RATE 95% CENTRATE INCLUDE POLYMER HRT 25.0 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 5,000 POLYMER DOSE 5 lb/dt FLOW (mgd) =.52 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 0.99 HRT (DAYS) 4.4 EMULSION POLYMER FLOW (GPM) = 058 SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 690 PERCENT ACTIVE 40% TSS (mg/l) =,597 (HRT need 6-7 days for at least sub-class B) CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 770 FINAL DILUTION 0.2% VSS (mg/l) =,277 CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 6,383 POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 20,286 CAKE (CFM) = - VSS (lb/d) = 6,229 CAKE SPECIFIC WEIGHT 63 VSS/TSS RATIO 80% LB/CF COMBINED WAS FLOW (mgd) =.2 DAFT WAS INFLUENT BELT PRESS WASH WATER 0 MGD BELT-PRESS DEWATERING TSS (mg/l) = 0,000 CENTRIFUGE DAFT FLOW (mgd) = 0.00 THICKENED WAS VSS (mg/l) = 8,000 00% 0% FLOW (GPM) = 0 FLOW (mgd) = 0.00 TSS (lb/d) = 0,08 TSS (mg/l) = DIV/0! FLOW (GPM) = 0 CAKE THICKENESS 20.0% VSS (lb/d) = 80,865 VSS (mg/l) = DIV/0! TSS (mg/l) = 46,000 COLIDS CAPTURE RATE 97% TSS (lb/d) = - VSS (mg/l) = 36,800 WSAH WATER.6 MGD VSS (lb/d) = - TSS (lb/d) = - FILTRATE VSS (lb/d) = - FLOW (mgd) = 0.00 VSS/TSS RATIO 80% FLOW (GPM) = 0 DAFT (WAS THICKENNING) TSS (mg/l) = DIV/0! TSS (lb/d) = - TRICKLING FILTER SLUDGE PRODUCT SOLIDS CONCENTRATION 4.6% FLOW (mgd) = 0.08 COLIDS CAPTURE RATE 99.5% TSS (mg/l) = 20,000 CENTRIFUGE DIGESTER VSS (mg/l) = 6,000 00% 0% TSS (lb/d) = 4,046 TOTAL WASTE FLOW VSS (lb/d) =,237 DAFT UNDERFLOW FLOW (mgd) = 0.0 FLOW (mgd) = 0.00 FLOW (GPM) = 0 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW RECYCLE FLOW TO P TSS (mg/l) = DIV/0! TSS (lb/d) = - FLOW (mgd) = 2.5 FLOW (mgd) = 0.00 VSS (mg/l) = DIV/0! FLOW (GPM) = 748 FLOW (GPM) = 0 TSS (lb/d) = - TSS (mg/l) =,270 TSS (mg/l) = DIV/0! VSS (lb/d) = - VSS (mg/l) = 889 VSS (mg/l) = DIV/0! VSS/TSS RATIO 80% TSS (lb/d) = 26,669 TSS (lb/d) = - VSS (lb/d) = 8,668 VSS (lb/d) = - VSS/TSS RATIO 70% VSS/TSS RATIO 70% P P2 DAFT Underflow 0% 00% TO AS INFLUENT RECYCLE FLOW TO P2 FLOW (mgd) = 2.5 FLOW (GPM) = 748 TSS (mg/l) =,270 VSS (mg/l) = 889 TSS (lb/d) = 26,669 VSS (lb/d) = 8,668 VSS/TSS RATIO 70% 32 P age

84 OCSD Solids Loading Projection White Paper Plant 2 - Liquid Process Mass Balance - Condition RAW INFLUENT PRIMARY INFLUENT Flow (mgd) = 75 Flow (mgd) = 87 PRIMARY EFFLUENT AS PLANT INFLUENT AS EFFLUENT BOD (mg/l) = 300 BOD (mg/l) = 259 Flow (mgd) = 86 FLOW (mgd) = 35.0 FLOW (mgd) = 33.9 TSS (mg/l) = 340 TSS (mg/l) = 338 BOD (mg/l) = 04 BOD (mg/l) = 04 BOD (mg/l) = 4.0 BOD (lb/d) = 87,650 BOD (lb/d) = 87,650 TSS (mg/l) = 85 TSS (mg/l) = 85 TSS (mg/l) = MGD GAP WATER FROM OCWD TSS (lb/d) = 22,670 TSS (lb/d) = 245,02 BOD (lb/d) = 75,060 BOD (lb/d) = 30,400 BOD (lb/d) =,29 P OUTFALL EFFLUENT VSS (lb/d) = 80,770 VSS (lb/d) = 203,409 TSS (lb/d) = 6,253 TSS (lb/d) = 24,808 PURE OXYGEN ACTIVATED SLUDGE PLANT TSS (lb/d) =,553 5 MG 23 MG VSS/TSS= 85% PW RAW SEW RAW SEWAGE HEADWORKS & INFLUENT AERATION BASINS SECONDARY CLARIFIERS TOTAL OCEAN OUTFALL 67 MG PUMP STATION INFLUENT INFLUENT PRIMARY CLARIFIERS BOD Removal = 60% TSS & VSS Removal = 75% lbs TSS Yield / lb BOD Removed =.0 COMBINED P2 SECONDARY EFFLUENT FLOW (mgd) = 0.00 P RECYCLE FLOW TO P2 SOLIDS FROM CHEM FLOW (mgd) = 49 BOD (mg/l) = 22,43 FLOW (mgd) = 2.52 FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) BOD (mg/l) = 8.4 TSS (mg/l) = 4,000 FLOW (GPM) = 748 Dose (mg/l) = 8 TSS (mg/l) = 3.5 VSS (mg/l) = 32,800 TSS (mg/l) = 270 TSS (lb/d) =,259 BOD (lb/d) = 3,437 BOD (lb/d) = - VSS (mg/l) = 889 POLYMER SOLIDS AS WAS TSS (lb/d) = 5,540 TSS (lb/d) = - TSS (lb/d) = Dose (mg/l) = 0.2 FLOW (mgd) =.5 VSS (lb/d) = - VSS (lb/d) = 8668 TSS (lb/d) = 25 TSS (mg/l) = 3,200 VSS (mg/l) = 2,720 TF/SC EFFLUENT TO OUTFALL P RECYCLE FLOW TO P2 TSS (lb/d) = 30,645 FLOW (mgd) = 5.5 VSS (lb/d) = 26,049 BOD (mg/l) = 5.5 Dry Solids 0.32% TSS (mg/l) = 9.5 PRIMARY SLUDGE VSS/TSS Ratio 85% BOD (lb/d) = 70 P2 RECYCLE FLOW PLUS PW/GAP WASHWATER FLOW (mgd) = 0.52 TSS (lb/d) =,226 P PRIMARY SLUDGE DIVERSION FLOW (mgd) = 9.42 BOD (mg/l) = 25,963 FLOW (GPM) = 654 TSS (mg/l) = 45,000 Dry Solids Conc.= 4.5% TSS (mg/l) = 72 VSS (mg/l) = 33,300 VSS/TSS Ratio= 74% VSS (mg/l) = 5 BOD (lb/d) = 2,590 TF/SC EFFLUENT TSS (lb/d) = 5673 TSS (lb/d) = 95,43 FLOW (mgd) = 50.3 VSS (lb/d) = 397 VSS (lb/d) = 44,406 BOD (mg/l) = 5.5 TSS (mg/l) = 9.5 BOD (lb/d) = 2,308 TRICKLING FILTER (P2-90) TSS (lb/d) = 3,987 TF/SC INFLUENT FLOW (mgd) = 5 TRICKLING TRICKLING BOD (mg/l) = 04 FILTERS FILTER 35 MGD PUMPED TO GWRS TSS (mg/l) = 85 /SOLIDS SECONDARY BOD (lb/d) = 44,660 CONTACT CLARIFIERS TSS (lb/d) = 36,445 lbs TSS Yield / lb BOD Removed = 0.85 COMBINED SECONDARY SLUDGE FLOW (mgd) = 2.24 TSS (mg/l) = 3,347 VSS (mg/l) = 2,759 TSS (lb/d) = 62,657 TF/SC WSS VSS (lb/d) = 5,658 FLOW (mgd) =.0 TSS (mg/l) = 3,500 VSS (mg/l) = 2,800 TSS (lb/d) = 32,02 VSS (lb/d) = 25,60 Dry Solids 0.35% VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 33 P age

85 OCSD Solids Loading Projection White Paper Plant 2 - Solids Process Mass Balance Condition DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 0.65 FLOW (mgd) = 0.65 ACTIVE (lb/d)= 3,683 SOLIDS (LB/D) = 42,90 FLOW (GPM) = 45 FLOW (GPM) = 45 ACTIVE (gpd)= CAKE WET TONS = 255 TSS (mg/l) = 47,388 TSS (mg/l) = 27,24 FLOW(gpm)= 48.9 CAKE (CF/D) = 7,975 VSS (mg/l) = 36,025 VSS (mg/l) = 5,85 CAKE (CFM) = 5.5 TSS (lb/d) = 256,547 TSS (lb/d) = 47,330 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 95,03 VSS (lb/d) = 85,84 LB/CF PRIMARY SLUDGE FLOW (mgd) = 0.52 TRUCK LOADOUT TSS (mg/l) = 45,000 CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS 255 WET TONS/DAY VSS (mg/l) = 33,300 DIGESTER 00% 0% TSS (lb/d) = 95,43 CAKE THICKENESS 28% VSS (lb/d) = 44,406 WORKING VOLUME CUFT 2,620,32 (I,J,K as holders) COLIDS CAPTURE RATE 97% HRT 30.2 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 28,000 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 0.8 HRT (DAYS) 3.5 DAFT WAS INFLUENT (Need at least 8 days for Class B) SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 558 FLOW (mgd) = 2.24 CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 659 FLOW (GPM) = 559 THICKENED WAS CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 4,420 TSS (mg/l) = 3,347 FLOW (mgd) = 0.3 CAKE (CFM) = - VSS (mg/l) = 2,759 FLOW (GPM) = 90 CAKE SPECIFIC WEIGHT 63 TSS (lb/d) = 62,657 TSS (mg/l) = 57,000 LB/CF VSS (lb/d) = 5,658 VSS (mg/l) = 46, MGD COMBINED SECONDARY SLUDGE TSS (lb/d) = 6,404 BELT PRESS WASH WATER FLOW (mgd) = 2.24 VSS (lb/d) = 50,625 BELT-PRESS DEWATERING TSS (mg/l) = 3,347 DAFT (WAS THICKENNING) VSS (mg/l) = 2,759 CAKE THICKENESS 22.0% TSS (lb/d) = 62,657 COLIDS CAPTURE RATE 97% VSS (lb/d) = 5,658 PRODUCT SOLIDS CONCENTRATION 5.7% WASH WATER.6 mgd COLIDS CAPTURE RATE 98.0% FILTRATE FLOW (mgd) = 0.00 DAFT UNDERFLOW FLOW (GPM) = 0 FLOW (mgd) = 2.2 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW FLOW (GPM) = 469 TSS (lb/d) = - FLOW (mgd) = 2.92 TSS (mg/l) = 7 FLOW (GPM) = 2028 VSS (mg/l) = 59 TOTAL WASTE FLOW TSS (mg/l) = 233 TSS (lb/d) =,253 FLOW (mgd) = 0.0 VSS (mg/l) = 63 VSS (lb/d) =,033 FLOW (GPM) = 0 TSS (lb/d) = 5,673 TSS (mg/l) = DIV/0! VSS (lb/d) = 3,97 TSS (lb/d) = - VSS/TSS RATIO 70% 34 P age

86 OCSD Solids Loading Projection White Paper Plant - Liquid Process Mass Balance - Condition 2 DAFT UNDERFLOW FLOW (mgd) = MGD PUMPED FROM P2 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! VSS (mg/l) = DIV/0! CENGEN COOLING WATER 2 MGD TSS (lb/d) = 0 VSS (lb/d) = 0 MF BACKWASH AS INFLUENT FLOW (mgd) = 32 BOD (mg/l) = 22 TSS (mg/l) = 70 COMBINED P SECONDARY EFFLUENT RAW INFLUENT PRIMARY INFLUENT VSS (mg/l) = 56 AS EFFLUENT AND PUMPED Flow (mgd) = 00 Flow (mgd) = 03 PRIMARY EFFLUENT SECONDARY INFLUENT BOD (lb/d) = 32,3 FLOW (mgd) = 3.3 P2 TF/SC EFFLUENT to OCWD MF INFLUENT MF BACKWASH MF EFFLUENT/RO INFLUENT BOD (mg/l) = 300 BOD (mg/l) = 295 Flow (mgd) = 03 Flow (mgd) = 20 TSS (lb/d) = 8,442 BOD (mg/l) = 4.5 FLOW (mgd) = 75 FLOW (mgd) = 70 FLOW (mgd) = 7 FLOW (mgd) = 53 TSS (mg/l) = 340 TSS (mg/l) = 334 BOD (mg/l) = 49 BOD (mg/l) = 30 VSS (lb/d) = 4,754 TSS (mg/l) = 4.0 BOD (mg/l) = 4.7 BOD (mg/l) = 4.7 BOD (mg/l) = 29 BOD (mg/l) = 2 BOD (lb/d) = 250,200 BOD (lb/d) = 254,278 TSS (mg/l) = 84 TSS (mg/l) = 75 VSS (mg/l) = 3.2 TSS (mg/l) = 4.7 TSS (mg/l) = 4.7 TSS (mg/l) = 29 TSS (mg/l) = 2 TSS (lb/d) = 283,560 TSS (lb/d) = 287,705 VSS (mg/l) = 67 VSS (mg/l) = 60 BOD (lb/d) =,75 BOD (lb/d) = 6,825 BOD (lb/d) = 6,630 BOD (lb/d) = 4,078 BOD (lb/d) = 2,552 VSS (lb/d) = 24,026 VSS (lb/d) = 244,549 BOD (lb/d) = 27,39 BOD (lb/d) = 29,69 ACTIVATED SLUDGE PLANT NO. (P-82) TSS (lb/d) =,044 TSS (lb/d) = 6,894 TSS (lb/d) = 6,697 TSS (lb/d) = 4,45 TSS (lb/d) = 2,552 VSS/TSS= 85% VSS/TSS= 85% TSS (lb/d) = 7,926 TSS (lb/d) = 74,478 VSS (lb/d) = 835 VSS (lb/d) = 57,54 VSS (lb/d) = VSS/TSS Ratio 80% OCWD GWRS RAW SEWAGE HEADWORKS & VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS GWRS PRODUCT WATER 30 MGD INFLUENT MICROFILTRATION REVERSE OSMOSIS INFLUENT PRIMARY CLARIFIERS PUMP STATION BOD Removal = 50% TSS Removal = 75% lbs TSS Yield / lb BOD Removed = 0.90 VSS/TSS Ratio 80% RO DISCHARGE TO OCEAN OUTFALL 23 MGD SOLIDS FROM CHEM FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) OCSD GREEN ACRES 5 MGD Dose (mg/l) = 20 TSS (lb/d) = 6,680 MISCELLANEOUS PROCESS WASH WATER FLOW POLYMER SOLIDS AS WAS PW PS 0.3 MGD FLOW (mgd) = 3.3 Dose (mg/l) = 0.2 FLOW (mgd) = MGD (BECOME WASHWATER) GAP WATER FROM OCWD BOD (mg/l) = - TSS (lb/d) = 67 TSS (mg/l) = 0,000 TSS (mg/l) = - VSS (mg/l) = 8,000 BOD (lb/d) = 0 TSS (lb/d) = 26,80 TSS (lb/d) = 0 VSS (lb/d) = 2,44 SECONDARY EFFLUENT TO OCEAN OUTFALL 0 MGD VSS (lb/d) = 0 Dry Solids.00% PRIMARY SLUDGE VSS/TSS Ratio 80% FLOW (mgd) = 0.68 AS2 INFLUENT 0 MGD RECYCLE FLOW TO P BOD (mg/l) = 22,408 FLOW (mgd) = 60 BELT PRESS WASHING WATER FLOW (mgd) = 0.00 TSS (mg/l) = 4,000 Dry Solids Conc.= 4.% BOD (mg/l) = 30 FLOW (GPM) = 0 VSS (mg/l) = 32,800 TSS (mg/l) = 75 AS2 EFFLUENT TSS (mg/l) = DIV/0! BOD (lb/d) = 27,39 VSS (mg/l) = 60 FLOW (mgd) = 59.4 VSS (mg/l) = DIV/0! TSS (lb/d) = 232,626 VSS/TSS Ratio= 80% BOD (lb/d) = 65,052 BOD (mg/l) = 4.0 TSS (lb/d) = - VSS (lb/d) = 86,00 TSS (lb/d) = 37,358 TSS (mg/l) = 4.0 VSS (lb/d) = - VSS (lb/d) = 29,886 VSS (mg/l) = 3.2 VSS/TSS RATIO 70% BOD (lb/d) =,982 ACTIVATED SLUDGE PLANT NO. 2 (P-02) TSS (lb/d) =,982 VSS (lb/d) =,586 VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS lbs TSS Yield / lb BOD Removed = 0.80 RETURN ACTIVATED SLUDGE (RAS) AS2 WAS FLOW (mgd) = 0.58 TSS (mg/l) = 0,000 VSS (mg/l) = 8,000 TSS (lb/d) = 48,473 VSS (lb/d) = 38,779 Dry Solids.00% VSS/TSS Ratio 80% TF EFFLUENT FLOW (mgd) = 30 BOD (mg/l) = 4.7 TSS (mg/l) = 5.5 TF INFLUENT VSS (mg/l) = % Note: GWRS only take TF EF up to 25% of toal SE FLOW (mgd) = 30 TRICKLING FILTER (P-76) BOD (lb/d) = 3, mgd (AS EF + AS2 EF + TF EF)*25% BOD (mg/l) = 30 TSS (lb/d) = 3,868 0 mgd If TF EF less than 25%, 0 mgd to ocean outfall TSS (mg/l) = 75 TRICKLING VSS (lb/d) = 3,094 VSS (mg/l) = 60 TRICKLING FILTER VSS/TSS Ratio 80% BOD (lb/d) = 32,526 FILTERS SECONDARY TSS (lb/d) = 8,679 CLARIFIERS VSS (lb/d) = 4,943 lbs TSS Yield / lb BOD Removed = 0.60 COMBINED WAS PRIMARY SLUDGE FLOW (mgd) = 0.90 FLOW (mgd) = 0.00 TSS (mg/l) = 0,000 BOD (mg/l) = 22,408 VSS (mg/l) = 8,000 TSS (mg/l) = 4,000 TSS (lb/d) = 75,274 TRICKLING FILTER SLUDGE VSS (mg/l) = 32,800 VSS (lb/d) = 60,29 FLOW (mgd) = 0.08 BOD (lb/d) = - TSS (mg/l) = 20,000 TSS (lb/d) = - VSS (mg/l) = 6,000 VSS (lb/d) = - TSS (lb/d) = 3,447 VSS (lb/d) = 0,758 Dry Solids 2.00% TO PLANT 2 VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 35 P age

87 OCSD Solids Loading Projection White Paper Plant - Solids Process Mass Balance Condition 2 BLENDED CENTRIFUGE INFLUENT POLYMER FLOW THICKENED SLUDGE DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) =.66 ACTIVE (lb/d)= 2,008 FLOW (mgd) = 0.6 FLOW (mgd) = 0.6 FLOW (mgd) = 0.6 ACTIVE (lb/d)= 4,23 SOLIDS (LB/D) = 63,459 FLOW (GPM) = 55 ACTIVE (gpd)= FLOW (GPM) = 424 FLOW (GPM) = 424 FLOW (GPM) = 424 ACTIVE (gpd)= CAKE WET TONS = 292 TSS (mg/l) = 23,63 FLOW(gpm)= 8.2 TSS (mg/l) = 60,000 TSS (mg/l) = 60,000 TSS (mg/l) = 33,20 FLOW(gpm)= 70.3 CAKE (CF/D) = 9,22 VSS (mg/l) = 8,530 VSS (mg/l) = 48,000 VSS (mg/l) = 48,000 VSS (mg/l) = 2,20 CAKE (CFM) = 6.3 TSS (lb/d) = 32,347 TSS (lb/d) = 305,279 TSS (lb/d) = 305,279 TSS (lb/d) = 68,54 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 257,077 VSS (lb/d) = 244,224 VSS (lb/d) = 244,224 VSS (lb/d) = 07,458 LB/CF PRIMARY SLUDGE VSS/TSS RATIO 80% FLOW (mgd) = 0.68 TSS (mg/l) = 4,000 CENTRIFUGE DIGESTER CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS TRUCK LOADOUT VSS (mg/l) = 32,800 00% 0% CO-THICKENNING CENTRIFUGE DIGESTER 00% 0% 292 WET TONS/DAY TSS (lb/d) = 232,626 CAKE THICKENESS 28% 0 CY/DAY VSS (lb/d) = 86,00 PRODUCT SOLIDS CONCENTRATION 6% WORKING VOLUME CUFT 2,577,540 COLIDS CAPTURE RATE 97% COLIDS CAPTURE RATE 95% CENTRATE INCLUDE POLYMER HRT 3.6 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 5,000 POLYMER DOSE 5 lb/dt FLOW (mgd) =.7 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 0.79 HRT (DAYS) 5.6 EMULSION POLYMER FLOW (GPM) = 83 SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 547 PERCENT ACTIVE 40% TSS (mg/l) =,646 (HRT need 6-7 days for at least sub-class B) CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 770 FINAL DILUTION 0.2% VSS (mg/l) =,37 CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 5,055 POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 6,067 CAKE (CFM) = - VSS (lb/d) = 2,854 CAKE SPECIFIC WEIGHT 63 VSS/TSS RATIO 80% LB/CF COMBINED WAS FLOW (mgd) = 0.90 DAFT WAS INFLUENT BELT PRESS WASH WATER 0 MGD BELT-PRESS DEWATERING TSS (mg/l) = 0,000 CENTRIFUGE DAFT FLOW (mgd) = 0.00 THICKENED WAS VSS (mg/l) = 8,000 00% 0% FLOW (GPM) = 0 FLOW (mgd) = 0.00 TSS (lb/d) = 75,274 TSS (mg/l) = DIV/0! FLOW (GPM) = 0 CAKE THICKENESS 20.0% VSS (lb/d) = 60,29 VSS (mg/l) = DIV/0! TSS (mg/l) = 46,000 COLIDS CAPTURE RATE 97% TSS (lb/d) = - VSS (mg/l) = 36,800 WSAH WATER.6 MGD VSS (lb/d) = - TSS (lb/d) = - FILTRATE VSS (lb/d) = - FLOW (mgd) = 0.00 VSS/TSS RATIO 80% FLOW (GPM) = 0 DAFT (WAS THICKENNING) TSS (mg/l) = DIV/0! TSS (lb/d) = - TRICKLING FILTER SLUDGE PRODUCT SOLIDS CONCENTRATION 4.6% FLOW (mgd) = 0.08 COLIDS CAPTURE RATE 99.5% TSS (mg/l) = 20,000 CENTRIFUGE DIGESTER VSS (mg/l) = 6,000 00% 0% TSS (lb/d) = 3,447 TOTAL WASTE FLOW VSS (lb/d) = 0,758 DAFT UNDERFLOW FLOW (mgd) = 0.0 FLOW (mgd) = 0.00 FLOW (GPM) = 0 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW RECYCLE FLOW TO P TSS (mg/l) = DIV/0! TSS (lb/d) = - FLOW (mgd) = 2.0 FLOW (mgd) = 0.00 VSS (mg/l) = DIV/0! FLOW (GPM) = 359 FLOW (GPM) = 0 TSS (lb/d) = - TSS (mg/l) =,294 TSS (mg/l) = DIV/0! VSS (lb/d) = - VSS (mg/l) = 906 VSS (mg/l) = DIV/0! VSS/TSS RATIO 80% TSS (lb/d) = 2,23 TSS (lb/d) = - VSS (lb/d) = 4,786 VSS (lb/d) = - VSS/TSS RATIO 70% VSS/TSS RATIO 70% P P2 DAFT Underflow 0% 00% TO AS INFLUENT RECYCLE FLOW TO P2 FLOW (mgd) = 2.0 FLOW (GPM) = 359 TSS (mg/l) =,294 VSS (mg/l) = 906 TSS (lb/d) = 2,23 VSS (lb/d) = 4,786 VSS/TSS RATIO 70% 36 P age

88 OCSD Solids Loading Projection White Paper Plant 2 - Liquid Process Mass Balance - Condition 2 RAW INFLUENT PRIMARY INFLUENT Flow (mgd) = 00 Flow (mgd) = 2 PRIMARY EFFLUENT AS PLANT INFLUENT AS EFFLUENT BOD (mg/l) = 300 BOD (mg/l) = 267 Flow (mgd) = 2 FLOW (mgd) = 52 FLOW (mgd) = 50.0 TSS (mg/l) = 340 TSS (mg/l) = 333 BOD (mg/l) = 07 BOD (mg/l) = 07 BOD (mg/l) = 4.0 BOD (lb/d) = 250,200 BOD (lb/d) = 250,200 TSS (mg/l) = 84 TSS (mg/l) = 84 TSS (mg/l) = MGD GAP WATER FROM OCWD TSS (lb/d) = 283,560 TSS (lb/d) = 32,24 BOD (lb/d) = 00,080 BOD (lb/d) = 46,34 BOD (lb/d) =,668 P OUTFALL EFFLUENT VSS (lb/d) = 24,026 VSS (lb/d) = 26,02 TSS (lb/d) = 78,03 TSS (lb/d) = 36,32 PURE OXYGEN ACTIVATED SLUDGE PLANT TSS (lb/d) = 2,293 5 MG 23 MG VSS/TSS= 85% PW RAW SEW RAW SEWAGE HEADWORKS & INFLUENT AERATION BASINS SECONDARY CLARIFIERS TOTAL OCEAN OUTFALL 67 MG PUMP STATION INFLUENT INFLUENT PRIMARY CLARIFIERS BOD Removal = 60% TSS & VSS Removal = 75% lbs TSS Yield / lb BOD Removed =.0 COMBINED P2 SECONDARY EFFLUENT FLOW (mgd) = 0.00 P RECYCLE FLOW TO P2 SOLIDS FROM CHEM FLOW (mgd) = 49 BOD (mg/l) = 22,408 FLOW (mgd) =.96 FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) BOD (mg/l) = 0.6 TSS (mg/l) = 4,000 FLOW (GPM) = 359 Dose (mg/l) = 8 TSS (mg/l) = 6.9 VSS (mg/l) = 32,800 TSS (mg/l) = 294 TSS (lb/d) = 5,02 BOD (lb/d) = 4,359 BOD (lb/d) = - VSS (mg/l) = 906 POLYMER SOLIDS AS WAS TSS (lb/d) = 6,94 TSS (lb/d) = - TSS (lb/d) = 223 Dose (mg/l) = 0.2 FLOW (mgd) =.76 VSS (lb/d) = - VSS (lb/d) = 4786 TSS (lb/d) = 67 TSS (mg/l) = 3,200 VSS (mg/l) = 2,720 TF/SC EFFLUENT TO OUTFALL P RECYCLE FLOW TO P2 TSS (lb/d) = 46,848 FLOW (mgd) = -0.7 VSS (lb/d) = 39,82 BOD (mg/l) = 5.5 Dry Solids 0.32% TSS (mg/l) = 9.5 PRIMARY SLUDGE VSS/TSS Ratio 85% BOD (lb/d) = (32) P2 RECYCLE FLOW PLUS PW/GAP WASHWATER FLOW (mgd) = 0.66 TSS (lb/d) = (55) P PRIMARY SLUDGE DIVERSION FLOW (mgd) = 0.45 BOD (mg/l) = 27,0 FLOW (GPM) = 7255 TSS (mg/l) = 45,000 Dry Solids Conc.= 4.5% TSS (mg/l) = 85 VSS (mg/l) = 33,300 VSS/TSS Ratio= 74% VSS (mg/l) = 60 BOD (lb/d) = 50,20 TF/SC EFFLUENT TSS (lb/d) = 744 TSS (lb/d) = 249,272 FLOW (mgd) = 58.7 VSS (lb/d) = 5209 VSS (lb/d) = 84,46 BOD (mg/l) = 5.5 TSS (mg/l) = 9.5 BOD (lb/d) = 2,69 TRICKLING FILTER (P2-90) TSS (lb/d) = 4,649 TF/SC INFLUENT FLOW (mgd) = 60 TRICKLING TRICKLING BOD (mg/l) = 07 FILTERS FILTER 59 MGD PUMPED TO GWRS TSS (mg/l) = 84 /SOLIDS SECONDARY BOD (lb/d) = 53,739 CONTACT CLARIFIERS TSS (lb/d) = 4,899 lbs TSS Yield / lb BOD Removed = 0.85 COMBINED SECONDARY SLUDGE FLOW (mgd) = 3.08 TSS (mg/l) = 3,329 VSS (mg/l) = 2,754 TSS (lb/d) = 85,590 TF/SC WSS VSS (lb/d) = 70,84 FLOW (mgd) =.33 TSS (mg/l) = 3,500 VSS (mg/l) = 2,800 TSS (lb/d) = 38,742 VSS (lb/d) = 30,993 Dry Solids 0.35% VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 37 P age

89 OCSD Solids Loading Projection White Paper Plant 2 - Solids Process Mass Balance Condition 2 DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 0.84 FLOW (mgd) = 0.84 ACTIVE (lb/d)= 4,775 SOLIDS (LB/D) = 85,259 FLOW (GPM) = 584 FLOW (GPM) = 584 ACTIVE (gpd)= CAKE WET TONS = 33 TSS (mg/l) = 47,59 TSS (mg/l) = 27,242 FLOW(gpm)= 93.0 CAKE (CF/D) = 0,338 VSS (mg/l) = 36,209 VSS (mg/l) = 5,932 CAKE (CFM) = 7.2 TSS (lb/d) = 333,50 TSS (lb/d) = 90,989 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 253,859 VSS (lb/d) =,698 LB/CF PRIMARY SLUDGE FLOW (mgd) = 0.66 TRUCK LOADOUT TSS (mg/l) = 45,000 CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS 33 WET TONS/DAY VSS (mg/l) = 33,300 DIGESTER 00% 0% TSS (lb/d) = 249,272 CAKE THICKENESS 28% VSS (lb/d) = 84,46 WORKING VOLUME CUFT 2,620,32 (I,J,K as holders) COLIDS CAPTURE RATE 97% HRT 23.3 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 28,000 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) =.0 HRT (DAYS) 2.7 DAFT WAS INFLUENT (Need at least 8 days for Class B) SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 723 FLOW (mgd) = 3.08 CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 660 FLOW (GPM) = 24 THICKENED WAS CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 5,730 TSS (mg/l) = 3,329 FLOW (mgd) = 0.8 CAKE (CFM) = - VSS (mg/l) = 2,754 FLOW (GPM) = 23 CAKE SPECIFIC WEIGHT 63 TSS (lb/d) = 85,590 TSS (mg/l) = 57,000 LB/CF VSS (lb/d) = 70,84 VSS (mg/l) = 47, MGD COMBINED SECONDARY SLUDGE TSS (lb/d) = 83,878 BELT PRESS WASH WATER FLOW (mgd) = 3.08 VSS (lb/d) = 69,398 BELT-PRESS DEWATERING TSS (mg/l) = 3,329 DAFT (WAS THICKENNING) VSS (mg/l) = 2,754 CAKE THICKENESS 22.0% TSS (lb/d) = 85,590 COLIDS CAPTURE RATE 97% VSS (lb/d) = 70,84 PRODUCT SOLIDS CONCENTRATION 5.7% WASH WATER.6 mgd COLIDS CAPTURE RATE 98.0% FILTRATE FLOW (mgd) = 0.00 DAFT UNDERFLOW FLOW (GPM) = 0 FLOW (mgd) = 2.9 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW FLOW (GPM) = 208 TSS (lb/d) = - FLOW (mgd) = 3.95 TSS (mg/l) = 7 FLOW (GPM) = 274 VSS (mg/l) = 58 TOTAL WASTE FLOW TSS (mg/l) = 226 TSS (lb/d) =,72 FLOW (mgd) = 0.0 VSS (mg/l) = 58 VSS (lb/d) =,46 FLOW (GPM) = 0 TSS (lb/d) = 7,44 TSS (mg/l) = DIV/0! VSS (lb/d) = 5,209 TSS (lb/d) = - VSS/TSS RATIO 70% 38 P age

90 OCSD Solids Loading Projection White Paper Plant - Liquid Process Mass Balance - Condition 3 DAFT UNDERFLOW FLOW (mgd) = MGD PUMPED FROM P2 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! VSS (mg/l) = DIV/0! CENGEN COOLING WATER 2 MGD TSS (lb/d) = 0 VSS (lb/d) = 0 MF BACKWASH AS INFLUENT FLOW (mgd) = 8 BOD (mg/l) = 2 TSS (mg/l) = 6 COMBINED P SECONDARY EFFLUENT RAW INFLUENT PRIMARY INFLUENT VSS (mg/l) = 49 AS EFFLUENT AND PUMPED Flow (mgd) = 50 Flow (mgd) = 53 PRIMARY EFFLUENT SECONDARY INFLUENT BOD (lb/d) = 75,907 FLOW (mgd) = 80.7 P2 TF/SC EFFLUENT to OCWD MF INFLUENT MF BACKWASH MF EFFLUENT/RO INFLUENT BOD (mg/l) = 250 BOD (mg/l) = 249 Flow (mgd) = 52 Flow (mgd) = 69 TSS (lb/d) = 4,469 BOD (mg/l) = 4.5 FLOW (mgd) = 75 FLOW (mgd) = 70 FLOW (mgd) = 7 FLOW (mgd) = 53 TSS (mg/l) = 270 TSS (mg/l) = 269 BOD (mg/l) = 25 BOD (mg/l) = 5 VSS (lb/d) = 33,76 TSS (mg/l) = 4.0 BOD (mg/l) = 5.9 BOD (mg/l) = 5.9 BOD (mg/l) = 4 BOD (mg/l) = 2 BOD (lb/d) = 32,750 BOD (lb/d) = 38,634 TSS (mg/l) = 68 TSS (mg/l) = 63 VSS (mg/l) = 3.2 TSS (mg/l) = 5.9 TSS (mg/l) = 5.9 TSS (mg/l) = 4 TSS (mg/l) = 2 TSS (lb/d) = 337,770 TSS (lb/d) = 343,52 VSS (mg/l) = 54 VSS (mg/l) = 50 BOD (lb/d) = 3,029 BOD (lb/d) = 8,684 BOD (lb/d) = 8,436 BOD (lb/d) = 5,884 BOD (lb/d) = 2,552 VSS (lb/d) = 287,05 VSS (lb/d) = 29,993 BOD (lb/d) = 59,37 BOD (lb/d) = 6,869 ACTIVATED SLUDGE PLANT NO. (P-82) TSS (lb/d) = 2,693 TSS (lb/d) = 8,547 TSS (lb/d) = 8,303 TSS (lb/d) = 5,75 TSS (lb/d) = 2,552 VSS/TSS= 85% VSS/TSS= 85% TSS (lb/d) = 85,880 TSS (lb/d) = 88,432 VSS (lb/d) = 2,54 VSS (lb/d) = 68,704 VSS (lb/d) = VSS/TSS Ratio 80% OCWD GWRS RAW SEWAGE HEADWORKS & VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS GWRS PRODUCT WATER 30 MGD INFLUENT MICROFILTRATION REVERSE OSMOSIS INFLUENT PRIMARY CLARIFIERS PUMP STATION BOD Removal = 50% TSS Removal = 75% lbs TSS Yield / lb BOD Removed = 0.90 VSS/TSS Ratio 80% RO DISCHARGE TO OCEAN OUTFALL 23 MGD SOLIDS FROM CHEM FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) OCSD GREEN ACRES 5 MGD Dose (mg/l) = 20 TSS (lb/d) = 25,020 MISCELLANEOUS PROCESS WASH WATER FLOW POLYMER SOLIDS AS WAS PW PS 0.3 MGD FLOW (mgd) = 3.3 Dose (mg/l) = 0.2 FLOW (mgd) = MGD (BECOME WASHWATER) GAP WATER FROM OCWD BOD (mg/l) = - TSS (lb/d) = 250 TSS (mg/l) = 0,000 TSS (mg/l) = - VSS (mg/l) = 8,000 BOD (lb/d) = 0 TSS (lb/d) = 62,897 TSS (lb/d) = 0 VSS (lb/d) = 50,38 SECONDARY EFFLUENT TO OCEAN OUTFALL 0 MGD VSS (lb/d) = 0 Dry Solids.00% PRIMARY SLUDGE VSS/TSS Ratio 80% FLOW (mgd) = 0.83 AS2 INFLUENT 0 MGD RECYCLE FLOW TO P BOD (mg/l) = 23,089 FLOW (mgd) = 60 BELT PRESS WASHING WATER FLOW (mgd) = 0.00 TSS (mg/l) = 4,000 Dry Solids Conc.= 4.% BOD (mg/l) = 5 FLOW (GPM) = 0 VSS (mg/l) = 32,800 TSS (mg/l) = 63 AS2 EFFLUENT TSS (mg/l) = DIV/0! BOD (lb/d) = 59,37 VSS (mg/l) = 50 FLOW (mgd) = 59.5 VSS (mg/l) = DIV/0! TSS (lb/d) = 282,9 VSS/TSS Ratio= 80% BOD (lb/d) = 57,308 BOD (mg/l) = 4.0 TSS (lb/d) = - VSS (lb/d) = 226,329 TSS (lb/d) = 3,308 TSS (mg/l) = 4.0 VSS (lb/d) = - VSS (lb/d) = 25,047 VSS (mg/l) = 3.2 VSS/TSS RATIO 70% BOD (lb/d) =,985 ACTIVATED SLUDGE PLANT NO. 2 (P-02) TSS (lb/d) =,985 VSS (lb/d) =,588 VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS lbs TSS Yield / lb BOD Removed = 0.80 RETURN ACTIVATED SLUDGE (RAS) AS2 WAS FLOW (mgd) = 0.5 TSS (mg/l) = 0,000 VSS (mg/l) = 8,000 TSS (lb/d) = 42,274 VSS (lb/d) = 33,89 Dry Solids.00% VSS/TSS Ratio 80% TF EFFLUENT FLOW (mgd) = 30 BOD (mg/l) = 4.7 TSS (mg/l) = 5.5 TF INFLUENT VSS (mg/l) = % Note: GWRS only take TF EF up to 25% of toal SE FLOW (mgd) = 30 TRICKLING FILTER (P-76) BOD (lb/d) = 3, mgd (AS EF + AS2 EF + TF EF)*25% BOD (mg/l) = 5 TSS (lb/d) = 3,869 0 mgd If TF EF less than 25%, 0 mgd to ocean outfall TSS (mg/l) = 63 TRICKLING VSS (lb/d) = 3,096 VSS (mg/l) = 50 TRICKLING FILTER VSS/TSS Ratio 80% BOD (lb/d) = 28,654 FILTERS SECONDARY TSS (lb/d) = 5,654 CLARIFIERS VSS (lb/d) = 2,523 lbs TSS Yield / lb BOD Removed = 0.60 COMBINED WAS PRIMARY SLUDGE FLOW (mgd) =.26 FLOW (mgd) = 0.00 TSS (mg/l) = 0,000 BOD (mg/l) = 23,089 VSS (mg/l) = 8,000 TSS (mg/l) = 4,000 TSS (lb/d) = 05,7 TRICKLING FILTER SLUDGE VSS (mg/l) = 32,800 VSS (lb/d) = 84,37 FLOW (mgd) = 0.07 BOD (lb/d) = - TSS (mg/l) = 20,000 TSS (lb/d) = - VSS (mg/l) = 6,000 VSS (lb/d) = - TSS (lb/d) =,2 VSS (lb/d) = 8,897 Dry Solids 2.00% TO PLANT 2 VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 39 P age

91 OCSD Solids Loading Projection White Paper Plant - Solids Process Mass Balance Condition 3 BLENDED CENTRIFUGE INFLUENT POLYMER FLOW THICKENED SLUDGE DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 2.6 ACTIVE (lb/d)= 2,495 FLOW (mgd) = 0.76 FLOW (mgd) = 0.76 FLOW (mgd) = 0.76 ACTIVE (lb/d)= 5,234 SOLIDS (LB/D) = 203,062 FLOW (GPM) = 497 ACTIVE (gpd)= FLOW (GPM) = 526 FLOW (GPM) = 526 FLOW (GPM) = 526 ACTIVE (gpd)= CAKE WET TONS = 363 TSS (mg/l) = 22,2 FLOW(gpm)= 00.9 TSS (mg/l) = 60,000 TSS (mg/l) = 60,000 TSS (mg/l) = 33,20 FLOW(gpm)= 2.5 CAKE (CF/D) =,332 VSS (mg/l) = 7,769 VSS (mg/l) = 48,000 VSS (mg/l) = 48,000 VSS (mg/l) = 2,20 CAKE (CFM) = 7.9 TSS (lb/d) = 399,203 TSS (lb/d) = 379,243 TSS (lb/d) = 379,243 TSS (lb/d) = 209,342 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 39,362 VSS (lb/d) = 303,394 VSS (lb/d) = 303,394 VSS (lb/d) = 33,493 LB/CF PRIMARY SLUDGE VSS/TSS RATIO 80% FLOW (mgd) = 0.83 TSS (mg/l) = 4,000 CENTRIFUGE DIGESTER CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS TRUCK LOADOUT VSS (mg/l) = 32,800 00% 0% CO-THICKENNING CENTRIFUGE DIGESTER 00% 0% 363 WET TONS/DAY TSS (lb/d) = 282,9 CAKE THICKENESS 28% 0 CY/DAY VSS (lb/d) = 226,329 PRODUCT SOLIDS CONCENTRATION 6% WORKING VOLUME CUFT 2,577,540 COLIDS CAPTURE RATE 97% COLIDS CAPTURE RATE 95% CENTRATE INCLUDE POLYMER HRT 25.4 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 5,000 POLYMER DOSE 5 lb/dt FLOW (mgd) =.54 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 0.98 HRT (DAYS) 4.5 EMULSION POLYMER FLOW (GPM) = 07 SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 679 PERCENT ACTIVE 40% TSS (mg/l) =,552 (HRT need 6-7 days for at least sub-class B) CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 770 FINAL DILUTION 0.2% VSS (mg/l) =,24 CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 6,280 POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 9,960 CAKE (CFM) = - VSS (lb/d) = 5,968 CAKE SPECIFIC WEIGHT 63 VSS/TSS RATIO 80% LB/CF COMBINED WAS FLOW (mgd) =.26 DAFT WAS INFLUENT BELT PRESS WASH WATER 0 MGD BELT-PRESS DEWATERING TSS (mg/l) = 0,000 CENTRIFUGE DAFT FLOW (mgd) = 0.00 THICKENED WAS VSS (mg/l) = 8,000 00% 0% FLOW (GPM) = 0 FLOW (mgd) = 0.00 TSS (lb/d) = 05,7 TSS (mg/l) = DIV/0! FLOW (GPM) = 0 CAKE THICKENESS 20.0% VSS (lb/d) = 84,37 VSS (mg/l) = DIV/0! TSS (mg/l) = 46,000 COLIDS CAPTURE RATE 97% TSS (lb/d) = - VSS (mg/l) = 36,800 WSAH WATER.6 MGD VSS (lb/d) = - TSS (lb/d) = - FILTRATE VSS (lb/d) = - FLOW (mgd) = 0.00 VSS/TSS RATIO 80% FLOW (GPM) = 0 DAFT (WAS THICKENNING) TSS (mg/l) = DIV/0! TSS (lb/d) = - TRICKLING FILTER SLUDGE PRODUCT SOLIDS CONCENTRATION 4.6% FLOW (mgd) = 0.07 COLIDS CAPTURE RATE 99.5% TSS (mg/l) = 20,000 CENTRIFUGE DIGESTER VSS (mg/l) = 6,000 00% 0% TSS (lb/d) =,2 TOTAL WASTE FLOW VSS (lb/d) = 8,897 DAFT UNDERFLOW FLOW (mgd) = 0.0 FLOW (mgd) = 0.00 FLOW (GPM) = 0 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW RECYCLE FLOW TO P TSS (mg/l) = DIV/0! TSS (lb/d) = - FLOW (mgd) = 2.5 FLOW (mgd) = 0.00 VSS (mg/l) = DIV/0! FLOW (GPM) = 750 FLOW (GPM) = 0 TSS (lb/d) = - TSS (mg/l) =,248 TSS (mg/l) = DIV/0! VSS (lb/d) = - VSS (mg/l) = 874 VSS (mg/l) = DIV/0! VSS/TSS RATIO 80% TSS (lb/d) = 26,240 TSS (lb/d) = - VSS (lb/d) = 8,368 VSS (lb/d) = - VSS/TSS RATIO 70% VSS/TSS RATIO 70% P P2 DAFT Underflow 0% 00% TO AS INFLUENT RECYCLE FLOW TO P2 FLOW (mgd) = 2.5 FLOW (GPM) = 750 TSS (mg/l) =,248 VSS (mg/l) = 874 TSS (lb/d) = 26,240 VSS (lb/d) = 8,368 VSS/TSS RATIO 70% 40 P age

92 OCSD Solids Loading Projection White Paper Plant 2 - Liquid Process Mass Balance - Condition 3 RAW INFLUENT PRIMARY INFLUENT Flow (mgd) = 44 Flow (mgd) = 58 PRIMARY EFFLUENT AS PLANT INFLUENT AS EFFLUENT BOD (mg/l) = 250 BOD (mg/l) = 228 Flow (mgd) = 57 FLOW (mgd) = 90 FLOW (mgd) = 87.5 TSS (mg/l) = 270 TSS (mg/l) = 273 BOD (mg/l) = 92 BOD (mg/l) = 92 BOD (mg/l) = 4.0 BOD (lb/d) = 300,240 BOD (lb/d) = 300,240 TSS (mg/l) = 69 TSS (mg/l) = 69 TSS (mg/l) = MGD GAP WATER FROM OCWD TSS (lb/d) = 324,259 TSS (lb/d) = 359,340 BOD (lb/d) = 20,096 BOD (lb/d) = 68,86 BOD (lb/d) = 2,98 P OUTFALL EFFLUENT VSS (lb/d) = 275,620 VSS (lb/d) = 300,77 TSS (lb/d) = 89,835 TSS (lb/d) = 5,50 PURE OXYGEN ACTIVATED SLUDGE PLANT TSS (lb/d) = 4,03 5 MG 23 MG VSS/TSS= 85% PW RAW SEW RAW SEWAGE HEADWORKS & INFLUENT AERATION BASINS SECONDARY CLARIFIERS TOTAL OCEAN OUTFALL 6 MG PUMP STATION INFLUENT INFLUENT PRIMARY CLARIFIERS BOD Removal = 60% TSS & VSS Removal = 75% lbs TSS Yield / lb BOD Removed =.0 COMBINED P2 SECONDARY EFFLUENT FLOW (mgd) = 0.00 P RECYCLE FLOW TO P2 SOLIDS FROM CHEM FLOW (mgd) = 43 BOD (mg/l) = 23,089 FLOW (mgd) = 2.52 FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) BOD (mg/l) = 5.0 TSS (mg/l) = 4,000 FLOW (GPM) = 750 Dose (mg/l) = 8 TSS (mg/l) = 7.7 VSS (mg/l) = 32,800 TSS (mg/l) = 248 TSS (lb/d) = 2,67 BOD (lb/d) = 5,935 BOD (lb/d) = - VSS (mg/l) = 874 POLYMER SOLIDS AS WAS TSS (lb/d) = 9,224 TSS (lb/d) = - TSS (lb/d) = Dose (mg/l) = 0.2 FLOW (mgd) = 2.57 VSS (lb/d) = - VSS (lb/d) = 8368 TSS (lb/d) = 240 TSS (mg/l) = 3,200 VSS (mg/l) = 2,720 TF/SC EFFLUENT TO OUTFALL P RECYCLE FLOW TO P2 TSS (lb/d) = 68,524 FLOW (mgd) = 55.9 VSS (lb/d) = 58,246 BOD (mg/l) = 5.5 Dry Solids 0.32% TSS (mg/l) = 9.5 PRIMARY SLUDGE VSS/TSS Ratio 85% BOD (lb/d) = 2,565 P2 RECYCLE FLOW PLUS PW/GAP WASHWATER FLOW (mgd) = 0.78 TSS (lb/d) = 4,430 P PRIMARY SLUDGE DIVERSION FLOW (mgd) =.3 BOD (mg/l) = 27,823 FLOW (GPM) = 785 TSS (mg/l) = 45,000 Dry Solids Conc.= 4.5% TSS (mg/l) = 94 VSS (mg/l) = 33,300 VSS/TSS Ratio= 74% VSS (mg/l) = 66 BOD (lb/d) = 80,44 TF/SC EFFLUENT TSS (lb/d) = 884 TSS (lb/d) = 29,363 FLOW (mgd) = 65.8 VSS (lb/d) = 689 VSS (lb/d) = 25,608 BOD (mg/l) = 5.5 TSS (mg/l) = 9.5 BOD (lb/d) = 3,07 TRICKLING FILTER (P2-90) TSS (lb/d) = 5,2 TF/SC INFLUENT FLOW (mgd) = 67 TRICKLING TRICKLING BOD (mg/l) = 92 FILTERS FILTER 0 MGD PUMPED TO GWRS TSS (mg/l) = 69 /SOLIDS SECONDARY BOD (lb/d) = 5,235 CONTACT CLARIFIERS TSS (lb/d) = 38,325 lbs TSS Yield / lb BOD Removed = 0.85 COMBINED SECONDARY SLUDGE FLOW (mgd) = 3.79 TSS (mg/l) = 3,297 VSS (mg/l) = 2,746 TSS (lb/d) = 04,298 TF/SC WSS VSS (lb/d) = 86,865 FLOW (mgd) =.23 TSS (mg/l) = 3,500 VSS (mg/l) = 2,800 TSS (lb/d) = 35,774 VSS (lb/d) = 28,69 Dry Solids 0.35% VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 4 P age

93 OCSD Solids Loading Projection White Paper Plant 2 - Solids Process Mass Balance Condition 3 DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 0.99 FLOW (mgd) = 0.99 ACTIVE (lb/d)= 5,629 SOLIDS (LB/D) = 28,408 FLOW (GPM) = 688 FLOW (GPM) = 688 ACTIVE (gpd)= CAKE WET TONS = 390 TSS (mg/l) = 47,603 TSS (mg/l) = 27,233 FLOW(gpm)= CAKE (CF/D) = 2,88 VSS (mg/l) = 36,374 VSS (mg/l) = 6,004 CAKE (CFM) = 8.5 TSS (lb/d) = 393,575 TSS (lb/d) = 225,63 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 300,736 VSS (lb/d) = 32,324 LB/CF PRIMARY SLUDGE FLOW (mgd) = 0.78 TRUCK LOADOUT TSS (mg/l) = 45,000 CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS 390 WET TONS/DAY VSS (mg/l) = 33,300 DIGESTER 00% 0% TSS (lb/d) = 29,363 CAKE THICKENESS 28% VSS (lb/d) = 25,608 WORKING VOLUME CUFT 2,620,32 (I,J,K as holders) COLIDS CAPTURE RATE 97% HRT 9.8 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 28,000 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) =.2 HRT (DAYS) 2.3 DAFT WAS INFLUENT (Need at least 8 days for Class B) SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 853 FLOW (mgd) = 3.79 CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 660 FLOW (GPM) = 2634 THICKENED WAS CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 6,755 TSS (mg/l) = 3,297 FLOW (mgd) = 0.22 CAKE (CFM) = - VSS (mg/l) = 2,746 FLOW (GPM) = 49 CAKE SPECIFIC WEIGHT 63 TSS (lb/d) = 04,298 TSS (mg/l) = 57,000 LB/CF VSS (lb/d) = 86,865 VSS (mg/l) = 47, MGD COMBINED SECONDARY SLUDGE TSS (lb/d) = 02,22 BELT PRESS WASH WATER FLOW (mgd) = 3.79 VSS (lb/d) = 85,27 BELT-PRESS DEWATERING TSS (mg/l) = 3,297 DAFT (WAS THICKENNING) VSS (mg/l) = 2,746 CAKE THICKENESS 22.0% TSS (lb/d) = 04,298 COLIDS CAPTURE RATE 97% VSS (lb/d) = 86,865 PRODUCT SOLIDS CONCENTRATION 5.7% WASH WATER.6 mgd COLIDS CAPTURE RATE 98.0% FILTRATE FLOW (mgd) = 0.00 DAFT UNDERFLOW FLOW (GPM) = 0 FLOW (mgd) = 3.58 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW FLOW (GPM) = 2485 TSS (lb/d) = - FLOW (mgd) = 4.8 TSS (mg/l) = 70 FLOW (GPM) = 3337 VSS (mg/l) = 58 TOTAL WASTE FLOW TSS (mg/l) = 22 TSS (lb/d) = 2,086 FLOW (mgd) = 0.0 VSS (mg/l) = 54 VSS (lb/d) =,737 FLOW (GPM) = 0 TSS (lb/d) = 8,84 TSS (mg/l) = DIV/0! VSS (lb/d) = 6,89 TSS (lb/d) = - VSS/TSS RATIO 70% 42 P age

94 OCSD Solids Loading Projection White Paper Plant - Liquid Process Mass Balance - Condition 4 DAFT UNDERFLOW FLOW (mgd) = MGD PUMPED FROM P2 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! VSS (mg/l) = DIV/0! CENGEN COOLING WATER 2 MGD TSS (lb/d) = 0 VSS (lb/d) = 0 MF BACKWASH AS INFLUENT FLOW (mgd) = 92 BOD (mg/l) = 6 TSS (mg/l) = 63 COMBINED P SECONDARY EFFLUENT RAW INFLUENT PRIMARY INFLUENT VSS (mg/l) = 50 AS EFFLUENT AND PUMPED Flow (mgd) = 235 Flow (mgd) = 238 PRIMARY EFFLUENT SECONDARY INFLUENT BOD (lb/d) = 88,66 FLOW (mgd) = 9. P2 TF/SC EFFLUENT to OCWD MF INFLUENT MF BACKWASH MF EFFLUENT/RO INFLUENT BOD (mg/l) = 250 BOD (mg/l) = 249 Flow (mgd) = 237 Flow (mgd) = 254 TSS (lb/d) = 48,244 BOD (mg/l) = 4.5 FLOW (mgd) = 249 FLOW (mgd) = 70 FLOW (mgd) = 7 FLOW (mgd) = 53 TSS (mg/l) = 270 TSS (mg/l) = 269 BOD (mg/l) = 25 BOD (mg/l) = 8 VSS (lb/d) = 38,595 TSS (mg/l) = 4.0 BOD (mg/l) = 5.6 BOD (mg/l) = 5.6 BOD (mg/l) = 38 BOD (mg/l) = 2 BOD (lb/d) = 489,975 BOD (lb/d) = 495,292 TSS (mg/l) = 68 TSS (mg/l) = 64 VSS (mg/l) = 3.2 TSS (mg/l) = 5.5 TSS (mg/l) = 5.5 TSS (mg/l) = 37 TSS (mg/l) = 2 TSS (lb/d) = 529,73 TSS (lb/d) = 534,367 VSS (mg/l) = 54 VSS (mg/l) = 5 BOD (lb/d) = 3,420 BOD (lb/d) =,52 BOD (lb/d) = 7,869 BOD (lb/d) = 5,37 BOD (lb/d) = 2,552 VSS (lb/d) = 449,797 VSS (lb/d) = 454,22 BOD (lb/d) = 247,646 BOD (lb/d) = 250,98 ACTIVATED SLUDGE PLANT NO. (P-82) TSS (lb/d) = 3,040 TSS (lb/d) =,340 TSS (lb/d) = 7,746 TSS (lb/d) = 5,94 TSS (lb/d) = 2,552 VSS/TSS= 85% VSS/TSS= 85% TSS (lb/d) = 33,592 TSS (lb/d) = 36,44 VSS (lb/d) = 2,432 VSS (lb/d) = 06,873 VSS (lb/d) = 0895 VSS/TSS Ratio 80% OCWD GWRS RAW SEWAGE HEADWORKS & VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS GWRS PRODUCT WATER 30 MGD INFLUENT MICROFILTRATION REVERSE OSMOSIS INFLUENT PRIMARY CLARIFIERS PUMP STATION BOD Removal = 50% TSS Removal = 75% lbs TSS Yield / lb BOD Removed = 0.90 VSS/TSS Ratio 80% RO DISCHARGE TO OCEAN OUTFALL 23 MGD SOLIDS FROM CHEM FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) OCSD GREEN ACRES 5 MGD Dose (mg/l) = 20 TSS (lb/d) = 39,98 MISCELLANEOUS PROCESS WASH WATER FLOW POLYMER SOLIDS AS WAS PW PS 0.3 MGD FLOW (mgd) = 3.3 Dose (mg/l) = 0.2 FLOW (mgd) = MGD (BECOME WASHWATER) GAP WATER FROM OCWD BOD (mg/l) = - TSS (lb/d) = 392 TSS (mg/l) = 0,000 TSS (mg/l) = - VSS (mg/l) = 8,000 BOD (lb/d) = 0 TSS (lb/d) = 73,676 TSS (lb/d) = 0 VSS (lb/d) = 58,94 SECONDARY EFFLUENT TO OCEAN OUTFALL 74 MGD VSS (lb/d) = 0 Dry Solids.00% PRIMARY SLUDGE VSS/TSS Ratio 80% FLOW (mgd) =.29 AS2 INFLUENT 0 MGD RECYCLE FLOW TO P BOD (mg/l) = 23,057 FLOW (mgd) = 34 BELT PRESS WASHING WATER FLOW (mgd) = 0.00 TSS (mg/l) = 4,000 Dry Solids Conc.= 4.% BOD (mg/l) = 8 FLOW (GPM) = 0 VSS (mg/l) = 32,800 TSS (mg/l) = 64 AS2 EFFLUENT TSS (mg/l) = DIV/0! BOD (lb/d) = 247,646 VSS (mg/l) = 5 FLOW (mgd) = 32.8 VSS (mg/l) = DIV/0! TSS (lb/d) = 440,365 VSS/TSS Ratio= 80% BOD (lb/d) = 3,988 BOD (mg/l) = 4.0 TSS (lb/d) = - VSS (lb/d) = 352,292 TSS (lb/d) = 7,820 TSS (mg/l) = 4.0 VSS (lb/d) = - VSS (lb/d) = 57,456 VSS (mg/l) = 3.2 VSS/TSS RATIO 70% BOD (lb/d) = 4,43 ACTIVATED SLUDGE PLANT NO. 2 (P-02) TSS (lb/d) = 4,43 VSS (lb/d) = 3,545 VSS/TSS Ratio 80% AERATION BASINS SECONDARY CLARIFIERS lbs TSS Yield / lb BOD Removed = 0.80 RETURN ACTIVATED SLUDGE (RAS) AS2 WAS FLOW (mgd) =.7 TSS (mg/l) = 0,000 VSS (mg/l) = 8,000 TSS (lb/d) = 97,64 VSS (lb/d) = 78,09 Dry Solids.00% VSS/TSS Ratio 80% TF EFFLUENT FLOW (mgd) = 30 BOD (mg/l) = 4.7 TSS (mg/l) = 5.5 TF INFLUENT VSS (mg/l) = % Note: GWRS only take TF EF up to 25% of toal SE FLOW (mgd) = 30 TRICKLING FILTER (P-76) BOD (lb/d) = 3, mgd (AS EF + AS2 EF + TF EF)*25% BOD (mg/l) = 8 TSS (lb/d) = 3,869 0 mgd If TF EF less than 25%, 0 mgd to ocean outfall TSS (mg/l) = 64 TRICKLING VSS (lb/d) = 3,095 VSS (mg/l) = 5 TRICKLING FILTER VSS/TSS Ratio 80% BOD (lb/d) = 29,550 FILTERS SECONDARY TSS (lb/d) = 6,079 CLARIFIERS VSS (lb/d) = 2,863 lbs TSS Yield / lb BOD Removed = 0.60 COMBINED WAS PRIMARY SLUDGE FLOW (mgd) = 2.05 FLOW (mgd) = 0.00 TSS (mg/l) = 0,000 BOD (mg/l) = 23,057 VSS (mg/l) = 8,000 TSS (mg/l) = 4,000 TSS (lb/d) = 7,29 TRICKLING FILTER SLUDGE VSS (mg/l) = 32,800 VSS (lb/d) = 37,032 FLOW (mgd) = 0.07 BOD (lb/d) = - TSS (mg/l) = 20,000 TSS (lb/d) = - VSS (mg/l) = 6,000 VSS (lb/d) = - TSS (lb/d) =,659 VSS (lb/d) = 9,327 Dry Solids 2.00% TO PLANT 2 VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 43 P age

95 OCSD Solids Loading Projection White Paper Plant - Solids Process Mass Balance Condition 4 BLENDED CENTRIFUGE INFLUENT POLYMER FLOW THICKENED SLUDGE DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) = 3.4 ACTIVE (lb/d)= 3,896 FLOW (mgd) =.8 FLOW (mgd) =.8 FLOW (mgd) =.8 ACTIVE (lb/d)= 8,72 SOLIDS (LB/D) = 37,060 FLOW (GPM) = 2369 ACTIVE (gpd)= FLOW (GPM) = 822 FLOW (GPM) = 822 FLOW (GPM) = 822 ACTIVE (gpd)= 95.3 CAKE WET TONS = 566 TSS (mg/l) = 2,907 FLOW(gpm)= 57.5 TSS (mg/l) = 60,000 TSS (mg/l) = 60,000 TSS (mg/l) = 33,20 FLOW(gpm)= CAKE (CF/D) = 7,693 VSS (mg/l) = 7,526 VSS (mg/l) = 48,000 VSS (mg/l) = 48,000 VSS (mg/l) = 2,20 CAKE (CFM) = 2.3 TSS (lb/d) = 623,35 TSS (lb/d) = 592,49 TSS (lb/d) = 592,49 TSS (lb/d) = 326,866 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 498,652 VSS (lb/d) = 473,79 VSS (lb/d) = 473,79 VSS (lb/d) = 208,436 LB/CF PRIMARY SLUDGE VSS/TSS RATIO 80% FLOW (mgd) =.29 TSS (mg/l) = 4,000 CENTRIFUGE DIGESTER CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS TRUCK LOADOUT VSS (mg/l) = 32,800 00% 0% CO-THICKENNING CENTRIFUGE DIGESTER 00% 0% 566 WET TONS/DAY TSS (lb/d) = 440,365 CAKE THICKENESS 28% 0 CY/DAY VSS (lb/d) = 352,292 PRODUCT SOLIDS CONCENTRATION 6% WORKING VOLUME CUFT 2,577,540 COLIDS CAPTURE RATE 97% COLIDS CAPTURE RATE 95% CENTRATE INCLUDE POLYMER HRT 6.3 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 5,000 POLYMER DOSE 5 lb/dt FLOW (mgd) = 2.45 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) =.53 HRT (DAYS) 2.9 EMULSION POLYMER FLOW (GPM) = 705 SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 060 PERCENT ACTIVE 40% TSS (mg/l) =,522 (HRT need 6-7 days for at least sub-class B) CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 770 FINAL DILUTION 0.2% VSS (mg/l) =,28 CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 9,806 POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 3,66 CAKE (CFM) = - VSS (lb/d) = 24,933 CAKE SPECIFIC WEIGHT 63 VSS/TSS RATIO 80% LB/CF COMBINED WAS FLOW (mgd) = 2.05 DAFT WAS INFLUENT BELT PRESS WASH WATER 0 MGD BELT-PRESS DEWATERING TSS (mg/l) = 0,000 CENTRIFUGE DAFT FLOW (mgd) = 0.00 THICKENED WAS VSS (mg/l) = 8,000 00% 0% FLOW (GPM) = 0 FLOW (mgd) = 0.00 TSS (lb/d) = 7,29 TSS (mg/l) = DIV/0! FLOW (GPM) = 0 CAKE THICKENESS 20.0% VSS (lb/d) = 37,032 VSS (mg/l) = DIV/0! TSS (mg/l) = 46,000 COLIDS CAPTURE RATE 97% TSS (lb/d) = - VSS (mg/l) = 36,800 WSAH WATER.6 MGD VSS (lb/d) = - TSS (lb/d) = - FILTRATE VSS (lb/d) = - FLOW (mgd) = 0.00 VSS/TSS RATIO 80% FLOW (GPM) = 0 DAFT (WAS THICKENNING) TSS (mg/l) = DIV/0! TSS (lb/d) = - TRICKLING FILTER SLUDGE PRODUCT SOLIDS CONCENTRATION 4.6% FLOW (mgd) = 0.07 COLIDS CAPTURE RATE 99.5% TSS (mg/l) = 20,000 CENTRIFUGE DIGESTER VSS (mg/l) = 6,000 00% 0% TSS (lb/d) =,659 TOTAL WASTE FLOW VSS (lb/d) = 9,327 DAFT UNDERFLOW FLOW (mgd) = 0.0 FLOW (mgd) = 0.00 FLOW (GPM) = 0 FLOW (GPM) = 0 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW RECYCLE FLOW TO P TSS (mg/l) = DIV/0! TSS (lb/d) = - FLOW (mgd) = 4.0 FLOW (mgd) = 0.00 VSS (mg/l) = DIV/0! FLOW (GPM) = 2765 FLOW (GPM) = 0 TSS (lb/d) = - TSS (mg/l) =,234 TSS (mg/l) = DIV/0! VSS (lb/d) = - VSS (mg/l) = 864 VSS (mg/l) = DIV/0! VSS/TSS RATIO 80% TSS (lb/d) = 40,972 TSS (lb/d) = - VSS (lb/d) = 28,680 VSS (lb/d) = - VSS/TSS RATIO 70% VSS/TSS RATIO 70% P P2 DAFT Underflow 0% 00% TO AS INFLUENT RECYCLE FLOW TO P2 FLOW (mgd) = 4.0 FLOW (GPM) = 2765 TSS (mg/l) =,234 VSS (mg/l) = 864 TSS (lb/d) = 40,972 VSS (lb/d) = 28,680 VSS/TSS RATIO 70% 44 P age

96 OCSD Solids Loading Projection White Paper Plant 2 - Liquid Process Mass Balance - Condition 4 RAW INFLUENT PRIMARY INFLUENT Flow (mgd) = 235 Flow (mgd) = 253 PRIMARY EFFLUENT AS PLANT INFLUENT AS EFFLUENT BOD (mg/l) = 250 BOD (mg/l) = 232 Flow (mgd) = 252 FLOW (mgd) = 90 FLOW (mgd) = 87.4 TSS (mg/l) = 270 TSS (mg/l) = 277 BOD (mg/l) = 93 BOD (mg/l) = 93 BOD (mg/l) = 4.0 BOD (lb/d) = 489,975 BOD (lb/d) = 489,975 TSS (mg/l) = 70 TSS (mg/l) = 70 TSS (mg/l) = MGD GAP WATER FROM OCWD TSS (lb/d) = 529,73 TSS (lb/d) = 584,4 BOD (lb/d) = 95,990 BOD (lb/d) = 70,38 BOD (lb/d) = 2,95 P OUTFALL EFFLUENT VSS (lb/d) = 449,797 VSS (lb/d) = 488,275 TSS (lb/d) = 46,035 TSS (lb/d) = 52,26 PURE OXYGEN ACTIVATED SLUDGE PLANT TSS (lb/d) = 4,008 5 MG 97 MG VSS/TSS= 85% PW RAW SEW RAW SEWAGE HEADWORKS & INFLUENT AERATION BASINS SECONDARY CLARIFIERS TOTAL OCEAN OUTFALL 338 MG PUMP STATION INFLUENT INFLUENT PRIMARY CLARIFIERS BOD Removal = 60% TSS & VSS Removal = 75% lbs TSS Yield / lb BOD Removed =.0 COMBINED P2 SECONDARY EFFLUENT FLOW (mgd) = 0.00 P RECYCLE FLOW TO P2 SOLIDS FROM CHEM FLOW (mgd) = 246 BOD (mg/l) = 23,057 FLOW (mgd) = 3.98 FERRIC CHLORIDE SOLIDS RETURN ACTIVATED SLUDGE (RAS) BOD (mg/l) = 5.0 TSS (mg/l) = 4,000 FLOW (GPM) = 2765 Dose (mg/l) = 8 TSS (mg/l) = 8. VSS (mg/l) = 32,800 TSS (mg/l) = 234 TSS (lb/d) = 35,278 BOD (lb/d) = 0,84 BOD (lb/d) = - VSS (mg/l) = 864 POLYMER SOLIDS AS WAS TSS (lb/d) = 6,564 TSS (lb/d) = - TSS (lb/d) = Dose (mg/l) = 0.2 FLOW (mgd) = 2.62 VSS (lb/d) = - VSS (lb/d) = TSS (lb/d) = 392 TSS (mg/l) = 3,200 VSS (mg/l) = 2,720 TF/SC EFFLUENT TO OUTFALL P RECYCLE FLOW TO P2 TSS (lb/d) = 69,937 FLOW (mgd) = 58.5 VSS (lb/d) = 59,446 BOD (mg/l) = 5.5 Dry Solids 0.32% TSS (mg/l) = 9.5 PRIMARY SLUDGE VSS/TSS Ratio 85% BOD (lb/d) = 7,269 P2 RECYCLE FLOW PLUS PW/GAP WASHWATER FLOW (mgd) =.26 TSS (lb/d) = 2,556 P PRIMARY SLUDGE DIVERSION FLOW (mgd) = 3.79 BOD (mg/l) = 27,923 FLOW (GPM) = 9573 TSS (mg/l) = 45,000 Dry Solids Conc.= 4.5% TSS (mg/l) = 22 VSS (mg/l) = 33,300 VSS/TSS Ratio= 74% VSS (mg/l) = 85 BOD (lb/d) = 293,985 TF/SC EFFLUENT TSS (lb/d) = 3996 TSS (lb/d) = 473,776 FLOW (mgd) = 58.5 VSS (lb/d) = 9797 VSS (lb/d) = 350,594 BOD (mg/l) = 5.5 TSS (mg/l) = 9.5 BOD (lb/d) = 7,269 TRICKLING FILTER (P2-90) TSS (lb/d) = 2,556 TF/SC INFLUENT FLOW (mgd) = 62 TRICKLING TRICKLING BOD (mg/l) = 93 FILTERS FILTER 0 MGD PUMPED TO GWRS TSS (mg/l) = 70 /SOLIDS SECONDARY BOD (lb/d) = 25,852 CONTACT CLARIFIERS TSS (lb/d) = 93,774 lbs TSS Yield / lb BOD Removed = 0.85 COMBINED SECONDARY SLUDGE FLOW (mgd) = 5.64 TSS (mg/l) = 3,36 VSS (mg/l) = 2,763 TSS (lb/d) = 58,76 TF/SC WSS VSS (lb/d) = 30,038 FLOW (mgd) = 3.02 TSS (mg/l) = 3,500 VSS (mg/l) = 2,800 TSS (lb/d) = 88,239 VSS (lb/d) = 70,59 Dry Solids 0.35% VSS/TSS Ratio 80% TO SOLIDS HANDLING SHEET 45 P age

97 OCSD Solids Loading Projection White Paper Plant 2 - Solids Process Mass Balance Condition 4 DIGESTERE INFLUENT DIGESTED SLUDGE POLYMER FLOW DEWATERED CAKE FLOW (mgd) =.59 FLOW (mgd) =.59 ACTIVE (lb/d)= 9,027 SOLIDS (LB/D) = 350,258 FLOW (GPM) = 03 FLOW (GPM) = 03 ACTIVE (gpd)=,050.9 CAKE WET TONS = 625 TSS (mg/l) = 47,463 TSS (mg/l) = 27,257 FLOW(gpm)= CAKE (CF/D) = 9,546 VSS (mg/l) = 36,084 VSS (mg/l) = 5,877 CAKE (CFM) = 3.6 TSS (lb/d) = 628,788 TSS (lb/d) = 36,09 CAKE SPECIFIC WEIGHT 64 VSS (lb/d) = 478,03 VSS (lb/d) = 20,334 LB/CF PRIMARY SLUDGE FLOW (mgd) =.26 TRUCK LOADOUT TSS (mg/l) = 45,000 CENTRIFUGE BELT PRESS CENTRIFUGE DEWATERING CAKE SILOS 625 WET TONS/DAY VSS (mg/l) = 33,300 DIGESTER 00% 0% TSS (lb/d) = 473,776 CAKE THICKENESS 28% VSS (lb/d) = 350,594 WORKING VOLUME CUFT 2,620,32 (I,J,K as holders) COLIDS CAPTURE RATE 97% HRT 2.3 POLYMER DOSE 20 lb/dt CENTRATE PLUS POLYMER WORKING VOLUME (CF) 28,000 VSS REDUCTION 56% DEWATERED CAKE EMULSION POLYMER FLOW (mgd) = 2.0 HRT (DAYS).4 DAFT WAS INFLUENT (Need at least 8 days for Class B) SOLIDS (LB/D) = - PERCENT ACTIVE 40% FLOW (GPM) = 366 FLOW (mgd) = 5.64 CAKE WET TONS = - FINAL DILUTION 0.2% TSS (mg/l) = 660 FLOW (GPM) = 399 THICKENED WAS CAKE (CF/D) = - POLYMER DENSITY 8.59 lb/g TSS (lb/d) = 0,833 TSS (mg/l) = 3,36 FLOW (mgd) = 0.33 CAKE (CFM) = - VSS (mg/l) = 2,763 FLOW (GPM) = 226 CAKE SPECIFIC WEIGHT 63 TSS (lb/d) = 58,76 TSS (mg/l) = 57,000 LB/CF VSS (lb/d) = 30,038 VSS (mg/l) = 46, MGD COMBINED SECONDARY SLUDGE TSS (lb/d) = 55,02 BELT PRESS WASH WATER FLOW (mgd) = 5.64 VSS (lb/d) = 27,437 BELT-PRESS DEWATERING TSS (mg/l) = 3,36 DAFT (WAS THICKENNING) VSS (mg/l) = 2,763 CAKE THICKENESS 22.0% TSS (lb/d) = 58,76 COLIDS CAPTURE RATE 97% VSS (lb/d) = 30,038 PRODUCT SOLIDS CONCENTRATION 5.7% WASH WATER.6 mgd COLIDS CAPTURE RATE 98.0% FILTRATE FLOW (mgd) = 0.00 DAFT UNDERFLOW FLOW (GPM) = 0 FLOW (mgd) = 5.32 TSS (mg/l) = DIV/0! TOTAL RECYCLE FLOW FLOW (GPM) = 3693 TSS (lb/d) = - FLOW (mgd) = 7.29 TSS (mg/l) = 7 FLOW (GPM) = 5059 VSS (mg/l) = 59 TOTAL WASTE FLOW TSS (mg/l) = 230 TSS (lb/d) = 3,64 FLOW (mgd) = 0.0 VSS (mg/l) = 6 VSS (lb/d) = 2,60 FLOW (GPM) = 0 TSS (lb/d) = 3,996 TSS (mg/l) = DIV/0! VSS (lb/d) = 9,797 TSS (lb/d) = - VSS/TSS RATIO 70% 46 P age

98 Orange County Sanitation District TM : OCSD Solids Facilities Summary and Design Basis Appendix C Task.2 White Paper Review Meeting Minutes The following is a copy of the meeting minutes from the White Paper workshop. May 9, 207 C Biosolids Master Plan

99 PS5-0 OCSD BIOSOLIDS MASTER PLAN DRAFT MEETING MINUTES B&V Job No Date: February 8,206 Page: of 4 Meeting Location: OCSD Administration Building - Conference Rooms A & B Meeting Date: February 6, 206 Meeting Time: 2:30 PM to 2:30 PM Meeting Topic: Task.2 Review White Paper Analysis & Loading Criteria Revision Date: Authored By: Dan Buhrmaster Attendees: Handouts: See attached agenda list See attached handouts The key points that were discussed in the meeting are summarized below and follow the order of the meeting agenda. Some points may not be recorded in the same sequence as actually discussed. Action items are noted below and included in the Action Item Log attached to these minutes. No. Item Action By Due Date SAFETY MOMENT 2 TASK OVERVIEW Jim Clark briefly reviewed Task activities using a handout from the contract scope of work. 3 MEETING PURPOSE AND DECISIONS NEEDED Jim Clark stated that the primary purpose of the meeting was to discuss the White Paper analysis by OCSD staff based on review by the B&V/BC team. Decisions needed: () agree on assumptions for White Paper or make adjustments and (2) consensus on the design loadings in Table 5 and Table 6. 4 WHITE PAPER FLOW AND LOADING ANALYSIS Dan Buhrmaster presented an overview of white paper review comments from B&V/BC. The B&V/BC team concurs with the per capita approach for flows, BOD, and TSS. There was discussion regarding the basis for these numbers but the meeting attendees agreed with the white paper values. Sludge yield values were discussed at length. OCSD elaborated on these values and they are based on the most recent 5 years of data. Both B&V and BC mentioned old yield values from the past; however, they agreed that the white paper values are appropriate. The above represents the author s understanding of the items discussed and the decisions made during the context of the meeting. All items are assumed to be correct if the author is not contacted with clarifications.

100 PS5-0 OCSD BIOSOLIDS MASTER PLAN DRAFT MEETING MINUTES B&V Job No Date: February 8,206 Page: 2 of 4 No. Item Action By Due Date Primary clarifier (PC) performance was discussed at length. OCSD reviewed the basis of the numbers in the white paper. Chemically enhanced primary treatment (CEPT) is currently practiced at both plants and the assumed performance for current conditions reflect plant data for the past several years. OCSFD is considering reducing BOD removal efficieny at the PCs for future scenarios. One reason is that OCSD is currently adding chemicals in the upstream sewers for odor control purposes. The result is improved PC performance. There is not guarantee that OCSD will continue chemical feed in the influent sewers. OCSD will make a final evaluation to decide whether to revise the white paper values or not. OCSD Peaking factors were reviewed at the meeting. B&V and BC shared peaking factors that were used for some other projects. The consensus was that the peaking factors used in the white paper (5-Day =.2 and max hour =.6) are reasonable for OCSD Plant and Plant 2 for this project. OCSD will change the title of Table 6 to read Recommended Design Loadings for Solids Handling Facilities. This better identifies these values and how they will be used. The four conditions given in the white paper were reviewed and there was a consensus to keep these as shown no changes. All values in the white paper are considered acceptable for this master plan, except that OCSD will further investigate the primary clarifier performance parameters before finalizing the white paper. OCSD will re-publish the white paper to capture any text changes and any changes that are identified by OCSD to PC performance. 5 DISCUSSION OF HOW WHITE PAPER LOADINGS WILL BE USED Tom Chapman led the discussion of how the white paper numbers will be used for the master plan, particularly in Task 4. The centrifuge performance values were discussed. During the master plan work, the B&V/BC team will use a range of values for centrifuge performance The above represents the author s understanding of the items discussed and the decisions made during the context of the meeting. All items are assumed to be correct if the author is not contacted with clarifications.

101 PS5-0 OCSD BIOSOLIDS MASTER PLAN DRAFT MEETING MINUTES B&V Job No Date: February 8,206 Page: 3 of 4 No. Item Action By Due Date when evaluating facility requirements for handling dewatered cake solids. A low end value of approximately 25% solids concentration is considered more appropriate for these particular facilities for conceptual design. 6 DISCUSSION OF TM CURRENT OUTLINE, STATUS, AND EXCERPTS Jon Hay led this discussion. OCSD prefers that the introduction to each TM be specific to that TM rather than a lengthy general introduction to the entire project. Sharon Yin commented that the excerpts of TM provided by B&V during the meeting were not sufficient for extensive discussion. B&V advised that there is still work to perform and there is adequate time to complete the Draft TM per the project schedule (March 5), including internal QC review. OCSD gave input to B&V regarding some of their expectations for this TM. OCSD is looking for a consise document that emphasizes tables and graphs rather than text. Sharon will provide comments to B&V regarding the table of contents shown at the meeting. For projects that have an X prefix, do not show these in the TM. These projects are not on the budget books and if they are shown, this could confuse some OCSD staff. Per OCSD use the latest information on Share Point for future Plant and Plant 2 facilities. Review previous OCSD comments on the TMs for SP-4 to know some things to avoid. Tom Chapman will provide a paragraph write-up regarding how data from the mass balance will be used for the master plan Task 4. For the SWET tool (cost analysis) in Task 4 Tom will use white paper Condition 25 mgd to Plant and the remainder to Plant 2. B&V has documented comments from operations staff regarding the Plant and Plant 2 site tours. Sharon Yin will advise B&V on how this information will or will nto be used for TM. OCSD BC OCSD The above represents the author s understanding of the items discussed and the decisions made during the context of the meeting. All items are assumed to be correct if the author is not contacted with clarifications.

102 PS5-0 OCSD BIOSOLIDS MASTER PLAN DRAFT MEETING MINUTES B&V Job No Date: February 8,206 Page: 4 of 4 No. Item Action By Due Date 7 REMAINING SCHEDULE AND MEETINGS FOR TASK Jim Clark reviewed the remaining meeting dates for Task see attached file a summary of all project meetings. B&V/BC requested that the date for the Task 3.3 meeting to present Draft TM 3 be changed to July 9, 206. OCSD indicated that this change should be acceptable unless otherwise nofitified. 8 ACTION ITEMS B&V and OCSD reviewed the action items noted above. B&V will add these items to the project Action Item Log. DFB Major Decisions: None The above represents the author s understanding of the items discussed and the decisions made during the context of the meeting. All items are assumed to be correct if the author is not contacted with clarifications.