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Springfield Sugar Creek WWTP Screw Press - Bioset Report

Dewatering Screw Press & Bioset System

REPORT PRESENTED BY:

SCHWING BIOSET, INC. 350 SMC DRIVE, SOMERSET, WI 54025

PHONE: (715) 247-3433 FAX: (715) 247-3438

CONTACT:

TOM WELCH, SE REGIONAL SALES MANAGER PH: 239-216-1776

E-MAIL: [email protected]

SPRINGFIELD SUGAR CREEK WWTP 3300 MECHANICSBURG RD SPRINGFIELD, IL 62707

Schwing Bioset Screw Press – Bioset Pilot

June 17 – June 28, 2013



TABLE OF CONTENTS

Tab 1: Facility & Material Summary Tab 2: Schwing Bioset Test Equipment Tab 3: Pilot Test Results Tab 4: Conclusion

Schwing Bioset Screw Press & Bioset Setup at Sugar Creek WWTP



PLANT AND MATERIAL SUMMARY Sludge Type Waste Activated Sludge Solids Content 1.4 – 1.8% Volatile Solids ≈ 45 - 50%

TEST EQUIPMENT SUMMARY SLUDGE DEWATERING SCREW PRESS

Design Conditions: Schwing Bioset dewatering system sized for: Design dewatering rate (300 dry lbs/hr) At 1.5% solids

40 gallons / minute hydraulic capacity Model: FSP600 Quantity: One (1) Press Length: 15 feet 8.5 inches Press Width: 3 feet 9.9 inches Press Height: 4 feet 11.6 inches Design Capacity (1.5% solids): 395 dry lb/hr Press HP: 3 HP Weight est.: 6,330 lbs

System includes: 1. The SBI Screw Press system is designed for continuous dewatering of flocculated slurry. The

system consists of; a progressive cavity feed pump, polymer system, Screw Press dewatering unit, and controls.

2. The Screw Press dewatering unit compresses and dewaters flocculated slurry using a screw rotating at very slow speed in a perforated screen. Observation windows and flaps allow a direct view of the dewatering process. The simple operating principle is achieved with only a few functional component groups. Slow movement and the high quality design of the structural components guarantee a high service life.

3. Press dewatering system is powered using a Premium efficient, TEFC motor. Variation of the Screw speed is achieved with a VFD.

4. The system will continuously discharge cake from the press into the conveyor. The filtrate will discharge from a drip tray below the perforated screen into a discharge pipe.



5. For general housekeeping purposes the back washing cycle cleans the screens intermittently (generally less than 5 minutes/day). Dewatering operations are not suspended during washing cycle.

6. Air Compressor for discharge pressure cone actuator and movement of wash ring.

FSP600 Screw Press & Bioset Setup at Sugar Creek WWTP



SLUDGE DEWATERING FEED PUMP Quantity: One (1) Pump Type Progressive Cavity Model Liberty LL10 Flow 10-200 gpm

System includes: 1. The feed pump is VFD controlled equipped with an Endress Hauser flow meter at the pump

discharge. Pump speed is controlled by the flow meter and the pressure senor in the sludge flocculation tank.

Sludge Feed Pump



POLYMER FEED SYSTEM

Quantity: One (1) Model Velodyne VM-5P-1200-E Dilution water flow 2-20 gpm Neat polymer flow 0.25 - 5 gph

System includes: 1. Effective mixing of the water and polymer is achieved in Polymer Feed System. The water

polymer blend is manually controlled using a hand valve. In permanent installations the blend control is automated. The feed of the water polymer blend into the Sludge Flocculation Tank is by VFD controlled PC pump. The control panel automatically monitors the flow rate and the pressure of the Flocculation tank.

Polymer System Setup



SLUDGE FLOCCULATION TANK Quantity: One (1) Tank Volume 224.5 gal (850 L) Tank Depth 48 inches Tank Width 30 inches Tank Overall Height 60 inches Tank Weight 485 lbs

System includes: 1. Effective flocculation is achieved in the Sludge Flocculation Tank. It is a closed design with

observation windows for viewing of the current flocculation quality. Special designed paddle and flow breakers for effective mixing and gentle transport of the flocs. Diluted/activated polymer from the Polymer Mixing System enters sludge pipe at tee upstream of Sludge Flocculation Tank.

2. A pressure sensor is included in the top of the tank. The pressure sensor sends a signal back to the control panel to automate the system and prevent over pressurization of the tank.



Floc Mixing Tank



SCREW FEEDER CONTROL PANEL Quantity: One (1) Power Supply 480V/3Ø/60Hz

Scope includes: 1. The PLC Panel is NEMA4X, with Allen Bradley PLC and Panelview HMI touchscreen

controls the system. PLC includes operating program made in RSLogix5000; The PLC Panel shall be used to directly control and power Screw Press and all the feed equipment including: One (1) Sludge Feed Pump One (1) Dewatering Polymer Mixing System (via Polymer Mixing System Control

Panel). One (1) Sludge Flocculation Tank

Control Panel



TEST DATA SUMMARY SCREW PRESS NOTES: During the pilot test, Schwing Bioset collected samples and provided testing. The Sugar Creek WWTP personnel also collected and analyzed samples. The polymer used was the Ashland Praestol K260 FL, which is a cationic polymer. This polymer was confirmed through jar testing to be the best polymer for this demo and was the only one used. This polymer is also used elsewhere at the district which provides ease of availability. As noted above, the Screw Press model used in the pilot test is the FSP 600 unit, which is a full scale unit. Due to the residence time within the Screw Press, any changes made to polymer, pressure or feed conditions take a considerable amount of time to be witnessed at the discharge. While this allows for fewer adjustments during a given operating day, Schwing Bioset believes the benefit of using a full size unit and, therefore, not having to scale the results like with a small scale unit, is far more beneficial than having a greater number of operational changes made per operating day with a smaller unit and then having to attempt to scale those results. The demo results in this report will be broken into two sections. Most of the results that will be discussed will be concerning the screw press. The goal for the first week is to optimize operating conditions for the screw press and once determined, ramp up the throughput to be able to provide enough material for the Bioset equipment to operate effectively. These two (2) demo units were not originally designed to run together and as a result, the Bioset System (capable of processing up to 35 gpm of dewatered sludge cake) was oversized relative to the screw press. Discussion will take place about the Bioset operation in a separate section, however, most of the results for testing were done by Springfield personnel and testing completed in their lab or at an accredited outside lab. Once we receive the results from their testing, we will amend the report to include the data. The second week will be to maintain consistent operation of the screw press and allow data to be taken over a longer period of time to show how consistent the screw press operation is from week to week. Most of the focus of the second week is to monitor the Bioset operation and for Springfield personnel to obtain samples for pH testing and fecal coliform testing. The original goal of the Bioset testing was to run at standard EPA time vs temperature protocol that would have the Bioset operation run at 158 F with a dwell time of 30 minutes. That would be followed up with the EPA PFRP protocol to have the Bioset operation run at 131 F with a dwell time of 40 minutes. If possible, since the Bioset operation can be used to produce Class B with a reduced lime dosage, a lower lime dosage would be used to produce a Class B end product for evaluation. It was decided that there was not enough time to do the last test protocol. As mentioned earlier, due to over sizing of the Bioset System (specifically an oversized reactor) normal retention time of 60 min would be amplified to 180 min or longer. This will make it difficult to monitor a difference between standard EPA protocol and the EPA PFRP protocol. It was determined that we would monitor temperatures in the reactor to make sure we would meet the EPA PFRP protocol of a minimum temperature of 131F for 40 minutes and would monitor



the total volume of material processed through the Bioset system over the entire time and determine the average amount of lime used over that time frame. The end product of the Bioset system would be segregated in piles in adjacent drying beds to monitor pH over a 30 day window to determine stability of the end product, and monitor solids content as the material would dry over time. Testing for pathogen regrowth would be done as well by Springfield personnel. Tuesday, June 18th : The pilot unit was connected to a feed line pulling from the holding tank next to the unit. The plant utilizes several basins and decants through 3 basins and ends up around 1.5% solids in the final basin. Based on previous demos running Waste Activated Sludge, we started with 30 lbs active polymer/dry ton. The unit was then filled and the pilot started. The objective for Tuesday was to run the unit at a reduced rate and to set the conditions for the formation of a sturdy floc. Since the screw press capacity is based on solids loading, the actual percent solids being fed to the operation was measured to determine the proper initial flow rate for the pilot test. It was determined that the incoming solids content was 1.85%, which was consistent with normal day to day operations. The flow rate was initially set at 11.7 gpm with an active polymer rate of 30 lbs/ dry ton. The high polymer dosage was used in order to assist with formation of a sturdy floc. As the pilot unit operation reached a steady state condition, the cake dryness improved as well as the capture rate, which was greater than 98% and, at times, close to 100%. The results of the pilot this day were as follows:

Time 11:00 13:30 14:30 Polymer K260FL K260FL K260FL

Feed Sludge DS 1.85 1.85 1.85 Flow GPM 11.7 13 26

Lbs Active Polymer /DS 30 28 28 Rapid Dry Cake % 31.08 30.67 n/a

% Utilization 27%

30.0% 61.0%

Wednesday, June 19th : The objective for Wednesday was to collect dewaterability and solids capture data for the press while running at the same flow rate as the day before and to make sure we could achieve consistent results with the polymer dosage. The flow rate was maintained at 26 gpm and the polymer dosage rate decreased throughout the day. Once we were comfortable running around design level flow rates, we increased the flow rate up to 100%



utilization of the machine solids loading. We knew that to achieve enough solids to allow the adjoining Bioset equipment to run effectively, we would need to run at higher flow rates. The results of the pilot this day were as follows:

Time 08:00 09:10 10:05 11:05 12:05 13:15 14:15 Polymer K260FL K260FL K260FL K260FL K260FL K260FL K260FL

Feed Sludge

DS

1.75 1.75 1.80 1.80 1.80 1.80 1.80

Flow GPM

26 26 26 26 26 44 44

Lbs Active Polymer

/DS

30 28 26 26 26 26 26

Rapid Dry

Cake %

32.34 29.54 28.95 29.16 31.90 30.66 30.61

% Utilization 61.0% 61.0% 59.0% 59.0% 59.0% 100.0% 100.0%

Thursday, June 20th : The goal for Thursday was to maintain the incoming flow rate at 100% of maximum utilization and to evaluate the results of this high throughput while reducing the polymer levels and to evaluate the effects of reducing the polymer dosage rate. The flow rate was maintained at 45 gpm and the polymer dosage rate decreased throughout the day, dropping the dosage rate 2 lbs/dry ton on the hour until the optimum level could be determined. It appears that the lowest polymer dosage rate that will provide satisfactory dewatered cake dryness is 14 lbs active polymer/dry ton. The incoming solids content was again measured and determined to be 1.80%, similar to the day before and was consistent throughout the day. At the end of the day, we increased the flow rate to give higher solids to the Bioset system.



The results for today’s pilot are as follows:

Time 08:15 09:15 10:15 11:15 12:15 13:15 14:15 14:30 Polymer K260FL K260FL K260FL K260FL K260FL K260FL K260FL K260FL Feed Sludge DS

1.80 1.80 1.80 1.80 1.80 1.80 1.80 1.80

Flow GPM

45 45 45 45 45 45 45 60

Lbs Active Polymer/DS

24 22 20 18 16 14 12 14

Rapid Dry Cake %

33.39 30.61 29.44 29.19 29.04 28.34 Lost Floc

30.64

% Utilization

100% 100% 100% 100% 100% 100% 100% 137%

Friday, June 21st : The goal for Friday was to maintain the incoming flow rate at 137% of maximum utilization and to evaluate the results of this high throughput. The flow rate was maintained at 60 gpm throughout the day. The demo was concluded early this day due to travel requirements. The incoming solids content was again measured and determined to be 1.80%, similar to the day before and was consistent throughout the day. The cleaning cycle was run at the end of the day and the screw press housing washed off with a hose. No other cleanout was required for shutdown and startup on Monday after a weekend shutdown will be shown to be an easy transition.

The results for today’s pilot are as follows: Time 07:30 10:30

Polymer K260FL K260FL Feed Sludge DS 1.80 1.80 Flow GPM 60 60

Lbs Active Polymer/DS 14 14 Rapid Dry Cake % 31.54 31.83

% Utilization 137% 137%



Material at approximately 30% dry solids content

Filtrate Capture - >98%

Monday, June 24th : The ease of startup after a weekend shutdown was monitored. All that was required was to turn the feed pump on, adjust the polymer level, and test the incoming solids, and start up the machine. The goal for Monday was to maintain the incoming flow rate as



close to 137% of maximum utilization based on the previous week throughput and to evaluate the results of this high throughput. The incoming solids content was again measured and determined to be 1.40%, which was lower than last week. We started the equipment assuming that the incoming solids were like the week before at 1.80% and started the flow rate where we had left off on Friday. After we determined the lower incoming solids, we increased the flow rate to maintain the same solids output for feeding the Bioset system.





Tuesday, June 25th : The goal for Tuesday was to maintain the incoming flow rate at 133% of maximum utilization and to evaluate the results of this high throughput. The incoming solids content was again measured and determined to be 1.40%. Since the goal is to monitor consistency of operation and feed solids to the Bioset system, the goal was to continue monitoring output of the machine over the day.

The results for today’s pilot are as follows: Time 07:30 10:00 12:00 14:00

Polymer K260FL K260FL K260FL K260FL Feed Sludge DS 1.40 1.40 1.40 1.40 Flow GPM 75 75 75 75

Lbs Active Polymer/DS

14 14 14 14

Rapid Dry Cake %

28.28 29.70 29.97 29.03

% Utilization 133% 133% 133% 133%



Wednesday, June 26th : The goal for Wednesday was to increase the incoming flow rate to 141% of maximum utilization and to evaluate the results of this high throughput. The incoming solids content was again measured and determined to be 1.49%. Since the goal is to monitor consistency of operation and feed solids to the Bioset system, the goal was to continue monitoring output of the machine over the day. We had to stop operations for almost 2 hours due to severe weather so we had fewer data points to monitor today.

The results for today’s pilot are as follows: Time 07:30 10:30 14:00

Polymer K260FL K260FL K260FL Feed Sludge DS 1.49 1.49 1.49 Flow GPM 75 75 75

Lbs Active Polymer/DS 14 14 14 Rapid Dry Cake % 30.04 32.08 32.00

% Utilization 141% 141% 141%

Thursday, June 27th : The goal for Thursday was to increase the incoming flow rate to above 150% of maximum utilization and finally to 200% of maximum utilization for a short period of time to determine the viability of the machine if it ever needed to be run at very high throughputs and to evaluate the results of this high throughput. The incoming solids content was again measured and determined to be 1.61%. Since the goal is to monitor consistency of operation and feed solids to the Bioset system, the goal was to continue monitoring output of the machine over the day. The plan was to stop screw press operations when the lime ran out in the Bioset system. Operations ceased just before noon and the demo was stopped and breakdown and cleanup of the equipment followed.







Bioset Process – Class A Stabilization Process

The Bioset system shall receive dewatered cake from the above Screw Press for this facility. The system thoroughly mixes approximately 9% by volume of quicklime and 0.06% by volume of sulfamic acid with dewatered biosolids in the Twin Screw mixer. The mixture is pumped via Schwing Bioset Piston Pump into the Bioset reactor. Previously operating under the time/temperature formula of option 1B of the 503 rule for pathogen destruction (70C/30minutes), on August 16, 2011 the Bioset process was accepted as a PFRP process and can now operate at 55C for 40 minutes. This reduces the operating costs by as much as 30%. A copy of this approval letter is included for your reference. The chemical reaction releases 480 btu’s/lb of heat from the lime and 865 btu’s/lb of heat from the acid. The high amount of lime also creates sustained elevated pH levels in the material. Please refer to the process flow diagram below:

Throughout the stabilization process, ammonia gas is released from the reaction, contained in the system, and removed at the material discharge point using a 500 CFM water scrubber. The Bioset system generates a very minimal amount of residuals from the process. The diluted ammonia from the 500 CFM ammonia scrubber that uses approximately 8 gpm of water is the only by-product. This dilute ammonia solution will be sent back to the plant head works. Keeping the mixing and reaction process enclosed has the added benefit of eliminating many of the common issues found with lime stabilization. No lime dust is emitted at any point in the process and the only location for odors to escape is at the reactor discharge where they are easily captured by our scrubber.



Biosolids Processing Equipment Operations for this Demo on Average Process Material Description: Municipal Sewage Biosolids WAS Process Material Solids Content: ≈ 29% Total Dry Solids Process Material Density: 65 lb/ft3 Design Biosolids Processing Rate: ≈ 1800 wet-lb/hr Estimated Lime Feed Rate: 162 lb/hr (9% of wet sludge cake mass) Estimated Sulfamic Acid Feed Rate: 1 lb/hr (0.06% of wet sludge cake mass) Pump Flowrate (includes added chemicals): 1965 wet-lb/hour (3.95 GPM)

A. Lime Silo & Feeder – Provides storage and metering of quicklime (calcium oxide) into the

Twin-Screw Mixer inlet hopper. B. Sulfamic Acid Feeder – Provides storage and accurate metering of dry sulfamic acid into the

Twin-Screw Mixer inlet hopper. C. Collection Screw Conveyor – Receives Biosolids from Screw Press and transfers material to

the Twin-Screw Mixer inlet hopper. D. Twin-Screw Mixer – The Twin-Screw Mixer allows for the blending of the sludge, lime, and

acid into a homogenous mixture. It also helps feed this mixture into the Reactor Feed Pump. E. Reactor Feed Pump – The Reactor Feed pump moves the sludge/lime/acid mixture through

the Reactor Vessel. F. Hydraulic Power Unit - Reactor Feed Pump – The Hydraulic Power Unit drives the Reactor

Feed Pump. G. Reactor Vessel – The insulated plug-flow reactor is used to achieve the required time and

temperature to meet EPA regulations for Class A/EQ biosolids. H. Ammonia Scrubber – Captures and treats ammonia emissions at the reactor discharge outlet. I. Control Panel - Bioset Process – Used to operate and monitor all Bioset System equipment

and instrumentation. A. LIME SILO & FEEDER Quantity: One (1) Material of Construction: A36 carbon steel Material Storage: Quicklime (Calcium Oxide) Design Storage Capacity: 1.5 tons Lime Motor Size – Lime Discharger: 0.5 HP; 460V / 3 / 60Hz

B. SULFAMIC ACID FEEDER Quantity: One (1) Motor size: 1/4 HP, 90VDC



Material of Construction: 304 Stainless Steel Material Storage: Sulfamic Acid Design Storage Capacity: 50 lb bag storage

C. COLLECTION SCREW CONVEYOR Quantity: One (1) Material of Construction: A36 Carbon Steel Auger Diameter: 12 inches Auger Length: Approximately 20 feet Motor size: 5 HP, 480V / 3 / 60Hz

D. TWIN-SCREW MIXER Quantity: One (1) Model: SD 350 Material of Construction: A36 Carbon Steel Inlet Opening Length: 60 inches Inlet Opening Width: 24 inches Motor Size – Twin-Screw Mixer: 7.5 HP; 460V / 3 / 60Hz

E. REACTOR FEED PUMP Quantity: One (1) Model: KSP 12 V(K)L Design Flowrate: 12 - 100 LPM (3 - 25 GPM) Pumping Stroke Length: 500 mm (19.7 inches) Diameter - Material (Pumping) Cylinders: 180 mm (7 inches) Diameter - Differential (Hydraulic) Cylinders: 90 mm (3.5 inches) Cylinder Ratio: 4.0:1 Diameter - Suction Poppets: 210 mm (8.2 inches) Diameter – Discharge Poppets: 150 mm (5.9 inches) Diameter – Discharge Outlet: 180 mm (7 inches)

F. REACTOR FEED PUMP HYDRAULIC POWER UNIT Quantity: One (1) Model: 110-25 HP Reservoir Size: 110 liters (30 gallons) Motor Size: 18.5 kW (25 HP) Hydraulic Pump (Sludge Pump): Rexroth A11VO40EP2D Electrical Service: 460 Volt / 3 Phase / 60 Hertz



G. REACTOR VESSEL Quantity: One (1) Material of construction: A36 carbon steel Diameter: 1.2m (48 inches) Length: 3m (10 feet) nominal Design Residence Time: 60 minutes

H. AMMONIA SCRUBBER Quantity: One (1) Motor Size – Ammonia Scrubber: 1 HP; 460V / 3 / 60Hz

I. CONTROL PANEL – BIOSET PROCESS Quantity: One (1)

The following shall be controlled/adjusted/monitored using the touchscreen interface:

LIME FEED RATE INTO THE MIXER HOPPER. In Automatic Mode, the lime feed rate shall be adjusted as a fixed percentage of the sludge cake feed rate, based on Reactor Vessel temperature measurements.

SULFAMIC ACID FEED RATE INTO THE MIXER HOPPER. In Automatic Mode, sulfamic acid feed rate shall be a fixed percentage of the lime feed rate.

PUMPING RATE FOR THE REACTOR FEED PUMP. OPERATION OF THE AMMONIA SCRUBBER. In Automatic Mode, the Ammonia

Scrubber shall run whenever the Reactor Feed Pump is in operation.

TEST DATA SUMMARY BIOSET OPERATIONS

As mentioned earlier in the report, the main Bioset data was captured by the Springfield personnel. However, we did monitor the incoming temperature of the material to dewater and it was determined to be 82.2 F consistently. Based on our formulas to determine the amount of chemicals required for PFRP with incoming solids at 29%, it was determined that the lime and acid amounts required to get to 131F would be at 8.09% of the incoming product. If we were to run at the Standard EPA Time/Temperature protocol, with the same incoming temperature and solids, it was determined that the lime and acid amounts required to get to 158F would be at



12.82% of the incoming product. Since we had varying amounts of incoming quantities of solids, and a range of incoming solids % from 28 to 33% solids, it was difficult to manage the exact amount of lime addition during the duration of the demo. We did monitor temperatures through the reactor and maintained the temperatures consistently above the PFRP required temperature of 131F. At times we were able to obtain temperatures above 158F as shown on the screenshot below. There would be some variability in end product during the initial demo, but from Tuesday, June 25 onward, we would be very comfortable in saying that all material coming out of the Bioset operation would meet Class A material.

Screenshot of Bioset Control Panel during Demo

Due to the incoming solids having at least 29% solids content, we did monitor final solids content coming from the reactor. We took one on Friday, June 21st and the reading was 40.7%. We took one on Wednesday, June 26th and the reading was 40.72%. We took two readings on Thursday, June 27th and the readings were 43.42% and 42.79%. During the entire time of running the Bioset operation, we monitored the number of gallons that were pumped through the system with our Sludge Flow Measurement System. We verified that we pumped 5368 gallons of dewatered solids and chemicals. That calculates out to 44,769 pounds of total material. We know that we used ≈ 6000 pounds of quicklime as we used 3 bags total during the demo. We also used less than a 50 pound bag of sulfamic acid during the demo, estimated to be about 30 pounds of usage. If you average the chemical usage over the entire demo, it would show that we used on average 8.66% lime and acid of the incoming product, which corresponds well to our calculations.



For normal production, particularly during the winter months, if the incoming sludge temperature would drop down to 55F, then the chemical usage would spike up to around 12.82% of the incoming product to meet the EPA PFRP protocol. There has been interest to determine the cost savings that would be gained by just using the Bioset process to meet Class B. During the summer months, based on the results that we saw in our demo of just using 8.66% chemicals, the cost savings to produce Class B may not be warranted based on the advantages of producing a Class A product from a disposal standpoint. The testing could be more easily determined in a production environment after the Bioset system is installed. Springfield personnel will be providing their own test results to be added to this report. Once received, we will amend the report and include them for a final report.

Bioset End Product at ≈ 41% Solids

Bioset End Product to be monitored for 30 days or longer at Sugar Creek



CONCLUSIONS The pilot was able to demonstrate that the Schwing Bioset Screw Press is capable of dewatering the waste activated sludge at the Springfield Sugar Creek WWTP. The pilot unit was the Schwing Bioset Model FSP600 (an actual full scale unit). While processing between approximately 240 and 789 dry lbs per hour, the unit was able to produce cake consistently on average of 30.41% solids. To keep up with the demand of the Bioset operation, we routinely ran at 135% of solids loading capacity and still obtained results around 30% solids. The solids capture was generally above 94% even at the higher throughputs. We determined that the polymer chosen, the Ashland Praestol K260 FL performed very well. Due to the extended run time of two weeks, we were able to determine an optimum polymer dosage of 14 lbs/dry ton of active polymer and obtain very consistent results in an extended time frame. The Bioset operation performed very well and was able to run on average final solids of around 40% or higher. The average amount of chemicals used during the trial was 8.66% of the incoming product and was consistent with our calculations. Once we receive the final results from the Springfield personnel, we will add the results to this report. Springfield personnel will also monitor the end product piles onsite at the Sugar Creek plant for the next 30 days and potentially longer. They will provide results to us and we will publish those results once obtained.

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