LANTHANUM CARBONATE CENTRIFUGE TRIALOCTOBER 2014

PurposeThe purpose of the Lanthanum carbonate centrifuge trial was to determine the following criteria:

Can we successfully centrifuge Lanthanum carbonate Can the centrifuged material meet specifications Can we achieve feed rates conducive to reaching Phase I goals for Lanthanum Oxide. Phase I Rates are 4,416 MT/year

or 14.2 MT/day of La Oxide. This equates to a centrifuge rate of 6.18 Kg/min of La Carbonate for one centrifuge and would require 4 centrifuges of the same capacity currently being used (assuming 300 Kg per discharge with a cycle time of 48.5 min per centrifuge).

DescriptionLanthanum Carbonate slurry was produced from the Lanthanum Precips into Lanthanum Surge Tank, TK131. This slurry was then transferred to the Centrifuge Feed Tank, F65-TK130, using one of the ODS pumps at the bottom of TK131. The Lanthanum Carbonate slurry in F65-TK130 was then circulated in the feed header for the centrifuges and fed only to Centrifuge 160, F65-CENH160. The plan for the trial included using Centrifuge 160, F65-CENH160, so that only one centrifuge would be contaminated with Lanthanum. The discharge spool piece on CENH160 was removed and a modified spool piece was installed to allow the filtrate and wash water to be sent to the tote for collection. The tote was then pumped back to F60-TK131 as needed to keep the centrifuge running. This filtrate and wash water collected in F60-TK131 was pumped to the lanthanum thickeners.

There were two separate Lanthanum centrifuge trials performed. The first trial was performed using a 20 micron cloth and the second trial was performed using a 30 micron cloth. Between the two trials, Didy Oxalate clean up material was re-slurried and transferred into the centrifuge feed tank and then run through Centrifuge 160.

Samples were taken of each cake discharge and sent to the lab for PSD, Na, Cl and tREO analyses. Samples were also taken of the water wash for Na analysis.

Below is a flow diagram of the Centrifuge trial.

A typical centrifuge cycle consists of four phases. These phases are the Loading Phase, the Washing Phase, the Spinning Phase and the Discharge Phase. All four phases contribute to the overall cycle time of one batch of material through the centrifuge.

Loading Phase – This phase has the potential to contribute the most time to the overall cycle time. The centrifuges in use are currently loaded by cake thickness. The cake is loaded into the centrifuge until the cake sensor senses that the cake has built to a layer matching the desired thickness setting set by the operator. The cake sensor will initiate a drain step and allow the centrifuge to re-load more cake after the draining step. This draining and re-loading may occur numerous times until the basket is full and the centrifuge moves to the Washing Phase.

Washing Phase – This phase will always contribute the same amount of time to each cycle that has been preset by the operator. The water wash is done with hot RO water. A spray bar inside the centrifuge is equipped with 7 spray nozzles that are adjusted to cover the entire cake in the basket as it spins past the spray bar. This creates a plug flow of wash water through the cake to the discharge of the centrifuge.

Spinning Phase – This phase will always contribute the same amount of time to each cycle that has been preset by the operator. The spinning phase is usually performed at a higher speed and removes the free water that is left in the cake from the Washing Phase. The time for the spinning is determined to achieve a moisture level on the discharged cake.

Discharge Phase – This Phase discharges the cake from the centrifuge and contributes the least amount of time to the overall cycle. This phase moves the cutting knife into the cake and removes it from the basket. The cake falls from the knife blade into an internal hopper that feeds and auger that moves the material out of the centrifuge onto a conveyor that moves the material into a sling.

For Trial 1, the Loading Phase accounted for 75% of the overall time per centrifuge cycle. For Trial 2, the Loading Phase accounted for 71 % of the overall time per centrifuge cycle. Each Cycle and its parameters can be seen in the tables in the Appendix. White boxes outlined in red indicate a change to the parameter for that particular cycle.

CENTRIFUGE TRIALS

TRIAL 1

Trial 1 of the Lanthanum Carbonate Centrifuge trials involved filtering approximately 8,400 gallons of La Carbonate slurry through centrifuge 160. This run required nine centrifuge cycles which yielded 2,245 Kg of La Carbonate solids that had an average moisture content of 25 % free moisture. The 20 micron cloth was very good at capturing the solids. The filtrate was visually very clear (no visible suspended solids). However, this cloth limited the feed rate to less than 30 gpm and was hard for the filtrate and wash water to pass through during the loading and washing phases. This tight cloth was causing the filtrate to puddle on top of the cake and this liquid would build up and would activate the cake sensor sending the centrifuge into numerous drains per cycle. The result of this was long loading times.

The first cycle was fed at 42 gpm and discharged a visually cloudy filtrate. Cycle 2 was fed at 30 gpm with visually clear filtrate. Cycles 3 through 9 were fed at 28 gpm with visually clear filtrate. The average loading phase time was 72 minutes with an average total cycle time of 96 minutes. The average cake discharge weight for the 9 cycles was 241 Kg. This led to an average centrifuge rate of 2.50 Kg/min of La Carbonate for Trial 1 which is 40.6% of Phase I rates on an Oxide basis for one centrifuge. The best centrifuge cycle during this trial achieved a centrifuge rate of 2.95 Kg/min of La Carbonate which is 47.7% of Phase I rates on an Oxide basis for one centrifuge. See the graph below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7 CYCLE 8 CYCLE 90.00

1.00

2.00

3.00

4.00

5.00

6.00

7.00

TRIAL 1 CENTRIFUGE RATE FOR ONE CENTRIFUGE

PHASE I RATEACTUAL RATE

KG/M

IN

The Samples taken for the cake discharges in Trial 1 were analyzed for %LOI, %H2O, %Cl(w/w), %Na2O(w/w) and tREO. This data can be seen the Table 1 at the end of this section.

The %Na/tREO data was well below the specification of 0.25% for the first 8 cycles with the ninth cycle being just slightly higher than specification. The increase in the Na content through the last 3 cycles is unexplainable because cycles 6 through 9 were run with the same parameters. See the graph below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7 CYCLE 8 CYCLE 90.0000

0.0500

0.1000

0.1500

0.2000

0.2500

0.3000

% Na2O/Treo TRIAL 1

Na2OSPEC

% N

a2O

When the conductivity reading and the analytical results for the %Na content of the filtrate for cycle 9 are plotted with the analytical data for the cake, the indication is that the %Na content of the cake for cycle 9 would have been below the specification. This could be an anomaly with the analytical result for the cake from cycle 9. Another theory for this high Na reading for cycle 9 could be due to a non-soluble Na crystalline structure that may have been formed in the Precip process. See the graph below.

CYCLE 1

CYCLE 2

CYCLE 3

CYCLE 4

CYCLE 5

CYCLE 6

CYCLE 7

CYCLE 8

CYCLE 9

0.0000

0.0500

0.1000

0.1500

0.2000

0.2500

0.3000

0

50

100

150

200

250

% Na2O/Treo for Cake and Filtrate

Na2O CAKESPECCONDUCTIVITY Filtrate Na Reading Filtrate

% N

a2O

The %Cl/tREO was well below the Grace specification of 0.6% for all 9 centrifuge cycles. With exception to cycle 6 and cycle 9, the remaining 7 cycles for Trial 1 met the specification of 0.20% maximum indicated for BASF. See the graph below

CYCLE 1

CYCLE 2

CYCLE 3

CYCLE 4

CYCLE 5

CYCLE 6

CYCLE 7

CYCLE 8

CYCLE 9

0.0000

0.1000

0.2000

0.3000

0.4000

0.5000

0.6000

0.7000

% CHLORIDE/tREO

CHLORIDEGrace specBASF spec (max)

% C

HLO

RIDE

TRIAL 2

Trial 2 of the Lanthanum Carbonate Centrifuge trials involved filtering approximately 8,700 gallons of La Carbonate slurry through centrifuge 160. This run required seven centrifuge cycles which yielded 1,762 Kg of La Carbonate solids that had an average moisture content of 29 % free moisture. The 30 micron cloth was as effective as the 20 micron cloth at capturing the solids as this filtrate was also very clear with no visible suspended solids. The 30 micron cloth was not as limiting on the feed rate as the 20 micron cloth. Feed rates with the 30 micron cloth were 75 % better than the feed rates with the 20 micron cloth. Even with better feed rates, this cloth was still causing the filtrate to puddle on top of the cake and this liquid would build up and would activate the cake sensor sending the centrifuge into numerous drains per cycle. The loading times for this trial were 19.4% shorter than the trial with the 20 micron cloth.

The first cycle was fed at 42 gpm and all other cycles were fed at 49 gpm. The filtrate remained visually clear with 49 gpm being the maximum feed rate achievable. The average loading phase time was 58 minutes with an average total cycle time of 82 minutes. The average cake discharge weight for the 7 cycles was 252 Kg. This led to an average centrifuge rate of 3.08 Kg/min of La Carbonate for Trial 2 which is 49.7 % of Phase I rates on an Oxide basis for one centrifuge. The best centrifuge cycle during this trial achieved a centrifuge rate of 3.79 Kg/min of La Carbonate which is 61.3 % of Phase I rates on an Oxide basis for one centrifuge. Attempts to change the parameters to achieve better centrifuge rates were unsuccessful and led to the decline in the centrifuge rates per cycle. See the graph below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 70.00

1.00

2.00

3.00

4.00

5.00

6.00

7.00

TRIAL 2 CENTRIFUGE RATE FOR ONE CENTRIFUGE

PHASE I RATEACTUAL RATE

KG/M

IN

The Samples taken for the cake discharges in Trial 2 were analyzed for %LOI, %H2O, %Cl(w/w), %Na2O(w/w) and tREO. This data can be seen the Table 2 at the end of this section.

The %Na/tREO data for Trial 2 was well below the specification of 0.25% for all the cycles with the exception of the second centrifuge cycle. The increase in the Na content for the second cycle was due to the Centrifuge feed valve leaking through and allowing slurry to enter the centrifuge during the wash and spinning steps. A hand valve was closed at the end of the loading phase for all subsequent cycles to prevent slurry from entering the centrifuge during the Wash and Spinning phases. See the graph below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 70.000

0.100

0.200

0.300

0.400

0.500

0.600

0.700

0.800

0.900

% Na2O/Treo TRIAL 2

Na2OSPEC

% N

a2O

Feed valve leak-ing through

The %Cl/tREO was well below the Grace specification of 0.60 % for all centrifuge cycles except cycle 2. The BASF specification of 0.20 % maximum was achieved by the remaining cycles. See the graph below

CYCLE 1

CYCLE 2

CYCLE 3

CYCLE 4

CYCLE 5

CYCLE 6

CYCLE 7

CYCLE 8

CYCLE 9

0.000

0.200

0.400

0.600

0.800

1.000

1.200

% CHLORIDE/tREO

CHLORIDEGrace specBASF spec (max)

% C

HLO

RIDE

Feed valve leaking through

TABLE 1:

% LOI % tREO (100-LOI) %H2O %(w/w) Cl %(w/w)Na2O %Cl/tREO %Na/tREONR-0043-141009 LA CENT CAKE #1 55.2 44.8 23.4 0.026 0.005 0.058 0.012NR-0043-141008 LA CARB CYCLE 2 CAKE 57.2 42.78 30.9 0.003 0.028 0.007 0.065NR-0043-141008 LA CARB CYCLE 3 CAKE 57.4 42.61 31.3 0.042 0.016 0.099 0.038NR-0043-141010 LA CENT CAKE 4 56.8 43.24 26.8 0.029 0.009 0.067 0.020NR-0043-141010 LA CENT CAKE 5 61.9 38.06 36.3 0.033 0.021 0.087 0.054NR-0043-141010 LA CENT CAKE 6 58.6 41.44 29.3 0.139 0.010 0.335 0.023NR-0043-141010 LA CENT CAKE 7 60.3 39.69 33.3 0.045 0.045 0.113 0.114NR-0043-141010 LA CENT CAKE 8 58.8 41.25 28.1 0.014 0.077 0.033 0.187NR-0043-141010 LA CENT CAKE 9 57.8 42.25 25.4 0.145 0.120 0.343 0.284

TABLE 1 -- Solids Analyses Trial 1

TABLE 2:

% LOI %H2O % tREO (100-LOI) %(w/w) Cl %(w/w)Na2O %Cl/tREO %Na2O/tREONR-0043-CENT CAKE 2.1 54.9 30.1 45.1 0.048 0.020 0.106 0.044NR-0043-CENT CAKE 2.2 57.5 40.5 42.5 0.484 0.330 1.140 0.777NR-0043-CENT CAKE 2.3 56.6 39.1 43.4 0.029 0.016 0.067 0.037NR-0043-CENT CAKE 2.4 54.3 35.9 45.7 0.068 0.019 0.149 0.042NR-0043-CENT CAKE 2.5 53.8 35.2 46.2 0.085 0.048 0.184 0.103NR-0043-CENT CAKE 2.6 51.9 32.5 48.1 0.094 0.037 0.195 0.077NR-0043-CENT CAKE 2.7 52.6 33.5 47.4 0.027 0.011 0.058 0.022

Table 2 -- Solids Analyses Trial 2

TRIAL COMPARISON

The table below shows the comparison of the data between the two centrifuge trials.

CLOTH SIZE

(MICRON)

SLURRY FEED % TSS

FEED RATES (GPM)

TOTAL FILTRATE FED (GAL)

TOTAL CAKE

DROPPED (KG)

AVG CYCLE TIME (MIN)

AVG WEIGHT DROPPED PER CYCLE

(KG)

AVG MOISTURE

CONTENT (%)AVG

%Cl/tREOAVG

%Na2O/tREO

AVG CENT RATE

(KG/MIN)

PERCENT OF PHASE

I RATE (%)

TRIAL 1 20 10.6 28 8400 2245.5 96 241 25.2 0.127 0.089 2.50 40.6TRIAL 2 30 16.8 49 8700 1762 82 252 29.4 0.271 0.157 3.08 49.7

The centrifuge rate of both Trials compared to Phase I rates is shown below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7 CYCLE 8 CYCLE 90.00

1.00

2.00

3.00

4.00

5.00

6.00

7.00TRIAL 1 & 2 CENTRIFUGE RATE FOR ONE CENTRIFUGE

PHASE I RATE TRIAL 1 20 micron TRIAL 2 30 micron

KG/M

IN

Both of the centrifuge trials produced Lanthanum Carbonate cake that was below the percent sodium specification of 0.25%Na/tREO.Cycle 2 on Trial 2 was above the specification due to the centrifuge feed valve leaking slurry into the centrifuge during the Wash and Spinning Phases. Cycle 9 on Trial 1 was slightly above the specification for %Na with no known explanation. The conductivity readings that were taken on the wash filtrate along with the analysis from the lab would indicate that the %Na on cycle 9 would have been expected to be below the specification. See the graph below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7 CYCLE 8 CYCLE 90

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

TRIAL 1 & 2 % Na2O/tREO

SPEC % Na2O/tREO TRIAL 1 % Na2O/tREO TRIAL 2

% N

a2O

Feed valve leaking through

Both of the centrifuge trials produced Lanthanum Carbonate cake that was below the Grace specification of 0.6 % Cl/tREO. Cycle 2 for Trial 2 was above this specification of 0.6% Cl due to the centrifuge feed valve leaking slurry into the centrifuge while performing the Wash and Spinning Phases. For the total of 16 cycles, 13 out of 16 cycles (or 81.25 %) were below the BASF maximum specification of 0.20 % Cl/tREO. See the graph below.

CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7 CYCLE 8 CYCLE 90

0.2

0.4

0.6

0.8

1

1.2TRIAL 1 & 2 % CHLORIDE/tREO

Grace spec BASF spec (max) % CHLORIDE TRIAL 1 % CHLORIDE TRIAL 2

% C

HLO

RIDE

Feed valve leaking through

SUMMARY AND CONCLUSIONS

SUMMARYWith the assumption of 300 Kg of Lanthanum Carbonate cake being discharged at each centrifuge cycle and the use of the current size of centrifuge, a cycle time of approximately 48 minutes would be required per centrifuge and four centrifuges would be required to meet Phase I rates for La Oxide. This performance would equate to a centrifuge rate of 6.18 kg/min of La Carbonate per centrifuge. In both centrifuge trials, the centrifuge rates for Trial 1 and Trial 2 were 40.6 % and 49.7 % of Phase I rates for four centrifuges, respectively. This improved performance toward Phase I rates for Trial 2 is due to the decrease in the loading times which is attributed to the larger 30 micron cloth that was used for Trial 2. However, the Lanthanum Carbonate cake produced during these two trials had acceptable free moisture content and the quality was well within specifications for Na and Cl. The spinning time during the Spinning Phase was decreased after the first and second cycle of Trial 1 to increase the moisture in the cake that was being discharged from the centrifuge. The first two cake discharges from Trial 1 were very dusty when entering the sling from the conveyor. All of the Lanthanum Carbonate that was centrifuged during these two trials was fed to the new La Calciner and converted to La Oxide with no negative impacts during conveying or calcining of the material.

The following conclusions can be drawn from the two Lanthanum Carbonate Centrifuge Trials. Lanthanum Carbonate can be successfully centrifuged directly from the Lanthanum Carbonate Precips without

thickening of the slurry. The Na and Cl content of the centrifuged cake can be washed away in the centrifuge wash phase to meet

specifications. The centrifuged cake was averaging moisture contents of 25 to 30% and was fed into the Lanthanum calciner with no

negative issues. The ability to wash the Na and Cl out of the cake with a minimal amount of RO water would greatly reduce the

hydraulic load currently used at the Lanthanum thickeners and drum filter. This would also eliminate the use of many pieces of aged equipment and the costs associated with maintaining the equipment.

Further testing with a larger size cloth (~40 micron) in the centrifuge is recommended to see if better centrifuge rates can be achieved to reach the Phase I goals. Based on the increased centrifuge rate experienced between the 20 micron and 30 micron cloths, a significant increase in the centrifuge rate would be expected with the increased cloth size from 30 micron to 40 micron. This would require about 5-7 days of no production for the NDPR circuit to run another trial using one of the NDPR centrifuges.

The current centrifuge capacities would be expected to achieve discharge weights of La Carbonate cake on average of 300 Kg. However, the required cycle time of about 48 minutes needed to meet the Phase I rates may not be feasible. For Lanthanum Carbonate, Centrifuges with a larger capacity may need to be explored to keep the number of centrifuges required and the cycle times per centrifuge to a minimum.

Subsequent to these two Lanthanum Carbonate Trials, a visit by the manufacturer of the centrifuges (ComiCondor) was made to Mountain Pass. Much was learned from the representative from ComiCondor on how to feed the centrifuges and reduce the loading times and maximize the amount of material loaded. These teachings have been applied to the centrifuge operations for NDPR with much success in achieving loading rates and cycle times congruent with Phase I rates for NDPR.

APPENDIX

TRIAL 1 CENTRIFUGE DATAcycle time CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7 CYCLE 8 CYCLE 9

Phase List Name Parameter Spec typical min.Loading P1 Basket Reading Speed(rpm) 300 300 300 500 500 500 600 600 600 600Loading P2 Loading Time(sec) 2700 25 2700 2700 2700 2700 2700 2700 2700 2700 2700Loading P3 Cake Thickness(in) 3 3 3 3 4 4 4 4 4 4Loading P4 Basket Draining Speed(rpm) 750 750 600 700 700 700 700 700 700 700Loading P5 Drain Time(sec) 60 4 60 30 30 30 30 15 15 15 15Loading P6 Basket Spinning Speed(rpm) 800 800 800 800 800 800 800 800 800 800Loading P7 Spinning Time(sec) 20 0.33 20 20 20 20 20 20 20 20 20Loading P8 Endphase Selection By ThicknessWash 1 P1 Basket Wash Speed(rpm) 800 800 800 800 800 800 800 800 800 800Wash 1 P2 Wash Time(sec) 600 10 600 600 600 600 600 600 600 600 600Wash 1 P3 Drain Time(sec) 45 0.75 45 45 45 45 45 45 45 45 45Wash 1 P4 Cake Thickness(in) 3.2 3.2 3.2 3.2 4.2 4.2 4.5 4.5 4.5 4.5Wash 1 P5 Number of Washes 1 1 1 1 1 1 1 1 1 1Wash 1 P6 Basket Spinning Speed(rpm) 1200 1200 1200 1200 1200 1200 1200 1200 1200 1200Wash 1 P7 Spinning Time(sec) 20 0.33 20 20 20 20 20 20 20 20 20Spinning P1 Basket Initial Speed(rpm) 1200 1200 1200 1200 1200 1200 1200 1200 1200 1200Spinning P2 Spinning Time(sec) 600 10 600 420 360 360 360 360 360 360 360Spinning P3 Basket Final Speed(rpm) 400 400 400 400 400 400 400 400 400 400

Discharge P1 Basket Cutting Speed(rpm) 150 150 150 150 150 150 150 150 150 150Discharge P2 Stop Knife Cutting Time(sec) --- --- --- --- --- --- --- --- --- ---

Expected Cycle Time (min) 50.4 50.4 45.4 44.4 44.4 44.4 43.4 43.4 43.4 43.4Actual Cycle Times (min) 112 80 90 93 120 104 95 96 78 96 AverageActual Loading Time(min) 85 46 60 72 97 82 76 75 55 72 Average

Feed Rate (gal/min) 45 30 28 28 28 28 28 28 28Dropped Cake Weight (Kg) 208 195 185 249.5 296 294 280 262 200 241 Average

Actual Centrifuge Rate (Kg/min) 1.86 2.44 2.06 2.68 2.47 2.83 2.95 2.73 2.56 2.50Phase I Centrifuge Rate (Kg/min) 5.37 5.37 5.37 5.37 5.37 5.37 5.37 5.37 5.37

% moisture reading 18.9 20.51 21.7 22.7 33.7 27.5 31 26.9 23.8 25 Average

Wash Water Conductivity ReadingsBeginning of Wash O/R O/R O/R O/R O/R O/R O/R O/R

Middle of Wash 3.54 264 748 382 263 156 302 197End of Wash 105.5 62 82 224 63 69 195 125

Laboratory Na Reading of WashBeginning of Wash (ppm) 46670 53340 52460 57640 58160 60780 45150

Middle of Wash (ppm) 25.9 42.7 179 97.6 104 175 108End of Wash (ppm) 88.2 15.1 115 17.6 19.1 113 59.3

%Cl/treo 0.0580 0.0070 0.0986 0.0671 0.0867 0.3354 0.1134 0.0332 0.3432 0.1270 Averagespec 0.6 0.6 0.6 0.6 0.6 0.6 0.6 0.6 0.6

BASF spec 0.15 0.15 0.15 0.15 0.15 0.15 0.15 0.15 0.15

%Na2O/treo 0.0121 0.0652 0.0375 0.0199 0.0544 0.0231 0.1141 0.1867 0.2840 0.0886 Averagespec 0.25 0.25 0.25 0.25 0.25 0.25 0.25 0.25 0.25

TRIAL 2 CENTRIFUGE DATAcycle time CYCLE 1 CYCLE 2 CYCLE 3 CYCLE 4 CYCLE 5 CYCLE 6 CYCLE 7

Phase List Name Parameter Spec Effect typical min.Loading P1 Basket Reading Speed(rpm) 300 600 600 700 700 800 700 700Loading P2 Loading Time(sec) 2700 25 2700 2700 2700 2700 2700 2700 2700Loading P3 Cake Thickness(in) 3 4 4 4 4 4 4 4Loading P4 Basket Draining Speed(rpm) 750 700 700 800 800 950 800 800Loading P5 Drain Time(sec) 60 4 15 15 15 15 10 10 10Loading P6 Basket Spinning Speed(rpm) 800 800 800 800 800 800 800 800Loading P7 Spinning Time(sec) 20 0.33 20 20 20 20 20 20 20Loading P8 Endphase Selection By ThicknessWash 1 P1 Basket Wash Speed(rpm) 800 800 800 800 800 800 800 800Wash 1 P2 Wash Time(sec) 600 10 600 720 720 720 600 600 600Wash 1 P3 Drain Time(sec) 45 0.75 45 45 45 45 45 45 45Wash 1 P4 Cake Thickness(in) 3.2 4.5 4.5 4.5 4.5 4.5 4.5 4.5Wash 1 P5 Number of Washes 1 1 1 1 1 1 1 1Wash 1 P6 Basket Spinning Speed(rpm) 1200 1200 1200 1200 1200 1200 1200 1200Wash 1 P7 Spinning Time(sec) 20 0.33 20 20 20 20 20 20 20Spinning P1 Basket Initial Speed(rpm) 1200 1200 1200 1200 1200 1200 1200 1200Spinning P2 Spinning Time(sec) 600 10 420 480 480 480 480 480 480Spinning P3 Basket Final Speed(rpm) 400 400 400 400 400 150 150 150

Discharge P1 Basket Cutting Speed(rpm) 150 150 150 150 150 150 150 150Discharge P2 Stop Knife Cutting Time(sec) --- --- --- --- --- --- --- ---

Expected Cycle Time (min) 50.4 44.4 47.4 47.4 47.4 45.1 45.1 45.1Actual Cycle Times (min) 72 75 82 84 102 78 79 82 Average

Actual Loading Time(min) 50 50 58 61 78 56 56 58 AverageFeed Rate (gal/min) 42 49 49 49 49 49 49

Dropped Cake Weight (Kg) 253 284 259 262 326 220 158 252 AverageActual Centrifuge Rate (Kg/min) 3.51 3.79 3.16 3.12 3.20 2.82 2.00 3.08Phase I Centrifuge Rate (Kg/min) 5.37 5.37 5.37 5.37 5.37 5.37 5.37

% moisture reading 27.2 36.8 36.7 25.5 28.3 26.5 24.8 29 Average

Wash Water Conductivity ReadingsBeginning of Wash N/A N/A N/A N/A N/A N/A N/A

Middle of Wash N/A N/A N/A N/A N/A N/A N/AEnd of Wash 6000 12910 161 162 215 196 167

Laboratory Na Reading of WashBeginning of Wash (ppm) N/A N/A N/A N/A N/A N/A N/A

Middle of Wash (ppm) N/A N/A N/A N/A N/A N/A N/AEnd of Wash (ppm) 1042 2646 <1.0 <1.0 <1.0 <1.0 <1.0

%Cl/treo 0.106 1.140 0.067 0.149 0.184 0.195 0.058 0.2712 Averagespec 0.6 0.6 0.6 0.6 0.6 0.6 0.6

BASF spec 0.15 0.15 0.15 0.15 0.15 0.15 0.15

%Na2O/treo 0.044 0.777 0.037 0.042 0.103 0.077 0.022 0.1574 Averagespec 0.25 0.25 0.25 0.25 0.25 0.25 0.25