Alkaline Leach Resin-in-Pulp Pilot Plant testing of Monument Valley ore

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WIN-83 Metallurgy-~w Materials' ~ 1

-T.OPICAL REPORT WIN-83

ALKALINE LEACH RESIN-IN-PULP PILOT PLAN'T TESTIN'G OF MONUMENT VALLEY ORE

By

W. D. Charle.s and R. L. Shimmin

June 1, 1958 ·

w.

D. Charles Manager

12L~

R. L. Shimmin '

~K~

C. K. McArthur Technical Director

U. S. Atomic Energy Commission Contract N'o. AT(49-6)-924

National Lead Company, Inc. Raw Materials Development .Laboratory

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ABSTRACT W:IN-83 2

-During the period of November 27, 1955 ttirough January 31, 1956, various. -portions of the Monument Valley ore, Monticello Stockpile 46, were treated in the Alkaline Leach Resin-In-Pulp ;pilot Plant a.t

Grand Junction, Colorado, to study ion exchange characteristics with a low u.ranium .to vanadium ratio in the icin exchange fe·ed. The uranium to vanadium conc·entrations were s.uch that a ratio as low as 1.5:1 was attained with no detrimental effect on the ion exchange characteristics. The report contains detailed information on grinding, leaching, sand-slime separation, ion exchange, and precipitation as related to the processing of this ore.

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TABLE OF CONTENTS

INTIWDUCTION

SUMMARY

FLOWSHEET DESCRIPTION

A• Grinding R. Leaching

C. Mill Solution Make,.up

D. Sand-Slime Separation

E. Res:in-In-Pulp

F. Precipitation and Eluant Make~up

C~

TEsT WoRK

A, Grinding

B. Leaching

C. Mill Solution Make-up

D.• Sa:nd -slime Separation

E, Resin Adsorption

F. Elution and Precipitation

METALLURGICAL BALANCE · A?PENDIX

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WIN~83 ~ 3 -4 5 7 7 7 7 9 9 10 14

14

17

18

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INTRODUCTION WIN-83

4

-Monument Valley ore, Monticello Stockpile 46, was treated in the Alkaline Leach Resit)-In~Pulp Pilot Plant at Grand Junction, Colorado', at the request of the Raw Ma.teria:ls Division of the Atomic Energy Commission. The test program was from November 27, 1955 to January

·31,

1956. Purpose of the run was to determine tlie effect, if any, ofoperating with an ion exchange feed having a uranium to vanadium ratio of approximately 1:1. The amenability of Monument Valley ore to the .Alkaline Leach RIP process was also investigated.

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SUMMARY

From November 27, 1955 through January 31, 1956, an amenability test was conducted on Monument ·valley pre in the Alkaline Leach Resin-In-Pulp Pilot Plant. Various portions of the Monument Valley Btockpile were treated in .an attempt to achieve a low uranium to vanadium ratio in the ion exchange feed, in the range .of 1:1. This

ratio wa:s not '~~ot.t.ained; however, the uran.ium to vanadium

concen-trations were such that a ratio as low as 1.5:1 was attained with no detrimental effect on the ion exchange characteristics. The

adjus.tment of the ion exchange feed pH .to a range of 10.8 J:.o 11.1

did not prevent the adsorption of vanadium but successfully shifted

the adsorption equilibrium to favor the preferential loading of uranium.

With the feed to the circuit averaging 0.239% U30a and 0.837% v 2

o

5 ,

grinding conditions were adjusted to produce a class.ifier overflow pulp averaging 18.2 per cent solids which contained 25.4 per cent plus 100-mesh and 49.8 per cent minus-200 mesh material. The ball mill thickener operated effectively with an average underflow density of 1.49 (48.8 per cent solids) and required 0.09 lb of flocculent/ton of ore. With an average leach contact time of 43 hours, a .temperature of 90°C, a pulp density of 1.49, and aeration air added for oxidation, uranium and vanadium leach extractions were 96.3 and 25.0 per cent;, respectively. Decreasing the

tempera-ture to 80°C had essentially no effect on uranium extraction; however, there was a slight decrease in vanadium extraction.

Reagent requirements for mill solution make-up based on inventory

figures were 64.4 lb Na2

cn

3 and 17.5 lb NaHC03 per ton of ore. The

reagent recovery system was not used during the test.

The sand-slime separation circuit rejected approximately 58 per

cent of the total mill feed solids as sands with a solution averaging

0.037 g U30a/l. This represented a soluble loss of 0.38 per cent

.of the uranium in the mill feed. Water requirements were 0.66 gpm/tpd

to maintain an ion exchange feed.densi'ty .<>f 1.05.

Caustic requirements for pH adjustment of the ion exchange feed were 9 lb/ton of .ore. During a period from January 3 through January 15 hydrated lime was added to the ion exchange feed for pH adjustment and found to have no effect on ion exchange recovery; however, 4.0

per cent of the

u

₃

o

_{8 in solution was precipitating in .the sand-slime}

circuit due to localized high pH values and reported in the washed sands. Lime requirements under these conditions were 15 lb/ton of or·e.

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WIN-83

6

-With an average ion exchange feed assay of 0.56 g U308 and 0.27

g

v

_{2o5 per liter, the RIP circuit was operated successfully at an}

intended resin loading of 3.4 lb

u

_{3o8/cu ft WSR.}

!/

The ion exchange

circuit was operated at a solution to resin ratio of 6:1 with seven banks on exhaustion and five .on elutlon. The average change,- over time was 4.9 hours and a recovery of 98.7 per cent was realized.

Elutions were made with 1 ~ NaCl and the pregnant eluate

precip-itated by the acidification-n~utralization procedure. Pregnant

eluates averaged 9.88 g

u

_3o8/l and reagent requirements were

6.12 lb NaCl, 1.40 lb H2so4 , and 0.31 lb MgO per pound of

u

3o8

produced. The final product averaged 70.2%

u

_{3o8 and 1.46% V205.}

The calculated over-all uranium recovery amounted to 92.9 per cent while the actual recovery based on barrel weights and assays was 90.2 per cent resulting in an unaccountable loss of 2.7 per cent. Only 0. 5 per cent of the total V 2o5 in the mill feed reported in the final product.

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.FLQWSHEET DESCRil'TION

WIN~83

7

-A description of the flowsheet and process equipment us.ed in the Alkaline Rll' 1/ Pilot Plant ha& been reported previously. 2/ The. flowsheet-is shown in Figure 1 and the process is desc'i="ibed briefly as follows:

A. Grinding

Ore received from the Feed Preparation Plant is minus 3/16-in. and is fed to a 24 x 18-in. ball '!'ill in closed circuit with a 12-in. Dorr rake classifier. Mill solution is added from a steady-head tank to maintain the pulp at the desired density for grinding.

The classifier overflow is pumped to a 12 x 8-ft thickener. The thickener overflow returns to the mill solution make-up tank which is feeding the circuit.

( B. Leaching

The underflow from the ball mill thickener goes directly to the leach circuit which consists of two 5 x 5-ft and three ~ x 4~-ft

tanks arranged in series. The tanks are insulated with Fiberglas and the pulp is heated with steam coils. Agitation is provided by a variety of high speed impellers and pulp flow from tarik to

tank is by gravity. Provisions are made to add water to mill

solution at five points to make up for evaporation losses. Aeration air is. introduced into each tank through two pipes which discharge on opposite sides of the tank at impeller height and a chemical oxidant, if needed, is added by hand to the tanks.

c. Mill Solution Make-up

Make-up of depleted mill s.olution is. a batch operation using two 10 x Bjif.t. tanks. When the tank which is receiving the overflow from the grinding circuit thickener is full, it is sampled and dry Na2co₃ and NaHC03 are added to bring the s.olution up to leaching strength. It is then put on stream feeding the circuit while the second tank is filled.

1/ Resin-In~)?ulp

'i_!

Topical Report WIN-ll, Preliminary Pilot Plant Testing of ,Resin-In-Pulp Ion Exchange of Alkaline Leach Pulps, by

ORE GRINDING

m1·~t·~·~~·~U·~J·~· ~

ADSORPTION SLI ES (To TailinGI) ION EXCHANGE

*WHEN REQUIRED Figure I

ALKALINE LEACH RIP PROCESS

DESANDING YEl-LOWCAKE PRECIPITATION :0:

'!;;!

CX>I (X)

'"'

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D. Sand-Slime Separation

WIN-83

9

-The sand-slime separation circuit consists of four rubber-covered Esperanza-type drag classifiers, the first with 10-in. flights and the other three 4-in., and two 2-in. Dorrclones connected in series. A surge tank between the discharge of the second Dorrclone and the RIP cells helps to prevent surging of the ion exchange feed.

Underflow from the grinding circu~t thickener is pumped with overflow

from the first drag classifier to the first Dorrclone. The underflow

from this cone discharges into the first classifier and the overflow is the feed for the second cone. Underflow from the second cone dis-charges, into the second classifier and the cone overflow is ion

exchange feed. Sodium hydroxide is added to the overflow from the

first cone to raise the pH of the ion exchange from 10.0 to the range of 10.8 to 11.1. Water is added to the last classifier and the sands are washed countercurrently and discharged to tails. The sand-slime separation circuit is operated to produce a minus 325-mesh

slime product of an average density of 1.05.

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-E. Resin-In-Pulp Units

The ion exchange circuit consists of 14 one-cell units or banks arranged in a cascading system with provisions made for pumping back to the first bank. Each bank contains one 17-in. basket which holds 1.1 cubic foot of wet settled resin. The baskets move up and down at the rate of ten 6;-in. s.trokes per minute while pulp or solution flows through the bank.

In general, seven banks are on the loading or adsorption cycle, six are on elution, and one bank is being prepared for the next adsorption cycle. The dilute slime product from the sand-slime separation

circuit is the ion exchange feed and is fed to the first bank on adsorption. When the resin in this bank has been given sufficient time to reach an.intended U308 loading, the feed is advanced to the next bank and the pulp in the loaded bank is returned to the

ion exchange feed surge tank. The spare bank then becomes the

last bank on adsorption. Pulp from the last bank on adsorption

goes to tailings. The loaded bank which was removed from the adsorption cycle is washed free of pulp and becomes the last bank on elution. At this time, the eluate in the lead bank previously removed from the head of the elution circuit is pumped to the next bank _on elution and, hence, through the circuit. This is then followed by a volume of made-up eluant. Displaced pregnant eluate from the sixth, or last, bank on elution goes to precipitation.

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WIN-83

10

-Although the resin remains fixed within· any one basket, the manner in which solution or pulp is advanced from bank to bank produces a countercurrent effect. Changeover time, or the time a bank is in any one relative position, is calculated from the feed rate and uranium content of the ion exchange feed and from the desired or possible resin capacity.

F. Precipitation and Eluant Make-up

Although various precipitation and eluant make-up procedures are available, the H2S.04 -MgO procedure is commonly utilized.

Pregnant eluate is s.tored in one of two 5 x 41J;-ft stainless steel tanks in 500 gallon batches. !1ixing is by slow-sweep agitators. The uranium is precipitated as. follows: (1) sulfuric acid is added to pH 2.5 to 3.0 and the s.olution is heated to SO"C to drive off· CO~ and (2) the pH is raised to 7.0 by adding MgQ. The resultant ·precip1tate is filtered in a plate and frame filter press and the

filtrate .is discarded. The filter cake is washed with water and the wash liquor is returned to one of two 6 x 6-ft tanks for eluate make-up to 1

!i

NaCl. The yellow cake is dried, sampled, barreled, and shipped.

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TEST WORK WIN:-83 11

-The flowsheet shown in Figure 1 was used during the treatment of Monument Valley ore, A sunnnary of operational data obtained during

this alkaline RIP amenability test is presented in Table L A

total of 206.58 dry tons of ore was processed at a rate of 3.89

tons per day; During 1273 .8 hours of operation, the leach extraction

varied from 91.5 to 96.5 per cent and averaged 95.4 per cent,

Altho'ugh ion exchange adsorption data for the run averaged 98,6 per· cent, recovery was over 99 per cent a large portion of the time,

A. Grinding

The minus 3/16-in. crushed ore, which had an average assay of

0.239'-

u

₃

o

_{8 and 0.837% V205 , was fed to the ball mill and was}

ground in mill solution which contained 40 g Na2C03 and 10 g NaHC03 per liter, Daily belt feed data are presented in Appendix Table 1. Leaching solution was added to the ball mill discharge to control the density in the classifier overflow at 1.18, or 18.2 per cent

solids, for the entir~e run, Under these conditions, the classifier

overflow solids averagecl 25.4 per cent plus 100-mesh and 49.8 per cent minus 200-mesh·material.

The ball mill thickener operated effectively with an average under£low density of 1.49 .£1.8.8 per cent solids) and a flowrate

of 0.81 gpm. Separan 26l~addition for flocculation of the pulp

was 0 .087 lb/ton of ore. Daily grinding and ball mill thickener

data are included in Appendix Table 2. Daily flow data are presented

in Appendix Table 3 ..

B. Leaching

Average leach constants for the run consisted of a 43-hour residence time at a pulp density of 1.49 (48.8 per cent solids) with aeration air added for oxidation: Daily leaching data are shown in Appendix Table 4. During the periocl from November 27 through December 21,

the leach temperature in the Alkaline RIP Plant was 90°C, On

December 22, the temperature was decreased to 80°C in order to determine the effect of a somewhat lower temperature on extraction .in the leach circuit. Uranium and vanadium leach gradients were

taken under both condition~ and the data are shown in Table IL

The amount of water required for make-up of evaporation losses in the leach tanks was 1"5 tol)s per ton of feed at 90°C .as compared to 0.72 ton per ton of feeq at 80°C.

1/

The use of Separan 2610 does not constitute an endorsement of

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Table I

Sunnnary of Pilot Plant Data Alkaline Leach - RIP Pil.ot Plant

Monument Valley Ore Grinding ·and Leaching

Total dry tons milled

Ore feed rate, dry tons/24 hr Hours of operation

Leach contact time, hr Ore feed assay,

%

U303

%

v2o5 Leach concentration, g/1

1./

Na2co3 NaHC03 Residue assay, % U303

%

v2os Leach ext' n, '7. _{U 3o8}

%

v2o5 Sand-Slime Separation

Sand tails solution assay, g U303/l Soluble loss, %of U308 in feed Adsorption Feed, density gpm gpm/ton/day g

u

₃

o

₈₁₁ g

v

₂

o

₅₁₁ g Na₂

co

_{3 /l} g NaHC03/l Tails, g U303/l Recovery,

%

U303 Elution

Eluate volume to precipitation, gal/cu ft resin Pregnant eluate assay, g

u

_{3o8 /l}

Precipitation

Press filtrate, Water washes, g

1./

No. 5 leach tank discharge

WlN-83 12 -206.58 3.89 127 3.8 43.0 0.239 0.837 33.50 10.94 0.011 0. 716 95.41 14.50 0.037 0.38 1.05 2.51 0.65 0.56 0.27 10.90 1.03 0.007 98.6 36.6 9.88 0.004 0.050

Sample

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Belt feed BMCO Thickener Leach tank 1 2 3 4 5 Belt feed BMCO Thickener Leach tank 1 2 3 4 5

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Table II Leach Data Alkaline Leach - RIP Pilot

Monument Valley Ore Leach Tempe.rature, 9o•c

Plant

WIN.~83

13

-Date: December 20, 1955

. Solids Assax₂

%

%

Extraction

!!A

Y2.Qs.

!!3.Qa.

vzos

.294 1.16 .245 1.07 1.7 7.8 .1n 0.97 39.8 16.4 .042 0.89 85.7 23.3 .019 0.87 93.5 25.0 .014 0.86 95.2 25.9 .012 0.83 95.8 28.4 .011 0.87 96.3 25.0 Leach Temperature, 80"c .Date: January 8, 1956 .284 1.06 .231 1.01 1.9 3.8 .189 0.84 33.4 20.0 .037 0.82 83.4 22.7 .019 0.82 93.3 22.7 .013 0.85 95.3 19.8 .012 0.88 95.7 17.0 .011 0.96(?) 96.2 9.4

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WIN-.8) 14

-The data indicate that through the leaching circuit, decreasing the temperature to 80°C had essentially no e.ffect on uranium extraction. However, there is a slight decrease in vanadium extraction with this 10" reduction in leach temperature.

C. Mill Solution Make-up

Daily mill solution make-up data are shown in Table III. Con-sidering Na2C.03 and NaHC03 requirements to fill the circuit and the i.nventciry at the end .of the run, reagent use based on a runni.ng inventory was 64.4 lb NazC03 and 17.5 lb NaHG03 per t(ln of ore.

D. Sand-Slime Separation

The sand-slime circuit rejected an average of 2.26 tons of dry solids per day to tails at approximately 74 per cent solids.

A tot.al of 0.86 tons of solution assaying 0.037 g

u

₃

o

_{8 /l was sent}

to tails during the same period. This represented a soluble loss

of 0.36 per cent of the uranium in the mill feed. Daily drag

sands data are found in Appendix Table 5.

The data shaw that 41.8 per cent of the total solids which entered the Alkaline Pilot Plant was sent to the i.on exchange circuit. This necessitated a water addition of 2.56 gpm or 0.66 gallons per minute per ton of ore per day to. maintain an ion exchange feed density of 1.05 and resulted in a 15.2:1 water to solids ratio in the ion .exchange feed.

During the period from January 3 through January 14, pH adjustmll!nt of the ion exchange feed was accomplished with hydrated lime

instead of caustic. The lime w.as added as a dry powder to the overflow of No. 1 drag classifier. llaily ion exchange data, presented in Appendix Tables 6 and 7, show that the use of lime

had no apparent effect on ion exchange.recovery based on solutio.n assays. Lime requirements were approximately 15 pounds per ton of ore treated as compared to 9 pounds NaOH per ton when using

caustic for pH adjustment. The discharge of No. 5 leach tank,

No.. 4 drag sands, and the ion exchange ta.ils were sampled period-ically and the solids assayed during the lime addition. The data

obtained are presented in Table IV. A similar sampling program

was initiated during the last two weeks ol;.the run while using caustic for pH adjustment. Solids assays during this period "+e

presented in T.able V. The data indicate that approximately 4.

p

per cent .of the U308 in so.lution was precipitating when hydrat,ad lime was used for pH adjustment. There was no evidence that

caustic addition had a similar effect. Precipitation of dis<';qlved

u

₃

o

_{8 was probable due to localized high pH value.s near the :;urface}

of sniall CaO particles. This localized pH effect might be minimized in future aperatio.ns if lime were added as a smooth slake at approxi• mately 20 per cent s.olids ins.tead of as a dry powder.

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Table III

Daily Mill Solution Make-up Data

.Alkaline .Leach - RIP Pilot l'lan.t

Monument Valley Ore

Malte-up

WIN-83

.~ 15 "

Date Make-up Rea!!ient₂ lb .Concentrati.on ₂ !!iLl

1955 - 56 No. _Na2co3 NaHC0₃ Na₂

co

₃ NaHC03

11/27 1 1385.0 350.5 38.9 11.8 11/28 2 366.0 168.0 37.5 9.1 12/3 3 1375.0 347.0 42.5 8.9 12/11 4 1323.0 341.5 33.7 11.6 12/15 5 1337.0 275.0 30 .. 6 14.8 12/19 6 1400.0 650.0 33.6 10.2 12/21 7 1309.0 312.0 30.8 11.3 12/28 8 1247.0 281.3 30.4 9.7 1/6 9 1313.0 312.0 45.8 13.0 1/11 10 1010.3 345.5 29.2 10.1 1/15 11 1310.0 302.0 27.8 11.8 1/20 12 1284.0 268.0 25.9 12.7 Avg 33.9 11.2 Total 14659.3 3952.8 Inventory, 1/31/56 1355.6 337.6 Total reagents used, lb 13303.7 3615.2 lb/ton 64.4 17.5

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1956

l2!!.:!&

1/5

1/6

1/7

1/6

1/9

1/10

1/11

Table

IV

WIN-63

16

-Uranium in Leached Solids Using Lime for pH Adjustment

Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Lime

Overflmr

Steady

Add

1

_n

_~

_{!!;308 in So;!,ids}

Ho.

l

llJ:ag

~ad

IAnk !,b,LTon

No,

₂

_I..

_I•

Dl;:ag SAnds

\

10,92

n.01

19.2

,010

,009

10,95

10.96

12.0

,010

,010

n.oo

10.96

13.7

.on

.010

n,20

10.92

15.6

.on

,010

10,96

10.92

19.6

,012

n,20

10,97

13.7

.on

.010

n,lO

10.92

16,7

,012

,010

Avg

.on

,ow

Weighted Avg

,021

Ia:t!le

Y.

~

:J:ails

.046

•042

.056

.040

.036

,036

,Oil!~

Uranium in Leached Solids Using Caustic for pH Adjustment

Alkaline I.each - RIP Pilot Plant

Monument Valley Ore

H

NaOH

1956

Overflmr

Steady

Add'n

$

ll~06

in Solids

Date

No, 1 Drag

Head :J:ank Lb,LTon No, 5 L,:J:. Drag Sands IX Tails

1/23

10,12

10.92

9.3

.013

.on

.027

1/24

10.12

10.91

9.5

.on

,007

.026

1/25

10.13

10.90

10,3

.010

,006

.024

1/26

10,15

10.65

n.l

,010

.007

,025

1/27

10.12

10.90

10,9

.on

,006

,025

1/26

10,10

10,60

n.9

.010

.007

,023

1/29

10.40

.

10.96

7.3

,010

,006

.• 026

Avg

.on

,007

,026

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.E .•. Resin ~ption W.Itf~83 - 17 ·~

Rohm & Haas, XE.-123, resin

lf

was used in t)le ion exchange circuit during this test program on Monument Valley ore. This: res:i.n had been used previously during amen11bility tests. on La Sal .and Utex ore. A resin loss of 1.5 per cent was noted in 1275 hours of operation of the ion exchange .circuit, Part of this 1os.s is thought to be from attrition Md part was caused by sl!Inpling and spills.

The ion exchange feed from the sand-slime circuit at

a

contained approximately 6 .·2 per cent solids by weight. the pulp after adjustment with caustic aver11ged 10.95,

density of 1.05 The pH of

The primary objective of this test work on Monument Valley o;re was to determine the effect, if any, of operating with an ion exchange feed having .a uranium to vanad,ium ·ratio of approximately 1:1. In

illl attempt to achieve this ratio. various high grade portions ·of

Stockpile 46 were processed. F.or the period from December 5 to JMuary 10 the feed to the plf~I~t var'f.ed as shown in Table VI.

As:

the data show,. a uranium to vanadium ratio of 1:1 was not attained, Further attempts to obtilin a higher grade vilnadium .ore fro!l;l this

stockpile were then ab.andoned. ·

Table VI

Alkaline Leach .,. Rll'. Pilot Plant

Monument Valley Ore

.Belt Feed ₂ % _{lXF• g;/1 U308:V205}

UJOS V205

.fuQa

. vzo§ Ratio

.IX Tails., g/1 U;~Os

Vill5

12/5 .152 0.370 .500 .123 4.1:1 .007 .125 12/9 ,214 0.812 .520 .183 3.8:1 .002 .148 12/13 .251 0.784 .610 .231 2.6:1 .oo5 . 260 12/18 .275 1.14 .670. .375 1.8:1 12/22

£:./

.243 0.964 .630 .344 1.8:1 .009 .312 .009 .340 12/27 .264 1.19 .530 .3.08 1. 7:1 .008 .291 12/31 .254 1.01 .510 .. 351 1. 5:1 .0.02 .. 316 1/6 .248 0.9.90 .440 .255 1. 7:1 .005 .249 1/10 .258 0.852 .480 .260 1. 9:1 .0.02 ,280

The use of XE-123 does not constitute an end.orsetitent 9f this resin nor does it mean that XE-123 is the only res.in suit11ble for the R!l' process •

The temperature in .the leach circuit was de.creased fro!l;l 90"C to 80°C and the sand-slime circuit was operated to produce illl

:tX ilt a density of 1.05 to. 1.06 irtstead of 1.06 to 1.07 grli)D.s per ml.

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WIN-83 18

-The ion exchange circuit was operated at a solution to resin ratio of 6:1 with seven banks on exhaustion and five on elution. With

the circuit operating under these conditions and the pH of the ion

exchange feed properly adjusted for vanadium elimination,

l/

samples

were taken of the ion exchange feed pulp, eluting solution, and

resin in each basket on January 27. These samples were taken

simultaneously at changeover. The solution and resin samples were

assayed for both uranium and vanadium and the results plotted in

Figures 2 and 3. These data show the expected decrease in vanadium

on the resin as it becomes loaded with uranium. The adjustment of

feed pulp pH has not prevented the adsorption of vanadium but

rather has shifted the equilibrium to favor the preferential loading

of uranium.

Daily ion exchange data are summarized and presented in Appendix Tables 6 and 7. With an average ion exchange feed assay of 0.563 g U308/l and the circuit operating at an intended loading of

3.4 lb U308 per cu ft of wet settled resin, the ion exchange tails

averaged 0.007 g u3o8;1. The average changeover time was ~.9 hours

and a recovery of 98.7 per cent was realized.

F. Elution and Precipitation

Daily elution and eluate make-up data are shown in Appendix

Table 8. The eluant used was a neutral solution of l ~ NaCl. A

total of 40 gallons of pregnant eluate, 4.9 equivalent resin volumes,

was sent to precipitation per bank eluted. There were five banks

on elution with the eluate to resin ratio at 6:1. Pregnant eluates averaged 9.88 g u3o8 11 and final eluate from the lead bank on elution averaged 0.12 g u 3o8 /l. Samples of eluted resin which were stripped in the laboratory showed the elution was complete. Pregnant eluate was precipitated in 550-gallon batches. The pre-cipitated slurry was filtered and washed in a plate and frame press. Both the press filtrate and water washes were discarded. Daily filtrate and wash data are presented in Appendix Table 9 while daily reagent requirements for precipitation are shown in Appendix

Table 10. Additional precipitation data showing daily yellow cake

assays are presented in Appendix Table 11. A total of 20 precipi-tations were made producing 1269.2 lb of yellow cake containing 891.0 lb u 3o8 . Precipitations of the pregnant eluates were made by adding H2S04 to adjust the pH to 2.7 - 3.0, heating to so•c, agitating 2 - 3 hours, and then neutralizing to pH 7 with MgO. Reagent requirements for elution and precipitation were 1.40 lb

H2so4 , 0.31 lb MgO, and 6.12 lb NaCl per pound of

u

_{3o8 produced.}

l/

Topical Report :wrN-39, Alkaline Res.in-In-Pulp Process for the

,!1

Exhaustion

..

_Elution

l15.0

Ion Exchange Feed

. 56 _

g

u

₃

o

₈₁₁ . 321

s v

₂

o

₅₁₁

....

10.0 .... ... _po ... 00 " 0.6 " s:: s:: 0 0

....

_.u

....

.u

"'

0.5

_"'

...

...

.u c v 2 : : .u s:: s::

"'

_"'

cJ

"

s:: _0.4 s:: 0 o.- -.... 0 0

_"'

'

0 s:: _5.0 s:: 0 0

....

_0.3 U308

....

.u .u

"

"

....

....

0 0

"'

0.2 CJl 0 0.1 U308 1 2 3 4 5 6 7 8 9 10 11 12 13 14 Bank I _:0:: H

,...z

Figure 2 \0 I 0>

Alkaline RIP Elution Gradient I VJ

55 50 1>1 45

g.;

.-< 40

...

00 00 35 0:

"'"

""

30

"'

0 ...:I

"'

....

25

"

·~ 20. 15 10 5 140---Exhaustion---~-- -.(---Elution---~--U308 1 2 3 4 5 v2o5 6 7_{Bank 8} 9 Figure 3

Alkaline RIP Resin Gradient Monument Valley Ore

10 12 13 14

'"'

H NZ 0 1 co I u>

c

c

(

METALLURGICAL BALANCE WI~-83 21

-A metallurgical balance with respect to uranium and vanadium for the Alkaline Leach - RIP Pilot Plant when Monument Valley ore was treated is presented in Tables VII and VIII, respectively. The uranium and vanadium content are from assays of samples taken in the Feed Preparation Plant and quantity of ore processed is based on truck weights. _{The calculated U308 recovery amounted 92.9}

per cent. Actual uranium recovery based on ba.rrel weights and assays was 90.2 per cent resulting in an unaccountable loss of 2.7 per cent. Vanadium elimination in .the ion exchange circuit was successful, in that only 0.5 per cent of the total V205 in the mill feed reported in the final product. A vanadium unaccountable loss of 0.3 per cent is reported.

Table VII

U30s Metallurgical Balance Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

U308

Tons

u

₃

og

Content Total

Treated % g/1 lb %

Feed 206.58 0.239 987.45 100.0

Residue 206.58 O.Oll 45.45 4.6

Leach liquor 942.00 95.4

Soluble loss in drag sands 0.039 3. 76 0.4

Adsorption uni.t feed 0.563 938.24 95.0

Adsorption unit tails 0.007 13.14 1.3

Solution to precipitation 9.88 925.10 93.7

P~;ess filtrate 0.004 3.81 0.4

Press water wash 0.043 4.40 0.4

Calculated product recovery 916.89 92.9

Product (1269.2 lb) 70.2 891.00 90.2

c

(

Table VIII

R2.0.5

Metallurgical Balance

Afkgl ine I.each -

RIP

Pilot Pla..'rlt

Monument Vall ey Ore

Tons

:i1:2Q;i

Treated

_...:L

gfi

_ill

Feed

206.58

0,837

3458.1

Leach residue

206.58

0,716

2958.2

Leach liquor

0,288

499.9

RIP tails

0.273

473.9

Eluate

0.168

26,0

Yellow cake

(1269.2

lb)

1.46

18.5

Unaccountable loss

7·5

WIN-83

22

-Total

%'

100,0

85.5

14.5

13.7

o.8

0.5

0,3

(

c

APPENDix

WIN-83

23

WIN-83 25

-c

Tab!e 1 (Contd) Daily Belt .Feed Data

Alkaline Leach - RIP Pilot Plant Monument Valley Ore

Time Dry Belt Feed Material

.~ hr Tons 1956

%

U~Os

u

3

o

8., lb

%

V;!OS

v

2

os

1.lb 1/3 21.0 3.91 .269 21.02 1.14 89.08 1/4 24.0 4.01 .260 20.86 1.02 81.82 1/5 24.0 4.01 .288 23.10 1.13 90.65 1/6 24.0 3.98 ,248 19.75 0.990 78.84 1/7 24.0 4.02 .215 17.30

!l;

72.

57.92 1/8 24.0 3.98 .284 22.62 1.01 80.44 1/9 24.0 4.00 .260 2(). 78 1.23 98.33 1/10 24.0 4.03 .258 20.80 0.852 64.66 1/11 24.0 4.02 . 241 19.38 . _{0.964 77.53}

c

1/12 24.0 4.02 .275 22.12 1.034 83.15 1/13 24.0 4.01 .237 19.01 0.832 66.74 1/14 24.0 3.96 .219 17.35 0. 715 56.64 1/15 24.0 4.00 .266 21.28 0.778 62.24 1/16 24.0 4.01 .266 21.33 0. 739 59.27 1/17 24.0 4.01 .250 20.03 0.801 64.18 1/18 24.0 4.02 .263 21.16 0.815 65.58 1/19 24.0 3.99 .169 13.50 0.534 42.65 1/20 24.0 3.96 .195 15.46 0~589 46.68 1/21 24.0 3.99 .189 15.08 0.557 44.44 1/22 24.0 4.00 .199 15.92 0.671 53.68 l/23 24.0 4.03 .184 14.81 0.676 54.42 1/24 24.0 3.95 .211 16.66 0.766 60.47 1/25 6.0 3.96 .232 18.36 0.995 78.35 Avg 3.89 .239 0.837

(

WIN-83 26

-c

Table 2

Daily Grinding .and Ball Mill Thickener Data Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Density, s;Lml

Classifier Thickener Flocc Add' n ·

Date Ball Mill O' flow U'flow ml[min lbLday

1955 11/27 1.58 1.20 7.8 O.lll ll/28 1.57 1.19 1.37 fl. 1 0.215 11/29 1.59 1.19 1.39 7.7 0.205 11/30 1.56 1.18 1.41 24.2 0.639 12/1 1.57 1.19 1.38 82.0 2.167 12/2 1.58 1.18 1.31 54.3 1.435 12/3 1.59 1.19 1.34 37.7 0.996 12/4 1.58 1.18 1.41 24.1 0.637

c

12/5 1.58 1.17 1.45 23.0 0.608 12/6 1.58 1.18 1.49 23.6 0.624 12/7 1.57 1.18 1.49 25.9 0.684 12/8 1.59 1.18 1.50 7:6 0.201 12/9 1.58 1.18 1.50 18.3 0.483 12/10 1.58 1.17 1.50 17.0 0.449 12/11 1.58 1.17 1.49 14.7 0.388 12/12 1.57 1.18 1.50 15.0 0.396 12/13 1.57 1.19 1.49 14.6 0.386 12/14 1.58 1.18 1.49 12.0 0.317 12/15 1.58 1.18 1.49 13.8 0.365 12/16 1.58 1.17 1.50 7.0 0.145 12/17 1.58 1.17 1.48 7.7 0.203 12/18 1.58 1.18 1.49 5.0 0.132 12/19 1.58 1.18 1.50 8.3 0.219 12/20 1.58 1.18 1.50 11.3 0.298 12/21 1.58 1.18 1.50 12.3 0.325 12/22 1.57 1.18 1.50 12.3 0.325 12/23 1.58 1.17 1.47 21.0 0.555 12/24 1.59 1.18 1.48 5.0 0.132 12/27 1.5~ 1.18 1.68 9.0 0.238 12./28 1.59 1.17 1.58 9.0 0.238 12/29 1.66 1.17 1.41 13.0 0.343 12/30 1.64 1.17 1.38 11.0 0.291 12/31 1.64 1.18 1.38 8.0 0.211

(

WIN-83 27

-(

Table 2 (Contd)

Daily Grinding .and Ball Mill Thickener Data Alkaline Leach - RIP Pilot Plant

.Monument Valley Ore

Densit:~:, gLml

·Classifier Thickener Flocc Add'n

~ Ball Mill O' flow

1956

U' flow ml/min lb/dax

1/3 1.63 1.18 1.55 8.5 0.225 1/4 1.64 1.18 1.43 14.0 0.370 l/5 1.64 1.18 1.44 8.0 0.2ll l/6 1.63 1.18 1.44 13.0 0 .. 343 1/7 1.64 1.18 1.49 15.0 0.396 1/8 1.64 1.18 1.50 12.5 0.330 l/9 1.64 1.18 1.50 16.0 0.423 1/10 1/64 1.18 1.51 13.0 0.343

c

1/ll 1.64 1.18 1.52 14.0 0.370 1/12 1.64 1.18 1.53 20.0 0.528 1/13 1.64 1.18 1.52 16.0 0.423 1/14 1.64 1.18 1.51 25.0 0.661 1/15 1.65 1.18 1.53 27.0 0.713 1/16 1.63 1.18 1.54 30.0

o.

793 1/17 1.65 1.18 1.51 34.0 0.898 1/18 1.62 1.18 1.51 28.6 0.756 1/19 1.64 1.18 1.53 ll.O 0.291 1/20 1.63 1.18 1.51 34.0 0.898 1/21 1.64 1.18 1.51 29.0 0.766 1/22 1.65 1.18 1.51 25.0 0.661 1/23 1.64 1.17 1.53 19.0 0.502 1/24 1.63 1.17 1.51 27.0 0.713 1/25 1.65 1.54 33.0 0.872 Avg 1.61 1.18 1.49 18.6 0.490

(

WIN-83 30

(

-'-·

_{Table 4}

Daily Leach Data No. 5 Leach Tank Discharge Alkaline Leach , RIP Pilot Plant

Monument Valley ·Ore

Leach

R.esidue₂ _% _{Solution, !!ill} .Ext'n, '7.

~ O.ensity

_tr3os

_~

u

_{3og .}

Na2

Co

₃ NaHC03

u1oa

v,os

..l9..55.

ll/27 11/28 ~ 11/29 11/30 L49 12/1 1.41 .012 .376 2.48 50.5 13.2 93.7 30.5 12/2 1.51 .011 .394 1.99 52.0 14 . .4 94.3 29.6 12/3 1.45 .011 .452 0.946 26.0 6.62 92.7 12/4 1.49 .016 .030 1.72- 42.5 8.86 89.2

c

12/5 1.50

.on

.514 2.00 47.6 10.90 92.2 12/6 1.51 .012 .494 2.09 45.5 12.60 91.5 12/7 1.47 .010 .466 2.4q 4?.2 11.50 94.8 31.9 12/8 1.50 .006 .356 2;25 ~8.0 10.50 97.5 49.2 12/9 1.50 .Ql;l .486 2.15 31.4 10.50 94.8 40.2 12/10 1.50 .011 .524 2.66 34.1 11.90 95.6 46.3 12/11 1.48 .010 .526 3.71 31.2 9.50 96.2 49.0 12/12 1.49 .011 .598 3.04 32.8 12.50 96.5 44.9 12/13 1.50 .012 .643 2.93 29.1 10.60 95.2 18.0 12/14 1.49 .012 . 754 3.25 30.7 10.60 94.4 12/15 1.50 .01:2 . 782 3.12 27.8 12.50 94.0 12/16 1.51 .010 . 745 2.83 27.0 9.53 97.0 35.5 12/17 1.50 .011 . 738 2.69 28.8 7.60 96.2 36.3 12/18 1.50 .011 . 754 2.80 32.5 7.60 95.8 33.8 lZ/19 1.50 .011 .815 3.19 33.6 10.20 96.3 29.7 ' 12/20 1.49 .b11 .868 3.28 37.0 8.90 95.5 11.8 12/21 1.47 .012 .885 2.92 30.8 9.90 95.4 16.9 12/22 1.49 .012 .885 2.93 29.9 9.30 95.2 8.2 12/23 1.50 .013 .937 3.32 33.6 7.60 93.4 12/24 1.50 12/27 1.47 .011 .880 3.12 36.3 11.4 95.8 25.9 12/28 1.51 .Oli .820 2.74 30.4 9.7 95.8 27.2 12/29 1.51 .011 .834 2.91 32.0 9.1 96.3 31.9 12/30 1.50 .009 .806 2.15 26.1 9.0 96.1 17.9 12/31 1.51 .010 .898 3.15 41.0 13.5 96.1 11.2

(

WIN~83

31

-c

Table 4 (Contd) Daily L.each Data

N"o. 5 Leach Tank Dis.charge Alkaline .Leach .~ RIP .Pilot Plant

Monument Valley Ore

Leach

.Residue, % Solution, g/1 Ext'n, %

Date Dens it;)::

_!!.3Qa.

_V205 U30a N"il2C03 N'all.CO@ u3oa

vzo

₅ 1956 1/3 1.51 .015 .887 2.55 39.4 10.2 94.3 22.2 1/4 1.46 .011 .938 3.04 42.1 11.8 95.3 17.7 1/5 1.51 .010 .963 3.22 40.5 14.4 96.5 14.8 1/6 1.51 .010 .94 4.01 45•8 13.0 96.0 9.1 1/7 1.50 .011 .97 4.27 43.7 11.6 94.9 1/8 1.50 .011 .94 3.9!j 40.0 9.87 96.1 6.9

c

1/9 1.50 .012 .88 3.34 36.8 11.0 95.4 28.5 1/10 1.49 .011 .87 3.16 31.7 11.6 95.7 1/11 1.50 .012 .90 3.3,8 32 .o 15.2 94.8 6.3 1/12 1.48 .013 . 81 2.95 . 27.5 10.4 95.1 21.4 1/13 1,50 .013 . 78 3.04 27.0 10.8 94.5 6.0 1/14 1.50 .013 .81 3.27 28.3 10.2 94.1 1/15 1.49 .013 .81 3.17 27.8 11.8 95.1 1/16 1.50 .012 . 79 2.93 27.2 10.2 95.5 1/17 1.51 .015 .71 3.43 27.5 11.2 92.2 11.3 1/18 1.50 .023 . 74 3.41 28.3 11.8 91.2 19.0 1/19 1.50 .017 .69 3.35 27.0 10.6 90.0 1/20 1.50 .015 .66 3.30 24.6 11.8 92.3 1/21 1.49 .016 .71 3.24 26.5 12.7 91.5 1/22 1.51 .015 .62 2.85 24.9 12.7 92.4 19.3 1/23 1.51 .013 .58 2.81 26.5 12.3 92.8 14.7 1/24 1.50

.pn

.56 2.52 26.1 11.5 94.6 27.3 1/25 1.50 2.5.4 26.7 11.1 Avg 1.49 .011 .716 2.91 33.5 10.94 95.4 14.5

(

WIN-83 32

-c

Table 5

Daily No. 4 Drag .Sands Data Alkaline. Leach - RIP .P;!.lot Plant

Monument Valley Ore

Solution

Tons Rejected/day Assay

Date Density Solids :solution g

u3oa/1

'I9'5s

11/30 12/1 1.73 1.94 0.94 12./2 L5s 1.23 0.85 .08 12/3 1.80 0.81 0.33 .04 12/4 2.Q7 l. 78 0.38 .03 12/5 1. 79 1.06 0.43 .04 12/6 1.88 2.58 0.87 .05 12/7 L~5 1.80 0.65 .06

c

12/8 1. 78 2.20 0.93 .05 12/9

Las

2.40 0.85 .05 12/10 l. 76 2.71 l. 22 .05 12/11 1.77 2.90 l. 27 .05 12/12 1. 76 2.05 0.93 12/13 1.71 1.93 0.99 .04 12/14 l.

76

2.61 1.19 .07 12/15 1.84 2.64 0.97 .04 12/16 ~.75 2.43 1.12 .07 12/17 1.19 2.42 0.76 .08 12/18 1 12/19 1.80 2.29

o.

72 12/20 ~.75 2.53 1.00 .07 12/21 ~.73 3.11 1.37 .08 12/22 :J-.79 2.96 1.38 .09 12/23 _1-·BQ 3.17 1 .. 27 .05 12/24

po

1.29 0.51 12/28

i.so

2.96 1.20 .05 12/29 1.85 1.89 0.68 .05 12/30 _H~ ,. 1.16 0.44 .05 12/31 1.87 1.24 0.43 .06

(

WIN-83 33

-(

Table 5 (Contd)

Daily No. 4 Drag S.ands Data Alkaline Leach .~ Ril' Pilot Plant

Monument Valley Ore

Solution

Tons .Rejected/day Assay

~ D.ensity Solids Soluti.on g.U@Os/1

1956 I

173

~.69 2.32 0.90 .02 l/4

'

2.06 0.80 .02 l/5 1.81 1.56 0.60 .03 l/6 1.81 2.03 0.78 .04 l/7 i.8o 1.89 0.76 .04 l/8 2.38 0.96 .03 l/9 2.24 0.90 .03 l/10 2.21 0.89 .04

c

1/ll 1.85 2.84 1.14 .04 l/12 1.87 2.37 0.83 .01 l/13 1.85 2.14 0.76 .04 l/14 2.54 0.90 .02 l/15 1.87 3.80 1.34 .02 l/16

Las.

2.49 0.83 .02 l/17 i.98 3.06 0.82 .02 l/18 1.94 2.54 0.75 .02 l/19 l. 96 1.94 0.53 .02 l/20 1.95 2.95 0.85 .02 l/21 1.84 2.87 1.06 .02 1/22 1.84 2.57 0.94 .02 l/23 1.83 2.53 0.95 .01 l/24 1.95 . 2.58 0. 72 .01 l/25 ]..84 2.69 1.00 .01 l/26 1.?6 1.74 0.79 .01 l/27 l. 75 l . 70 1.00 .02 l/28 1.81) 1.47 0.59 .01 l/29 1.80 1.16 0.47 .01 Avg 1.82 2.24 0.86 .037

(

WIN-83 34

-c

Table 6

Daily Resin-In-Pulp Uranium Adsorption Data Alkaline Leach - RIP Pilot Plant

_Monument Valley Ore

Ion Exchan~e Tails

Ion Exchan~e Feed Recovery

Da_te

_..E!.

Dens it)!: _BE!!! ~ iJ3os/l ~

u

_3o211 %

1955 11/30 10.3 1.04 3.31 . 78 12/1 10.4 1.04 1.05 0 76 .018 97.6 12/2 11.0 1.04 1.63 .58 .001 99.8 12/3 11.2 1.03 0.22 .45 .001 99.8 12/4 11.0 1.03 1.88

.so

.001 99.8 12/5 11.0 1.05 1.37

.so

.007 98.6 12/6 11.0 1.06 2.35 .60 .029 95.2 12/7 11.0 1.06 1.83 .59 .042 92.9 12/8 11.0 1.06 1.89 .60 .013 97 .8 12/9 10.9 1.06 2.05 .52 .002 99.6

c

12/10 10.9 1.06 1.93 .53 .004 99.3 12/11 10.9 1.06 1.98 .66 .015 97.7 12/12 10.8 1.06 2.17 .57 .004 99.3 12/13 10.9 1.06 1.60 .61 .005 99.2 12/14 10.9 1.06 2.33 .63 .007 99.5 12/15 10.9 1.06 2.18 .58 .002 99.7 12/16 10.9 1.06 3.03 .62 .006 99.0 12/17 10.9 1.06 1.88 _{·-· 64} .015 97.7 12/18 10.9 1.06 1. 78 .67 .009 98.0 12/19 10.9 1.06 2.31 .68 .012 98.2 12/20 10.9 1.06 2.59 .75 .018 97.6 12/21 10.9 1.05 2.52 .82 .073 91.1 12/22 10.9 1.05 3.17 .63 .009 98.6 12/23 10.9 1.05 2.25 .56 .005 99.1 12/24 11.0 1.05 2.72 .59 .002 99.6 12/28 11.0 1.05 3.83 .53 .008 98.5 12/29 11.1 1.05 2.30 .51 .006 98.8 12/30 11.0 1.05 1.53 .57 .006 98.9 12/31 11.0 1.04 1. 78 .51 .002 97.6 1956 1/3 11.0 1.05 3.32 .48 .005 99.0 1/4 11.0 1.05 2.62 .48 .005 99.0 1/5 11.0 1.04 2.97 .51 .039 92.4 1/6 11.0 1.04 2.93 .44 .005 98.9 1/7 11.0 1.05 2.50 .48 .002 99.6 1/8 10.9 1.05 2.84 .52 .002 99.6 ( 1/9 10.9 1.05 3.14 .49 .002 99.6

'·

WIN-83 35

-(

Table 6 (Contd)

.Daily Resin-In-Pulp Uranium Ads.orption Data Alkaline .Leach- RIP-Pilot Plant

Monument Valley Ore

Ion Exchange Tails

Ion·Exchange Feed Recovery

~ _E!L_ Densitl _~ J1i

u

₃

o

_{2 /l 8}

u

₃

o

₈₁₁ '7. 1956 1/10 11.0 1.05 2.56 .48 .002 99.6 1/11 10.9 1.05 2.73 .55 .002 99.6 1/12 11.0 l.d:S 3.34 .56 .002 99.6 1/13 10.9 1.05 2.43 .5} .003 99.4 1/14 10.9 1.05 2.66 .56 .002 99.6 1/15 11.0 1.05 2.73 .58 .004 99.3 1/16 10.9 LOS 3.42 .5.6 .003 99.5 1/17 10.9 1.05 2.83 .57 .004 99.3 1/18 11.0 2.51 .57 .002 99.7

c

1/19 10.9 3.24 .54 .003 99.4 1/20 11.0 2.49 .62 .004 99.4 1/21 10.9 2.99 .57 .003 99.5 1/22 10.9 2.86 .53 .001 99.8 1/23 10.9 2.80 .48 .002 99.6 1/24 10.9 2.82 .46 .002 99.6 1/25 10.9 3_.06 .. 44 .002 99.5 1/26 10.9 2.42 .44 .002 99.5 1/27 10.9 3.68 .§2 .006 98.8 1/28 10.8 3.15 .52 .008 98.5 1/29 11.0 3.82 .56 .023 95.9 Avg 10.9 1.05 2.51 .56 .007 98.6

.!'\

!

Table 7

Daily Miscellaneous .Resin-In-Pulp Adsorption Data Alkaline Leach - RIP Pilot Plant

Monument Valley {)re

Ion Exchan!iie Feed Ion Exchange Tails V205

Tons/day _{Solution, gJl} Salutian₂ g/1 Recovery

Date Sol ,ids Sol1_·n

VzO't Na2Co3 NaHC03 _{~ Na2co3} NaHC03 %

1955 11/30 0 .. 90 19.75 12/1 0.28 6.25 .162 22.3 9. 70 .12.2 19.7 6. 72 24.7 12/2 0.41 9. 7 5 .191 18.3 1. 76 .191 18.3 1.18 0.0 12/3 0.03 1.34 :148 15.4 1. 76 .161 16.8 1.00 9.4 12/4 0. 77 11.20 .131 87.7 2.60 .109 71.3 4.83 58.4 12/5 0.51 8.16 .123 17.2 0. 78 .125 17 .3 1.09 1.6 12/6 1.06 13.90 .200 17.7 0.90 .180 16.5 0.45 10.0 12/7 0. 79 10.85 .153 .134 12.4 12/8 0.89 11.19 .229 13.9 0.69 .231 13.1 1.09 8.8 12/9 0.92 12.09 .183 .148 19.1 12/10 0.89 11.41 .200 9.8 1.9 .200 9.8 1.2 0.0 12/11 0.93 11.69 .281 10.7 1.8 .249 10.7 1.8 11.4 12/12 0.91 12.87 .35 9.0 1.7 .270 9.0 0.8 22.9 12/13

o.

75 9.42 .31 8.9 1.6 .260 8.9 0.8 16.1 12/14 1.05 13.74 .301 8.5 1.7 .333 8.5 0.8 10.6 12/15 0.98 12.86 .235 7.8 0.5 .221 7.0 0.76 5.7 12/16 1.43 17.86 .298 8.8 0.44 .298 7.7 0.67 0.0 12/17 1.00 10.40 .333 9.9 0.50 .350 9.7

o.

73 5.1 I _:0: 12/18

o.

79 10.53 .375 8.7

o.

70 .312 9.8 1.50 16.8 '-'.Z H 12/19 1.04 13.65 .456 10.0 1.11 .358 9.4 0.42 21.5 Cl' ex> I I W 12/20 1.20 15.25 .421 10.3 1.26 .403 9.6 0.67 4.3

~'

_0,

(~'

Table 7 (Contd)

Daily Miscellaneous. Resin-In-Pulp Adsorption Data Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Ion Exchan~e Feed Ion:Exchange Tails _v2o5

Tons/day .Solution·, g/1 Recovery

Date Solids Sol1_n

v,os NazC03 NaHC03 VzOs Na2co3 l'laHC03 %

1955 1'2721 0.99 14.94 .473 12.2 .463 10.6 0.84 2.1 12/22 1.24 18.77 .344 9.6 0.13 .340 8.9 0.42 1.2 12/23 0.78 13.37 .298 9.0 .291 8.4 0.42 2.4 12/24 1.07 16.15 .280 8.9 .263 7.8 0.25 6.1 12/28 1.35 22.78 .308 9.5 .291 8.8 0.34 5.5 12/29 0.81 13.67 .291 7.4 .252 7.0 0.24 13.4 12/30 0.54 9.10 .323 8.1 0.4 .316 7.6 0.08 2.2 12/31 0.58 10.60 .351 7.8 0.7 .226 7.3 0.04 35.6 1956

ll3

1.26 19.68 .280 8.9 .284 7.8 0.30 1.5 1/4 0.86 15.61 .237 8.5 0.8 .222 8.3 0.17 6.3 1/5 0.89 17.71 .243 7.9 0.8 .226 7.8 0.2 4.7 1/6 0.89 17.49 .255 6.6 0.6 .249 6.5 nil 2.4 1/7 0.79 14.96 .280 7.0 0.8 .270 7.0 0.76 3.6 1/8 1.11 16.85 .290 6.8 0.9 .260 6.0 0.42 1.1 1/9 1.19 18.62 .290 6.7 1.2 .28 6.9 0.42 3.5 1/10 0.89 15.23 .260 6.4 0.9 .28 6.2 0.21 7.7 _{I :0:} 1/11 1.06 16.17 .281 6.6 0.6 .259 6.4 0.25 7.8 H

wz

1/12 1.18 19.86 .348 6.1 0.97 .305 5.7 0.38 1.2 -.J I CXJ 1/13 0.85 14.42 .287 6.4 0.18 .292 5.7 0.59 1.7 I W

/", _,f\,

Table 7 (Contd)

.Daily Miscellaneous Resin-In-Pulp Ads.orption Data

Alkaline Leach - RIP Pilot :Plant

Monument Valley Ore

Ion Exchange Feed Ion-Exchange Tails V2o5

Tons/day Solution, g/1 S.olution₂ g/1 Recovery

Date

· -

Solids S.ol'n

Y2Qs.

NazC03 _.NaJ!c;o3 _VzOs

_Nacco3

_{NaHC03 %}

1956 1/14 0.98 15.83 .368 7.7 0.17 .354 6.7 0.50 2.5 1/15 1.03 16.69 .286 8.5 0.22

.no

7.6 0.55 5.6 1/16 1.25 20.28 7.4 0.21 .259 6.7 0.67 1/17 1.07 16.79 .329 7.9 0.40 .333 7.2 0.55 12.1 1/18 0.96 14.86 . 32;9 7.9 0.29 .284 6.9 0.63 25.1 1/19 1.27 19.21 .308 7.6 0.17 .313 6.4 0.42 1.6 1/20 0.88 14.79 .392 8.3 0.07 .3:29 7.3 0.25 16.1 1/21 1.02 17.29 .514 7.3 0.25 1/22 1.08 16.96 .326 6.4 1.3 .315 5.8 0.84 3.5 1/23 0.99 16.61 .301 7.5 0.11 .291 6.6 0.42 3.3 1/24 1.07 16.72 .238 6.4 0.48 .294 5.8 1.68 2.1 1/25 1.16 18.14 .263 7.2 0.26 .239 6.5 0.50 9.7 1/26 0.85 14.37 .298 7.3 0.34 .)80 6.8 0.42 6.0 1/27 1.44 21.82 .368 7.9 0.62 .250 7.1 0.88 32.1 1/28 1.20 18.66 .308 9.4 0. 74 .285 8.8 0.55 7.5 1/29 1.39 22.65 .352 13.8 1.54 .330 12.5 1.13 6.3 Avg 0.96 14.85 .267 10.9 1.03 .272 10.0 0. 78 7.6 I ::;: H

wz

()0 I ()0 I

""

WII:'I-83 39

-(

Table 8

Daily Elution and Eluate Make-up Data Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Final Eluate Make-up

Eluate .Eluate Batch NaCl

.Date gal/day g U30g/l g U;Os/1 No;

_--.

lb

1955 12/2 120.0 13.28 .284 40 48:1 12/3 40.0 8.60 . .261 41 487 12/4 80.0 13.88 .214 12/5 80.0 11.94 .290 12/6 160.0 10.97 .362 12/7 160.0 7.75 .107 42 12/8 160.0 8.66 .088 12/9 160.0 10.84 .088

c

12/10 160.0 11.57 .130 283 12/11 160.0 10.55 .129 12/12 200.0 10.61 .109 44 487 12/13 160.0 10.68 .083 12/14 200.0 10.24 .107 12/15 200.0 10.65 .150 12/16 240.0 10.97 .145 45 292 12/17 200.0 10.65 .120 12/18 120.0 11.35 .102 12/19 200.0 10.51 .092 46 298 12/20 200.0 10.30 .078 12/21 200.0 10.55 .099 47 227 12/22 200.0 10.77 .126 12/23 160.0 11.33 .124 12/24 200.0 11.22 .122 12/27 240.0 11.08 .103 8 289 12/28 160.0 11.32 .110 12/29 160.0 11.51 .129 9 282 12/30 120.0 11.43 .143 12/31 80.0 12.60 .150 1956 1/3 . 120.0 12.48 .166 1/4 200.0 10.98 .140 1/5 160.0 10.75 .118 10 296 1/6 160.0 11.38 .098 1/7 200.0 11.30 .086 1/8 200.0 11.07 .115 11 241

(

1/9 160.0 11.66 .096 1/10 160.0 11.35 .090 12 268

WIN."83 40 -/ ( ,_ --Table 8 (Contd)

.Daily Elution and Eluate Make-up Data

Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Final .Eluate Make-ul!

Eluate Eluate Batch NaCl

Date gal/day _{g U308 /1}

1956

&

U70g/l No.

_.JJL

i7iT

200.0 11.09 ,098 1/12 i2o.o 11.20 .084 1/13 200.0 10.37 .088 1/14 160.0 10.65 .088 12 268 1/15 200.0 10.50 .076 1/16 280.0 10.25 .083 13 293 1/17 200.0 11.21 .093 1/18 200.0 11.05 .100 1/19 200.0 11.13 .106 14 275

c

1/20 200.0 10.21 .085 1/21 160.0 10.99 .080 15 1/22 160.0 11.11 .102 1/23 200.0 11.16 .111 1/24 160.0 9.94 .084 17 289 1/25 120 .o 9.36 .061 1/26 200.0 11.00 .085 1/27 200.0 10.31 .085 18 269 1/28 240:0 9.80 .081 1/29 240.0 9.05 .095 19 302 1/30 280.0 6. 72 .061 Avg 10.78 .120 Total 9800.0 5633

(

WIN:-83 41

-c

Table 9

Daily Press.Filtrate and Wash Data .Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Precip Pre.ss Filtrate ComEosite Water Wash Date No. g

u

₃

o

₄₃

Ll

g .C.l/1 ··~ MgS04·>·lb g

u

₃

o

₈₁₁

T9s5

J .I- -' »~ 12/7 1 .006 600 .270 12/10 2 .007 600 12.5 .191 12/12 3 .005 600 30.0 .110 12/16 4 .004 600 30.0 .041 12/19 5 .002 600 30.0 .027 12/21 6 .017 600 30.0 .037 12/27 7 .001 600 30.0 .022 12/29 8 .002 600 30.0 .016 1956 1/5 9 .003 600 30.0 .021

c

1/8 10 .003 600 30.0 .019 1/11 11 .002 600 30.0 .033 1/14 12 .002 600 30.0 .027 1/17 14 .OIJ7 600 30.0 .021 1/19 15 .001 600 30.0 .016 1/21 16 .008 600 30.0 .019 1/24 17 .002 600 30.0 .015 1/27 18 .002 600 30.0 .020 1/29 19 .001 600 30.0 .018 1/31 20 600 30 .o A';rg .004 600 29.1 .050

(

n

/"'",

Table 10

Daily Reagent Requirements for Precipitation .Alkaline Leach - RIP Pilot Plant

Monument Valley Ore

Reagent H

Precip Eluate Add '.n, lb After After

Date No. gal g U30s/l g V205/l H2S04 !:!gQ H2S04 Add'n Mg0 Add'n

195.5 12/7 1 550 11.67 .061 75.40 14.0 2.4 7.6 12./10 2 550 9.76 .010 54.98 14.0 2.5 7.8 12/12 3 550 10.74 .160 75.88 11.5 2.5 7.3 12/16 4 550 9.85 .210 60.59 15.0 2.5 7.7 12/19 5 550 11.05 .207 69.36 18.~ 2.5 7.4 12/21 6 550 10.01 .252 66.59 14.5 2.2 7.8 12/27 7 550 11.05 .263 60.96 14.5 2.5 7.8 12/29 8 550 11.30 .193 70.99 14.0 2.5 7.3 1956 1/5 9 550 11.96 .162 76.38 14.0 2.5 7.3 1/8 10 550 11.34 .64.63 13.8 2.5 7.6 1/11 11 550 11.51 .170 70.42 13.5 2.5 7.2 1/14 12 550

_{._ll,AO}

.126 65.89 12.5 2.5 7.2 1/16 13 550 7.44 .168 53.53 12.5 2.5 7.2 1/17 14 550 8.26 51.41 12.0 2.5 8.4 1/19 15

;;so

6.98 .175 47.24 12.0 2.5 7.2 1/21 16 550 10.44 .180 58.02 14.0 2.5 8.8 1/24 17 550 9. 70 65.36 17.0 2.5 9.0

·~

1/27 18 550 9.58 .196 60.99 13.8 2.5 7 .. 3 _""'"'~ 1/29 19 550 5.79 59.45 14.0 2.3 7.5 N I <XI 1/31 20 550 51.16 12.0 2.5 8.8 I W Avg 550 9.88 .169 62.99 13.8 2.5 7.7

c

Date No. 1955 12/7 1 12/10 2 12/12 3 12/16 4

c

12/19 5 12/21 6 12/27 7 12/29 8 1956

175

9 1/8 10 1/11 11 1/14 12 1/16 13 1/17 14 1/19 15 1/21 16 1/24 17 1/27 18 1/29 19 1/31 20 Avg Total

(

Table 11

Daily Yellow Cake Assays Alkaline - RIP ·Pilot Plant

Monument Valley Ore

PreciJ2itation

%

u3oa U3Qa, 1b % .V:i!;QS:

69.14 52.13 0.57 74.61 43.76 0, 70 76.30 48.67 1.32 78.31 44.94 1.63 77.61 50.52 1.63 74.18 45.69 1.76 75.22 50.55 1.68 70.12 51.72 1.21 71.18. 54.72 1.08 79.98 51.89 1.18 72.88 52.60 1.19 77.02 38.40 1.31 71.63 33.97 1.26 75.61 33.74 1.63 66

.&7·

31.92 0.24 75.60 47.74 1.63 67.85 44.39 1.16 76.27 43.82 1.27 70.27 26.50 1.47 61.63 43.33 2.47 891.00 Barrel .. No .• _{'7 •. U:;~Oa·} 1 73.8 2 74.1 3 73.0 4 70.2 5 69.2 6 60.8 70.2 WIN-83 43

-%.

v2os 1.

Zf>

1.60 1.11 1.34 1,~4 2.04

-

--1.46