ENGINEERING RESEARCH INSTITUTE THE UNIVERSITY OF MICHIGAN ANN ARBOR SOLVENT EXTRACTION STUDIES FOR RECOVERING URANIUM AND VANADIUM FROM LOW GRADE ORES Progress Report No. 1 PRELIMINARY DESIGN OF A PILOT PLANT FOR THE EXTRACTION OF 1 KG/DAY OF U238 FROM RAW ORE H. A. OHLGREN, Project Supervisor K, S. SANVORDENKER Project D-120 March, 1956

TABLE OF CONTENTS Page LIST OF FIGURES iii ABSTRACT iv I. OBJECTIVES 1 II. INTRODUCTION 2 A. Description of the Ore 2 B. Description of the Process 2 C. Basis of Equipment Design 3 III, PILOT PLANT FOR EXTRACTION OF URANIUM FROM RAW ORE 6 A. Process Description 6 IVo PILOT PLANT ITEM LIST 10 V. PRELIMINARY EQUIPMENT SPECIFICATIONS 12 VI, MATERIAL BALANCE 17 A. Leaching Column 17 B. Extraction Column 18 C. Stripping Column 19 VII. COST ESTIMATION 20 A. Equipment Costs 20 B. Fixed Capital Investment 22 ii

LIST OF FIGURES Figure Page 1 Flowsheet of a Pilot Plant for Extraction of Uranium from. Raw Ore 9 iii

ABSTRACT This report consists of a design of a pilot plant to extract one kilogram per day of U238 from raw ore by the direct acid leaching and selective solvent extraction process. The final product consists of uranyl-chloride solution which may be processed to convert the salt into metal or recovered in the crystalline form. Process design has been based on the use of Uravan stockpile ore, leached with dilute sulphuric acid. Flexibility of operation has been provided for the following: (1) Use of any uranium ore or spent fuel, (2) Leaching with any acid such as nitric, hydrochloric or hydrofluoric, and (3) Solvent extraction with any organic solvent. Material balances for uranium and vanadium and preliminary equipment specifications have been included. The fixed capital investment for the pilot plant has been estimated at $177,000. iv

I.o OBJECTIVES The foremost objective of this paper is to present specifications for designing a pilot plant for the preparation of 1 kg/day of Uranium 238, from a Colorado Plateau raw uranium ore. The pilot plant should be flexible enough to handle spent fuel from nuclear reactors and different ores of uranium~ The extraction process for uranium by selective liquid-liquid extraction in a pulse column should be utilized in preference to a chemicalseparations process. The design should include the following: (1) Flow sheets for: (a) dissolution in HNO3, H2S04, (Aq. 7.45M) HF, (b) off-gas scrubbers, (c) extraction columns, (d) stripping columns, (e) evaporation of uranyl solutions, and (f) solvent recycle. (2) Material balances in (a) no./day, noo/hr., gph, gpd, (3) Sizes for all equipment and control.s, (4) Preliminary specifications for: vessels, structures, etc., and (5) Costs. 1

II. INTRODUCTION Plant design for the extraction of uranium from raw ore depends essentially on the nature of the ore and the separation process. A pilotplant design, however, calls for unusual flexibility of operation and for handling limiting conditions during experimentation or modifications. Certain parameters have to be fixed as a basis of design and sufficient leeway left for foreseeable changes in operation. For the present case, these parameters are (1) the ore to be processed and (2) the extraction process. A. Description of the Ore The ore selected for processing is the "Uravan" stockpile material. This is a composite sample representing a large quantity of ore, blended and stockpiled by the AEC, which will be processed in the near future. The chemical composition of the ore is as follows: U308 0.15 % V205 1.90 SiO2 87.00 CaO 1.12 MgO o.85 Fe203 o.89 A1203 3.24 P205 0.09 CO2 0.80 B. Description of the Process The process selected is direct-acid leaching of the raw ore followed by hydroflouric-acid leaching to recover the unavailable uranium. Sulphuric acid is used for dissolution. The sulphuric acid leach solution containing 2

the uranium, vanadium and other components is subjected to selective extraction with Dodecyl phosphoric acid or DDPA for the separation of uranium. The uranium is then stripped from DDPA by hydrochloric acid from which it may be recovered as a salt for metal processing. C. Basis of Equipment Design Equipment design has been based with one important factor in mind: flexibility of operation. Enough leeway has been incorporated to handle different systems and variables. It may appear at first sight that the equipment is oversized. This is the very purpose of the design. Based on Uravan ore, the sulphuric acid requirements have been calculated and the acid makeup tanks designed. In case of any other ores, or for spent fuels, various acid strengths can be prepared without trouble. The leaching unit has been provided with a flexibility far above that required for Uravan ore. Published data indicate that uranium from Uravan ore is easily dissolved by diluted acid solutions even at room temperatures. For application to ores difficult to dissolve, the leach columns have been steam jacketed and provided with reflux condensers, thus making operation at boiling solution temperatures possible. The time of digestion has been arbitrarily fixed as one hour. The design has been made with the view of probable use of spent fuel for recovery of uranium. The second leaching unit has been designed for the recovery of the unavailable uranium, by leaching with hydrofluoric acid. The second unit is identical to the first with the exception of the material of construction. This unit will also make possible the study of the HF-U system with the same plant. It is often advantageous to separate vanadium by a salt-roast process. A muffle furnace is provided for this purpose. In case this process need be studied, 3

the first leaching unit may be used for extraction with water while the second may be used for extraction with acid. Acid extract tanks have been designed for a two-day hold-up. The extraction column has been designed for operation from maximum flooding capacities to mixer-settler conditions. The number of plates is variable and the recovery of uranium with the present system is expected to be over 99%. The free space at the top is designed for 15 minute phase separation time at the maximum flooding capacity, viz, 3000 gal/hr sq ft. The pumps used have variable capacities which may be controlled by a by-pass system and have the capacities corresponding to the throughputs of the extraction column. The stripping column handles comparatively a much smaller volume of liquid in the present case of Uravan ore and the organic solvent. However, the design has been based so as to accommodate any new system for experimentation and hence is made identical to the extraction column. For the present case, the stripping column will be operated for only about 1-1/2 hrs. a day. This may appear to be a form of idling of equipment, but would facilitate experimentation with new systems. A solvent-processing unit has been introduced for purifying the solvent for recycle and for separating out the unstripped materials. The volume of the acid solution from the stripper is so small that the concentration of uranium and recovery could be carried out in glass equipment on a bench scale. However, in case spent fuel is processed, an evaporator, condenser, etc., will be required and provision has been made on that basis. With the present system,.87 tons of ore processed per day for the recovery of about 1 kg U238/day, the concentration of uranium in the strip solution is about 122 g/l. The total volume of the strip solution is about 2-1/4 gallons/day which, being a small amount, could be stored in ten-gallon bottles. 4.

The further processing can be done on a batch scale rather than a continuous one. This would eliminate the entire "U concentration unit" for this particular system.

III. PILOT PLANT FOR EXTRACTION OF URANIUM FROM RAW ORE A. Process Description Process description will be read in conjunction with the flowsheet. The acid-leach process followed by solvent extraction is selected for the uranium extraction. The pilot plant broadly consists of (1) Leaching Unit I, (2) Leaching Unit II, (3) Extraction Unit, (4) Stripping Unit, (5) Solvent Processing Unit, and (6) Solution Concentration Unit. 1. Leaching Unit I This unit consists of an acid make-up tank (310-1), a preheater (212-1), a raw-ore feed-hopper (530-1), a leaching column (105-1), a reflux condenser (202-1), a cooler (105-1), a rotary filter (451-1), an ore receiver (550-1), and an acid-extract tank (501-1) with a diaphragm pump (400-1). The leaching solution which could be either sulphuric or nitric acid is made up in the acid make-up tank (310-1) and preheated to a temperature of 176~F in the heater (212-1). The temperature of the outgoing acid solution is maintained constant with a temperature control (601-1) in the heater. This acid solution is continuously fed to the leaching column (105-1). The raw ore ground to the required size is fed to the column from a raw-ore feedhopper (530-1). The leaching column is operated at the boiling point of the solution and heated by low-pressure steam. The digesting time is about one hour. The overhead vapors are condensed in the reflux condenser (202-1). The condensate is returned to the column and the noncondensibles vented to the stack. Compressed air may be bubbled through the column as an oxidizing agent and for stirring purposes. 6

The slurry from the leaching column is continuously removed, sent to the cooler (211-2) prior to being filtered in the rotary filter (451-1). The solids which contain the "unavailable uranium" are dumped in the ore receiver (550-1), dried in a compartment drier (700-1) and stored for use in the second leach column to recover the rest of the uranium. The filtrate containing the U308 in solution is stored in the acid extract tank (501-1) and pumped to the solvent-extraction column (100-1). 2. Leaching Unit II This unit is identical to Leaching Unit I except that the material of construction is selected to resist the corrosive action of hydrofluoric acid. The slurry from the Leaching Column II (105-2) after cooling in the cooler (211-2) is separated in a "raffinate receiver and ore separator" (550-2) where the waste ore and the acid solution are separated by gravity. The clear solution is stored in the acid-extract tank (501-2) and sent for chemical separation of uranium. To provide experimental flexibility, the raw ore may be roasted in the muffle furnace (300-1) before leaching. In such a case, the Leaching Unit I may be used for extraction of ore with water and Leaching Unit II may be used for extraction with acid. The same filter may be used for the solid separation and the extracts may be mixed or pumped individually to the Solvent Processing Unit. 3. Extraction Unit The extraction unit consists of a pulse-plate column (100-1) with a pulser (410-1) generating variable types of pulses, a stripped solution storage tank (500-1) and an organic extract-storage tank (500-2). The acid extract is fed to the top of the pulse column and the solvent to the bottom. The stripped-acid solution is removed from the bottom 7

and stored in the stripped-solution tank (500-1) for recovery of vanadium. The organic phase rich in uranium is removed from the top and stored for use in the stripping column. The extraction column is designed for the study of pulsecolumn variables. The nature of pulsation, the number of plates, plate spacing, etc. may be varied at will. The organic solvent may be selected on the basis of the acid used for leaching. In the present case where sulphuric acid is used for leaching,.1 M DDPA in kerosene serves as an ideal solvent. 4, Stripping Unit The stripping unit consists of the strip-makeup tank (310-3), the pulse column (100-2) with a pulse generator (410-2), and an acid solution storage tank (500-3). The organic phase is fed at the bottom of the column and the stripping solution is fed to the top of the column. The stripped organic phase is removed at the top and sent to the solvent processing unit. The acid solution, rich in uranium, is removed from the bottom and stored in the uranium-rich acid-solution tank for concentration of the uranium solution and for recovery of the acid. 5. Solvent-Processing Unit The solvent-processing unit has essentially been provided for experimental facility. It consists of a series of mixer settlers (300-1, 300-2, and 300-3) where the solvent is treated with caustic acid and water or any washing solvent desired. The solvent is then recirculated to the extraction column. 6. Uranium-Concentration Unit This consists of an evaporator (203-1), condenser (202-3), a uranyl solution storage tank (501-3) and acid-recycle solution tank (501-4). The solution is evaporated to increase the uranium concentration and to recover the acid used in the strip solution. The recovered acid may then be recycled to the stripping column. The uranium in solution is stored and may be processed for metal recovery or for separation as a salt. 8

TO STACK TO STACK TO STACK ONCE LEACHED ORE,CI RECYCLE WATER WATER WATER HCI MAKE UP IPCAUSTIC T ACID HSO, URAVANS MUFFLE FURNACE RAW ORE IN G LEACH I 1 STRIP 12AUSTIC - 2 WATE~ ~.~.~ Coo-I IO P I I ~ACID FEEDERRE FEEDER MAKE UP IAKE OP MAKE UP MAKE OP 530-1 MAKE P O - 310-3 310-4 310-S _310I1 1 | | 211-2 530-2 -I W LC AFI AFI 634-1 AFI 634-2 621 1 621-2 P621-4 REFLUX IREFLUX CONDENSER I CONDENSER 20 2-1 202-2.J TO SOLVENT PROCESSING I G +l........... aA I HEATER 0 RICH FEED 10 M I n NON COND. NIGASES GASES MIXER SETTLERS STEAM T CSTEAM FIAFPI EXTRACTION EXTRACTION 300- 002 00 COLUMN T CORP AIR COLUMN CO AIR 10ACTION5-1 105-2 PIC ti,~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~TAK500-5 500-6 500-7 COOLER COL OLERG. TO 2nd LEACHIN 211-1 O0- I I00 2- "SOLVENT REICLE TO VANADIUM RECOVERY U C FILTER RAFFINATE 410-1 410-2 STEAM CONDENSER RECEIVER 550-2 ORE I PIC URANYL SOLN.TO EVAP. MAKE UP ACID IDSTRIPPED ORGANIC U RICH ACIDCONC, U EXTRACT E C~L~I hi I I I EXTRACT SOLUTION EXTRACTI RECYCLE 501-1 501-2 500-1 l 500-2 o500-3 /500-4 501DIA. PUMP I 1 DIA. PUMP CENT PUMP DIA. PUMP CENT PUMP U P 400I1 400-2 401-1 400-3 401-2 - TO CHEMICAL SEPARATION OF U TO U SEPARATION a METAL PROCESSING TO VANADIUM RECOVERY I TO HCI RECOVERY FIG. I FLOW SHEET OF A PILOT PLANT FOR EXTRACTION OF URANIUM FROM RAW ORE

IV. PILOT PLANT ITEM LIST Item No. Description 100-1 Pulse plate column for extraction. 100-2 Pulse plate column for stripping. 105-1 Leaching Column I with steam jacket. 105-2 Leaching Column II with steam jacket. 202-1 Reflux condenser for leaching Column I. 202-2 Reflux condenser for leaching Column II. 202-3 Reflux condenser for evaporator. 203-1 Evaporator for uranyl solution. 212-1 Heater, steam coil type for acid solution. 212-2 Heater, steam coil type for acid solution. 211-1 Double pipe heat exchanger (acid resisting). 211-2 Double pipe heat exchanger (karbate material ). 300-1 Mixer settler. 300-2 Mixer settler. 300-3 Mixer settler. 310-1 Acid make-up tank. 310-2 Acid make-up tank (HF resisting). 310-3 Acid make-up tank. 310-4 Caustic make-up tank. 310-5 Acid make-up tank. 400-1 Acid extract pump (diaphragm type). 400-2 Acid extract pump (diaphragm type). 400-3 Acid extract pump (diaphragm type). 400-4 Acid recycle pump (diaphragm type). 401-1 Organic extract pump (centrifugal). 401-2 Solvent recycle pump (centrifugal). 410-1 Variable pulse generator. 410-2 Variable pulse generator. 451-1 Rotary filter (acid resisting). 10

Item No. Description 500-1 Stripped acid solution storage tank. 500-2 Organic extract solution storage tank. 500-3 Rich acid extract solution storage tank. 500-4 Solvent recycle tank. 500-5 Caustic wash solution tank. 500-6 Acid wash solution tank. 500-7 Aqueous wash solution tank. 501-1 Acid extract storage tank. 501-2 Acid extract storage tank. 501-3 Uranyl solution storage tank. 501-4 Acid recycle solution storage tank. 530-1 Raw ore feed hopper. 530-2 "Once leached ore" feed hopper. 550-1 Ore receiver. 550-2 Raffinate receiver. 601-1 Temperature control (indicating type, item no. 212-1). 601-2 Temperature control (indicating type, item no. 212-2). 614-1 Pressure controller (steam; item no. 105-1). 614-2 Pressure controller (steam; item no. 105-2). 614-3 Pressure controller (steam; item no. 203-1). 614-5 Pressure controller (air; item no. 105-1). 614-6 Pressure controller (air; item no. 105-2). 621-1 Flow indicator (area type; item no. 310-1). 621-2 Flow indicator (area type; item no. 310-2). 621-3 Flow indicator (area type; item no. 100-1). 621-4 Flow indicator (area type; item no. 310-3). 634-1 Level controller, item no. 100-1. 634-2 Level controller, item no. 310-3. 700-1 Air compartment dryer. 800-1 Gas muffle furnace. Total number of items (59). 11

V. PRELIMINARY EQUIPMENT SPECIFICATIONS Vessels a. Leaching Column - Item nos. 105-1 - 105-2 No. required - 2 (two) Type - Solid-liquid extraction column, steam jacketed Size - 1.25' I. D. 6.5' Height Steam Jacket - Bottom to 1' from top Operating pressure - Atmospheric Operating temp. - 300 F Material of construction - 1) Glass lined steel 2) Rubber lined steel b. Extraction column - Item nos. 100-1 - 100-2 No. required - 2 (two) Type - Pulse plate column Diameter of column - 2.5" Height - 8 Headers (top and bottom) Diameter - 12" Height - 12" Plate adjusting device - Center rod, threaded (st. st.) Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - Glass c. Acid-Makeup Tank - Item nos. 310-1 - 310-2 No. required - 2 (two) Type - Vertical with mech. agitator Size - I. D. = 3' H = 2.25' Capacity - 125 gal. Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - Steel, glass lined d. Preheater - Item nos. 212-1 - 212-2 No. required - 2 (two) Type - Vertical glass lined with steam coil, automatic temp. control Capacity - 62.5 gal. Steam coil area for heat transfer - 2.35 sq. ft. Duty - 17,500 Btu/hr. Operating pressure - Atmospheric Operating temp. - 200~F Material of construction - 1) steel, glass lined 2) steel, rubber lined 12

e. Ore Feed Hopper - Item nos. 530-1 - 530-2 No. required - 2 (two) Type - Conical, ( L = D ) Size - D = 3.5' L = 3-5' Material of construction - C. I. f. Reflux Condenser - Item nos. 202-1 - 202-2 No. required - 2 (two) Duty - 61,500 Btu/hr. Area of heat transfer - 6 sq. ft. Type - Shell and tube Operating pressure - Atmospheric Operating temp. - 212~F Material of construction - 1) steel shell, st. st. tubes 2) steel shell, karbate tubes g. Cooler - Item nos. 211-1 - 211-2 No. required - 2 (two) Type - Shell and tube Duty - 25,000 Btu/hr. Area of heat transfer - 15 sq. ft. Operating pressure - Atmospheric Operating temp. - 212~F Material of construction - 1) steel shell, st. st. tubes 2) steel shell, karbate tubes h. Ore Receiver - Item no. 550-1 No. required - 1 (one) Type - Vertical tank, open (vat) Size - I. D. = 3.0' L = 2.5' Material of construction - Wood i. Acid Extract Storage Tank - Item nos. 501-1 - 501-2 No. required - 2 (two) Type - Horizontal with cooling coils Size - I. D. = 3.5' L = 5.5' Capacity - 350 gal. Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - 1) glass lined steel 2) rubber lined steel j. Raffinate Receiver and Ore Separator - Item no. 550-2 No. required - 1 (one) 13

Type - Vertical with slanting bottom Size - D = 3' H 5.5' Capacity - 250 gal. Material of construction - Rubber lined steel k. Stripped Acid Solution Tank - Item no. 500-1 No. required - 1 (one) Type - Horizontal Size - I. D. = 3.5' L = 5.5' Capacity - 330 gal. Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - Glass lined steel 1. Organic Extract Tank - Item no. 500-2 No. required - 1 (one) Type - Horizontal Capacity - 150 gal. Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - Steel m. Uranium Rich Acid Solution Tank - Item no. 500-3 No. required - 1 (one) Type - Horizontal Capacity - 60 gal. Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - Glass lined steel n. Solvent Recycle Tank - Item no. 500-4 No. required - 1 (one) Type - Horizontal Capacity - 200 gal. Operating pressure - Atmospheric Operating temp. - Room temp. Material of construction - Steel o. Conc. Uranium Solution Tank - Item no. 501-3 Capacity - 25 gal. Type - Vertical Material of construction - Porcelain 14

p. Solvent Recycle Tank - Item no. 501-4 Capacity - 25 gal. Material of construction - Glass or porcelain q. Mixer Settlers - Item nos. 300-1 - 300-2 - 300-3 No. required - 3 (three) Capacity - 16.7 gal. Material of construction - Stainless steel r. Strip Solution Makeup Tank - Item no. 310-3 No. required - 1 (one) Type - Vertical with agitator Capacity - 25 gal. Material of construction - Porcelain s. Evaporator - Item no. 203-1 Type - Steam jacketed, open pan type, with dished top and condenser. Area of heat transfer - 3 sq. ft. Duty - 10,000 Btu/hr. Size - 1.5' D., hemispherical Material of construction - Jacketed, glass lined steel 2. Auxiliary Equipment a. Air Dryer - Item no. 700-1 No. required - 1 (one) Type - Compartment dryer, with air blower, electrical coils for heating, damper for air rate adjustment, shelves for solids handling. Size - 4' x 2' x 4' L D H Duty - 173,000 Btu/day Material of construction - Stainless steel b. Rotary Filter - Item no. 451-1 No. required - 1 (one) Type - Vacuum connection, washing arrangements, etc. (oliver filter). Capacity - 21 gal/hr filtrate Size - D = 1' L = 1' Filter cloth - Tafflon Area - 3.14 sq. ft. Material of construction - Stainless steel 15

c. Gas Muffle Furnace - Item no. 800-1 No. required - 1 (one) Dimensions - 2.5' x 2' x 3' Type - Gas muffle, oxidizing atmosphere Operating temperature - 800~C 3. Mechanical Equipment a. Diaphragm pump - Item nos. 400-1 - 400-2 No. required - 2 (two) Capacity - 20-100 gal/hr. Head required - 20' Material of construction - Stainless steel b. Centrifugal Pump - Item nos. 401-1 - 401-2 No. required - 2 (two) Capacity - 10-50 gal/hr. Head required - 20' Material of construction - Steel c. Pulse Generator - Item nos. 410-1 - 410-2 No. required - 2 (two) Type - Variable pulse, amplitude, and frequency d. Diaphragm Pump - Item nos. 400-3 - 400-4 No. required - 2 (two) Capacity - 20 gal/hr. Head required - 20' 16

VI. MATERIAL BALANCE A. Leaching Column FEED Stream nent lbs/day lbs/hr. kg/day g/hr. gal/hr. gal/day litres/hr. Ore U38 2.6.325 1.18 147.5 - - - 308 V205 33.0 4.125 14.95 1,856 Others 1,700 212.5 735.9 91,996 - - - Total 1,736 217 752.0 94,000 - - - Acid H20 1,330 166.25 603 75,370 19.9 159.5 75.2 H2SO4 70 8.75 31.75 3,970 1.0 7.5 3.78 Total 1,400 175 639.75 79,300 20.9 167 79 PRODUCT Stream Compo- lbs/day lbs/hr. g/hr. gal/hr. gal/day lbs/gal g/1 nent Ore U308 0.08.010 4.53 -. (Raffi.. nate) V205 16.55 2.062 935.3 - - Acid Solution 1,400 175 79,380 20.9 167 8.42 1.01 (Ex- U208 2.52.315 142.9 - -.0151 1.809 tract) v2o05 16.55 2.o62 935.3 - -.0987 11.84 Total 1,419 177.38 80,458 20.9 167 - 17

B. Extraction Column FEED CompoStream nent lbs/day lbs/hr. g/hr. gal/hr. gal/day lbs/gal g/l Acid olution 1, 400 175 o9,380 20.9 167 8.42 1.01 U08 2.52 ~ 315 i 142.9 - -.0151 1.809 V20o5 16.55 2.062 935.3 - -.0987 11.84 Total 1,419 177.38 0,458 20.9 167 - - Organic Solvent 236.5 29.6 1,343 4.18 33.5 7.08 0.85 PRODUCT CompoStream |nent lbs/day lbs/hr. g/hr. gal/hr. gal/day lbs/gal g/1 Acid Solution 1,400 175 79,380 20.9 167 8.42 1.01 nate) U3affi 08.024.003 1.36 - -.00014.017 nate) U308 V205 15.49 1.935 878 - -.0926 11.1 Total 1,415.5 176.9 80,259 20.9 167 - - Organic Solvent 236.5 29.6 1,343 4.18 33 5 7.08. 85 tract) V o5 1.06.127 57.6 - -.0162 1.95 Total 240 30.04 1,542.1 4.18 33.5 - - 18

C. Stripping Column FEED Stream Component lbs/day lbs/hr. g/hr. gal/hr. gal/day lbs/gal g/1 Organic Solvent 236.5 29.6 13,430 4.18 33.5 7.08.850 U308 2.496.312 141.5 -. 0398 4.78 V205 1.06.127 57.6 - -.0162 1.95 Total 240.1 30.0 13,600 4.18 33.5 - Acid Solution 24.01 3.0 1,360.305 2.44 9.83 1.180 PRODUCT Stream Component lbs/day lbs/hr. g/hr. gal/hr. gal/day lbs/gal g/l Organic Solvent 236.5 29.6 1,343 4.18 33.5 7.08.850 (Raffi- 1U308 0.025.003 1.34 - -.0007.085 nate) |2 5 Total 236.53 29.6 1,344 4.18 33.5 - - Acid Solution 24.01 3.0 1,360.305 2.44 9.83 1.18 (Extractl U308 2.471.309 140.16 - - 1.011 121.5 V205 1.06.127 57.6 - -.417 50 Total 27.56 3.436 1,557.8 ~305 2.44 - - Total U238/day = (2.471 ibs) (.4536 kg ) (714 U3 kg/day - ~.99 kg/day 19

VII. COST ESTIMATION A. Equipment Costs Item No. Description Material of Construction Cost $ Total $ 100-1 Pulse plate column Glass 600 100-2 Pulse plate column Glass 600 1,200 105-1 Leaching column Glass lined steel 2,500 105-2 Leaching column Rubber lined steel 2,500 5,000 202-1 Reflux condenser Steel shell st. st. tubes 600 202-2 Reflux condenser Steel shell st. st. tubes 600 202-3 Reflux condenser Steel shell st. st. tubes 300 1,500 203-1 Evaporator Jacketed, glass lined 1,000 1,000 212-1 Heater with steam coils Glass lined steel 1,000 212-2 Heater with steam coils Rubber lined steel 1,000 2,000 211-1 Heat exchanger Steel shell, st. st. tubes 1,000 211-2 Heat exchanger Steel shell, karbate tubes 1,000 2,000 300-1 Mixer settler Stainless steel 300 300-2 Mixer settler Stainless steel 300 300-3 Mixer settler Stainless steel 300 900 310-1 Acid makeup tanks Glass lined steel 1,250 310-2 Acid makeup tanks Glass lined steel 1,250 310-3 Acid makeup tanks Porcelain 300 310-4 Acid makeup tanks Porcelain 200 310-5 Acid makeup tanks Porcelain 200 3,200 400-1 Diaphragm pumps 200 400-2 Diaphragm pumps 200 400-3 Diaphragm pumps 200 400-4 Diaphragm pumps 200 800 401-1 Centrifugal pump Steel 200 401-2 Centrifugal pump Steel 200 400 410-1 Pulser 1,000 410-2 Pulser 1,000 2,000 451-1 Rotary filter st. st. 2,500 2,500 500-1 Acid solution storage tank Glass lined steel 2,000 500-2 Organic solvent tank Steel 350 500-3 Acid extract tank Glass lined steel 1,000 500-4 Solvent recycle tank Steel 500 500-5 Caustic solution tank Porcelain 200 500-6 Acid solution tank Porcelain 200 500-7 Aqueous solution tank Porcelain 200 4,450 20

Equipment Costs (continued) Item No. Description Material of Construction Cost Total 501-1 Storage tanks Gass lined. steel 2,000 501-2 Storage tanks Rubber lined steel 1,500 501-3 Storage tanks Porcelain 200 501-3 Storage tanks Porcelain 200 3,900 530-1 Feed hopper C. I. 300 530-2 Feed hopper C. I. 300 600 550-1 Ore receiver Wood 50 550-2 Raffinate receiver Rubber lined steel 1,250 1,300 700-1 Air dryer Stainless steel 1,500 1,500 800-1 Muffle furnace 2,000 2,000 Total Equipment Cost $36,250 21

B. Fixed Capital Investment Purchased Equipment Cost $ 36,250 Installation cost, (43% equipment cost) 15,160 Instrumentation 2,500 Piping, (86% equipment cost) 30,500 Installation cost for piping (43% piping cost) 13,100 Electrical auxiliaries, (10% equipment cost) 3,600 Buildings, (80o equipment cost) 28,200 Utilities, (20% equipment cost) 7,250 TOTAL $ 139,460 Physical plant cost $ 140,000 Engineering and construction, (15% physical cost) 21,000 Direct plant cost $ 161,000 Contractor s fee 16,000 TOTAL $ 177,000 Fixed Capital Investment $ 177,000 22